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Biofiltration Technology
For
Effective Control of Air Emissions
George A. Sorial
Department of Civil and Environmental Engineering
University of Cincinnati
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IntroductionIntroduction
Theory of the StudyTheory of the Study
ObjectivesObjectives
Materials and MethodsMaterials and Methods
ResultsResults
SummarySummary
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VOCsVOCs ? ?
Volatile organic compounds (VOCs)
They are found in the waste stream emitted from most processes employing organic or petroleum based solvents.
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1. The passage of the 1990 Amendments to the Clean Air Act:
significantly heightened the interest in the development of innovative
technologies for VOCs removal.
2. VOCs are precursors to the formation of ozone,
and they have their own toxicity.
3. International standard on environmental management (ISS14000):
demands the treatment of VOCs emission
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1. Source of VOCs to ambient atmosphere.
affected by the Clean Air Act Amendments.
2. Depends on domestic, commercial, and industrial sources
3. VOCs are transferred into the air mainly in case of aerated bioreactor.
(activated sludge process)
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1. Thermal oxidation, Catalytic oxidation,
Condensation, Carbon adsorption,
Membrane separation…
2. Biological treatment:
economical and ecological technology
3. Biofiltration
Clean air
VOC
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Biological Treatment6.0%
Catalytic Oxidation28.0%Thermal Oxidation
8.0%
Adsorption36.0%
Absorption19.0%
Condensation3.0%
Air Treatment Processes
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Biofiltration
Basic Design Principles
Support Media
Nutrients
Moisture
pH Control
Adequate Oxygen Level
Temperature
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TYPES OF BIOFILTERS
Classical Biofilters Biotrickling Filters orTrickle Bed Biofilters
Natural Organic Media Synthetic Media
Peat Compost Leaveswoodbark soil Inorganic Plastic
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1. Owner and location: Novartis; Basle, Switzerland
2. Air flow rate: 60,000 – 75,000 m3/h(Exhaust air from plant)
3. Pollutants: toluene, xylene, methanol, isopropanol, chloroform... Total conc. : 180 – 500 mg/m3
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4. Biofilter DesignInvestment costs ($2,000,000)Treatment costs
($1.44 per 1000 m3 off gas)
5. Biofilter PerformanceRemoval: 80 %
(depends on inlet loading)
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CLASSICAL BIOFILTERS
NATURAL ORGANIC MEDIA
Demonstrated Characteristics:
Loading limited (degradation rate of the medium is much higher than the VOC degradation rate. The VOC input has minor effect on microbial activity)
Sensitive to moisture content
Very sensitive to temperature
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Biofilter Applications History
Pre 1990: Principally for Nuisance Odor ControlSewage Treatment Odors Livestock Raising , Processing, and Rendering Flavors and Fragrances: Extraction / Processing Commercial Composting
Post 1990: Developed for VOC / Volatile Toxics ControlGroundwater Remediation: Vacuum Extraction VentingFibers Processing: Rayon FiberIndustrial Finishing : Painting, Lacquering, PrintingCommercial Fermentation: Bakeries, Breweries
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Conceptually identical process to the Conceptually identical process to the biofilterbiofilter• Microbial attachment: Synthetic inorganic or polymeric media• Intermittent delivery of Nutrient & Buffer to the media
Consistent Nutrient & pH controlConsistent Nutrient & pH controlOptimizing the waste utilizing kineticsOptimizing the waste utilizing kinetics
• Consistent• Long-term • High
Removal PerformanceRemoval Performance
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•Transient loading
• VOCs composition
• Emission mode: non-use periods
• Biomass accumulation
• Microbial activity
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Performance of Pelletized Biofilter at 1 and 2 Minutes EBRT without Backwashing
Sequential Date, days
0 20 40 60 80 100 120 140
Pre
ssu
re D
rop
, cm
wat
er
0
10
20
30
40
50
60
70
80T
olu
ene
Rem
ova
l Eff
icie
ncy
, %
0
10
20
3040
5060
7080
90100
Efficiency
Pressure Drop
Toluene Loading: g/m3h
11.1 oC 15.6 oC 21.1 oC 26.7 oC
2 min EBRT 1 min EBRT
6.13 12.3 24.5(50 ppmv) (50 ppmv) (100 ppmv)
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Solution
In situ up-flow washing with water, i.e., backwashing at a rate sufficient to fluidize themedia and permit rapid removal of excessbiomass growth
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IMPACT of NUTRIENT-N SPECIES
The relative performance of two biofilters was evaluated by varying the form of nutrient nitrogen
Nitrate-N vs Ammonia-N:
Nitrate-N fed biofilter demonstrated the following advantages:
Better steady state performance (overall)
Better recovery after backwash with time
Better removal with depth
Lower microbial yield (about 40% less)
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Effect of stepEffect of step--change in influent concentration (Phase I)change in influent concentration (Phase I)
Effect of nonEffect of non--use periods (Phase I)use periods (Phase I)
Effect of interchanging the feed Effect of interchanging the feed VOCsVOCs (Phase II)(Phase II)
Effect of Varying Effect of Varying VOCsVOCs composition (Phase III)composition (Phase III)
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Reactor : Independent labReactor : Independent lab--scale TBABscale TBAB
Media: Media: pelletizedpelletized biological support mediabiological support media
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Effluent Water
AirN2 + O2
VOCsParticulatesWaterCO2
S
S
S
S
S
S
S Sampling Location
VOCs
Effluent Air
7
3
1
4
2
5
6
8
1. Electronic Air Cleaner2. Mass Flow Controller3. Syringe Pump4. Nutrient Feed Control System5. Nutrient Feed Tank6. Spray Nozzle7. Trickle Bed Biofilter8. Pelletized Media
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Characterizing TBAB PerformanceCharacterizing TBAB Performance
Determination of critical loadingDetermination of critical loading
Impact of nonImpact of non--use periods on performanceuse periods on performance
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Feed VOCs
1.090.283.162.58Log Kow
0.000620.001940.1090.280K’H
Methyl isobutyl ketone (MIBK)
Methyl ethyl ketone (MEK)
StyreneToluene
Hydrophilic compoundsHydrophobic compounds
K’H = dimensionless Henry’s law constant, Kow = Octanol-water partition coefficient
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Experimental ConditionsExperimental Conditions
0.760.760.760.761.51 1.51 ~~ 2.022.021.231.23EBRT,EBRT,minmin
1.09 1.09 ~~ 5.435.430.7 0.7 ~~ 7.037.030.64 0.64 ~~ 3.173.170.7 0.7 ~~ 7.037.03Loading rateLoading ratekg COD/mkg COD/m33··ddayay
50 50 ~~ 25025050 50 ~~ 50050050 50 ~~ 33033050 50 ~~ 500500Inlet Conc.,Inlet Conc.,
ppmvppmv
MIBKMIBKMEKMEKStyreneStyreneTolueneToluene
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Results Results –– VOC removal capacity (Backwashing)VOC removal capacity (Backwashing)
Aromatic compoundsAromatic compounds
TolueneToluene•• Critical loadingCritical loading
3.5 kg COD/m3.5 kg COD/m33··dayday
(46.6 g/m(46.6 g/m33··hr)hr)
•• Maximum removal capacityMaximum removal capacity
6.0 kg COD/m6.0 kg COD/m33··dayday
(79.9 g/m(79.9 g/m33··hr)hr)
Loading rate, kg COD/m3day
0 2 4 6 8
Rem
oval
rat
e, k
g C
OD
/m3 da
y
0
2
4
6
8
Toluene100% Removal
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Results Results –– VOC removal capacity (Backwashing)VOC removal capacity (Backwashing)
Aromatic compoundsAromatic compounds
StyreneStyrene•• Critical loadingCritical loading
1.9 kg COD/m1.9 kg COD/m33··dayday
(25.8 g/m(25.8 g/m33··hr)hr)
•• Maximum removal capacityMaximum removal capacity
2.7 kg COD/m2.7 kg COD/m33··dayday
(36.6 g/m(36.6 g/m33··hr)hr)
Loading rate, kg COD/m3day
0 2 4 6 8
Rem
oval
rat
e, k
g C
OD
/m3 da
y
0
2
4
6
8
StyreneToluene100% Removal
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Results Results –– VOC removal capacity (Backwashing)VOC removal capacity (Backwashing)
Oxygenated compoundsOxygenated compounds
MEKMEK•• Critical loadingCritical loading
5.6 kg COD/m5.6 kg COD/m33··dayday
(95.6 g/m(95.6 g/m33··hr)hr)
•• Maximum removal capacityMaximum removal capacity
5.9 kg COD/m5.9 kg COD/m33··dayday
(100.7 g/m(100.7 g/m33··hr)hr)
Loading rate, kg COD/m3day
0 2 4 6 8
Rem
oval
rat
e, k
g C
OD
/m3 da
y
0
2
4
6
8
MEKTolueneStyrene100% Removal
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Results Results –– VOC removal capacity (Backwashing)VOC removal capacity (Backwashing)
Oxygenated compoundsOxygenated compounds
MIBKMIBK•• Critical loadingCritical loading
4.3 kg COD/m4.3 kg COD/m33··dayday
(65.9 g/m(65.9 g/m33··hr)hr)
•• Maximum removal capacityMaximum removal capacity
4.9 kg COD/m4.9 kg COD/m33··dayday
(75.1 g/m(75.1 g/m33··hr)hr)
Loading rate, kg COD/m3day
0 2 4 6 8
Rem
oval
rat
e, k
g C
OD
/m3 da
y
0
2
4
6
8
MIBKTolueneStyreneMEK100% Removal
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Results Results –– Comparison of VOC removal capacityComparison of VOC removal capacity
VOC Loading/Removal Rate, kgCOD/m3day
0 2 4 6 8
Toluene
Styrene
MEK
MIBK
Loading
5.43
7.03
3.17
7.03
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Results Results –– VOC removal capacityVOC removal capacity
VOC Loading/Removal Rate, kgCOD/m3day
0 2 4 6 8
Toluene
Styrene
MEK
MIBK
LoadingBackwashing5.43
7.03
3.17
7.03
4.34
5.64
1.9
3.52
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Results Results –– VOC removal capacityVOC removal capacity
VOC Loading/Removal Rate, kgCOD/m3day
0 2 4 6 8
Toluene
Styrene
MEK
MIBK
LoadingBackwashingNon-use Period
5.43
7.03
3.17
7.03
4.342.17
4.35.64
1.271.9
3.52
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Results Results –– Critical loading vs. Critical loading vs. KowKow
Kow (octanol-water partition coefficient)
0.1 1 10 100 1000 10000
Cri
tica
l loa
ding
, kg
CO
D/m
3 day
1
2
3
4
5
6
7
Toluene
MIBK
MEK
Styrene
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SummarySummary
1.1. Up to the critical VOC loading rate, the backwashing was effectiUp to the critical VOC loading rate, the backwashing was effective ve biomass control to attain consistently high removal performance.biomass control to attain consistently high removal performance.
2.2. NonNon--use periods can be considered as another means of biomass use periods can be considered as another means of biomass control at lower VOC loading rate. control at lower VOC loading rate.
3.3. ReacclimationReacclimation was a critical factor in was a critical factor in biofilterbiofilter peformancepeformance. . After nonAfter non--use periods, the active biomass affects use periods, the active biomass affects biofilterbiofilter responseresponse..
Experimental findings supported the handling limitation of Experimental findings supported the handling limitation of performance of the current performance of the current biofiltrationbiofiltration systemsystem
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Operating Condition
Sequence of Feed VOCsStyrene → MEK → Toluene → MIBK → Styrene
Inlet concentration of feed VOCs50 ppmv ~ the maximum allowable inlet concentration
Flow rate• Nutrient solution: 1.5 L/day• Air: 1.35 L/min (EBRT = 2.02 min)
Biomass control : Periodic in-situ backwashingFrequency: 1 hour of duration / a week
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Biofilter Response after interchanging VOCs
Acclimation Period, min
0 60 120 1000 2000 3000
Rem
oval
Eff
icie
ncy,
%
0
20
40
60
80
100
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Biofilter Response after interchanging VOCs
Acclimation Period, min
0 60 120 1000 2000 3000
Rem
oval
Eff
icie
ncy,
%
0
20
40
60
80
100
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Biofilter Response after interchanging VOCs
Acclimation Period, min
0 60 120 1000 2000 3000
Rem
oval
Eff
icie
ncy,
%
0
20
40
60
80
100
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Biofilter Response after interchanging VOCs
Acclimation Period, min
0 60 120 1000 2000 3000
Rem
oval
Eff
icie
ncy,
%
0
20
40
60
80
100
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g C
OD
/g N
0
50
100
150
200
Sequential Date, day
0 20 40 60 80 100 120 140 160
g C
O2
/g C
OD
0
1
2
Nitrogen Utilization and CO2 Production
High N utilizationHigh CO2 /COD
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1. Need more proteins to make up the enzymes for utilizing new substrate
2. Facultative organisms: Denitrifying microorganisms
• More utilization of nitrogen
• Nitrogen utilization and CO2 Production
Study of Microbial community structure & diversityStudy of Microbial community structure & diversity
High N utilizationHigh CO2 /COD
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High removal performances were observed in the interchanging VOC-fed TBAB.
TBAB easily acclimated to hydrophilic compounds (MEK & MIBK), while TBAB acclimations to hydrophobic compound (Toluene & Styrene) were delayed for more than 45 hrs.
Right after interchanging feeding VOCs, TBAB has shown unusual performances (high nitrogen utilization & high CO2/COD).
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Adsorption unit can be a buffer unit for a biofilter
Current application : Single bed of carbon filter
Consideration of current adsorption unitHigh loading & Large fluctuation → Losing buffer capacityInitial period of operation → No contaminant in effluent
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•• Conceptually simple process to PSAConceptually simple process to PSA
•• PSA (Pressure Swing Adsorption) : PSA (Pressure Swing Adsorption) :
→→ A technology for separation and purification for gas mixturesA technology for separation and purification for gas mixtures
→→ 4 Steps for operational function4 Steps for operational function
Feeding (Adsorption)
Depressurization
Purging (desorption)
Repressurization
Regeneration
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•• Conceptually simple process to PSAConceptually simple process to PSA
•• Hypothetically, adsorption rate is equal to its Hypothetically, adsorption rate is equal to its desorptiondesorption rate rate
→→ Operational function is simplified to a Operational function is simplified to a 22--stepstep
Feeding (Adsorption)
Purging (desorption)
Regeneration
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•• Cyclic operation : Shift of air flow directionCyclic operation : Shift of air flow direction
→→ Each bed will not be fully saturated with Each bed will not be fully saturated with adsorbateadsorbate
Clockwise
A
Waste GasGas to biofilter
BA
CounterclockwiseWaste Gas Gas to biofilter
A B
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ConceptConcept
2-Bed Adsorption
Will serve asWill serve as
•• Polishing unit during the initial acclimation period of the Polishing unit during the initial acclimation period of the biofilterbiofilter
•• Buffer unit in load fluctuation Buffer unit in load fluctuation
•• Feeding source without any feeding phase during nonFeeding source without any feeding phase during non--use periodsuse periods
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Evaluate Cyclic operation of Evaluate Cyclic operation of 22--bed adsorption unitbed adsorption unit as load equalizationas load equalizationFor air For air biofiltrationbiofiltration systemsystem
•• Mathematically simulate 2Mathematically simulate 2--bed adsorption unit performance bed adsorption unit performance
to compare to compare Cyclic operationCyclic operation vs. vs. NonNon--cyclic operationcyclic operation
•• Experimentally evaluate the performance of the integrated schemExperimentally evaluate the performance of the integrated scheme ofe of
22--bed adsorption unit with air bed adsorption unit with air biofilterbiofilter under transient loading of under transient loading of
toluene (toluene (Integrated unitIntegrated unit vs. vs. control unitcontrol unit))
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Experimental MethodsExperimental Methods
2-Bed Adsorption
•• 2 Beds 2 Beds
•• Dimension : 2.5 cm (D) Dimension : 2.5 cm (D) ×× 20 cm (L)20 cm (L)
•• Duration of one cycle : 8 hoursDuration of one cycle : 8 hours
•• EBRT: 5.6 sec (2.2 L/min)EBRT: 5.6 sec (2.2 L/min)
•• AdsorbateAdsorbate : Toluene: Toluene
•• Adsorbent : GAC (BPL 6 Adsorbent : GAC (BPL 6 ×× 16)16)
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Air
1. Air cleaner2. Mass flow controller3. Syringe pump4. Equalizing tank5. Flow meter6. 2-bed adsorber7. 4-way solenoid valve8. Supplemental air valve9. Biofilter
3
4
5
6
7
8
9
12
9
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•• Model simulation of Model simulation of cyclic operationcyclic operation of 2of 2--bed adsorption bed adsorption
•• Model simulation of Model simulation of nonnon--cyclic operationcyclic operation of 2of 2--bed adsorptionbed adsorption
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Mathematical model is formulated for a packed bed for simulation of the proposed cycle, which consists of overall and component material balances. • Linear driving force model is incorporated into the model in order to include
a mass transfer resistance with an adsorbent from a bulk gas phase. • Freundlich isotherm equation is used for expression of isotherm capacity.
Assumption: (1) no pressure drop along a bed, (2) an isothermal operation, and (3) a plug flow through a bed with no dispersion.
•• Model simulation of Model simulation of cyclic operationcyclic operation of 2of 2--bed adsorption bed adsorption
•• Model simulation of Model simulation of nonnon--cyclic operationcyclic operation of 2of 2--bed adsorptionbed adsorption
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•• Model simulation of Model simulation of cyclic operationcyclic operation of 2of 2--bed adsorption bed adsorption
Plug flow homogeneous surface diffusion model (PFHSDM) which is embedded in an Adsorption Design Software (AdDesignSTM) developed by Michigan Technological University is used.
The mechanisms incorporated in this model are:• Homogeneous surface diffusion• Film transfer resistance at the adsorbent surface • Advection dominates axial transport in bed.• Local equilibrium Freundlich isotherm exists at the adsorbent surface. • Freundlich isotherm equation is used for expression of isotherm capacity.
•• Model simulation of Model simulation of nonnon--cyclic operationcyclic operation of 2of 2--bed adsorptionbed adsorption
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Transient Feeding Condition 1: Transient Feeding Condition 1: Square wave change of inlet concentration- Base = 200 ppmv- Peak = 400 ppmv (15 mins / hour)
Time, min0 60 120 180
Inle
t C
onc. CH
CL
Effluent Response in 2Effluent Response in 2--bed Adsorptionbed Adsorption
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Effluent Responds in 2Effluent Responds in 2--bed Adsorptionbed Adsorption
Critical inlet Conc.(250 ppmv) to biofilter
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Effluent Responds in 2Effluent Responds in 2--bed Adsorptionbed Adsorption
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Effluent Responds in 2Effluent Responds in 2--bed Adsorptionbed Adsorption
Exp. observation
Exp. observation
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Integrated unitIntegrated unit vs. vs. Control unit Control unit
a) Integrated unit (2-bed adsorption + biofilter)
b) Control unit (biofilter)
1 10 100 1000
Eff
luen
t, p
pmv
1
10
100
Rem
oval
, %
0
20
40
60
80
100
Sequential Time, hrs1 10 100 1000
Eff
luen
t, p
pmv
1
10
100
Rem
oval
, %
0
20
40
60
80
100
Effluent concentrationRemoval efficiency
Detection limit (0.5 ppmv)
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Results: Results: Further ApplicationFurther Application
Time, min
0 60 120 180
Inle
t C
onc.
, ppm
v
0
200
400
600
800
a)8a)8--hr average effluent b) Reaction rate constanthr average effluent b) Reaction rate constant
Feeding conditionA B C D
Rat
e co
nsta
nt, s
ec-1
0.00
0.01
0.02
0.03
Feeding conditionA B C D
Eff
luen
t, m
g/m
3
0
100
200
300
Integrated unitControl unit Control unit Peak
Base
Integrated unitPeakBase
Feeding Condition
• Type A : 46.9 g/m3·hr
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Results: Results: Further ApplicationFurther Application
a)8a)8--hr average effluent b) Reaction rate constanthr average effluent b) Reaction rate constant
Feeding conditionA B C D
Rat
e co
nsta
nt, s
ec-1
0.00
0.01
0.02
0.03
Feeding conditionA B C D
Eff
luen
t, m
g/m
3
0
100
200
300
Integrated unitControl unit Control unit Peak
Base
Integrated unitPeakBase
Feeding Condition
• Type B : 46.9 g/m3·hr(High Peak)
Time, min
0 60 120 180
Inle
t C
onc.
, ppm
v
0
200
400
600
800
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Results: Results: Further ApplicationFurther Application
a)8a)8--hr average effluent b) Reaction rate constanthr average effluent b) Reaction rate constant
Feeding conditionA B C D
Rat
e co
nsta
nt, s
ec-1
0.00
0.01
0.02
0.03
Feeding conditionA B C D
Eff
luen
t, m
g/m
3
0
100
200
300
Integrated unitControl unit Control unit Peak
Base
Integrated unitPeakBase
Feeding Condition
• Type C : 56.3 g/m3·hr(Frequent Peak)
Time, min
0 60 120 180
Inle
t C
onc.
, ppm
v
0
200
400
600
800
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Results: Results: Further ApplicationFurther Application
a)8a)8--hr average effluent b) Reaction rate constanthr average effluent b) Reaction rate constant
Feeding conditionA B C D
Rat
e co
nsta
nt, s
ec-1
0.00
0.01
0.02
0.03
Feeding conditionA B C D
Eff
luen
t, m
g/m
3
0
100
200
300
Integrated unitControl unit Control unit Peak
Base
Integrated unitPeakBase
Feeding Condition
• Type D : 65.9 g/m3·hr(High & Frequent Peak)
Time, min
0 60 120 180
Inle
t C
onc.
, ppm
v
0
200
400
600
800
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Transient feeding condition 2:Transient feeding condition 2:10 hrs square wave change + 14 hrs starvation without toluene loadings
Time, hrs
0 5 10 15 20 25 30 35
Inle
t C
on
cen
trat
ion
, pp
mv
0
100
200
300
400
500
600
700
600ppmv (15min) → 200ppmv (15min) → 400ppmv(15min) → 200ppmv(15min) / 1 Hr
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DesorptionDesorption profiles of 2profiles of 2--bed bed adsoprionadsoprion unitunit
Sequential time, hrs
0 4 8 12 16 20 24
Eff
luen
t C
on
cen
trat
ion
, pp
mv
0
50
100
150
200
250
300
Square wave change loading Starvation without toluene loading(only air flow)
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Overall Removal Performance Overall Removal Performance (with backwashing as biomass control)
a) Integrated unit (2-bed adsorption+biofilter)
0.1 1 10Eff
luen
t C
on
c, p
pm
v
0
100
200
300
400
Sequential Time, hr0.1 1 10 0.1 1 10 R
emo
val E
ffic
ien
cy, %
0
20
40
60
80
100
Day 1 Day 3 Day 7
0.1 1 10
Day 5
Effluent, ppmv
Removal, %
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Overall Removal Performance Overall Removal Performance (with backwashing as biomass control)
a) Integrated unit (2-bed adsorption+biofilter)
0.1 1 10Eff
luen
t C
on
c, p
pm
v
0
100
200
300
400
Sequential Time, hr0.1 1 10 0.1 1 10 R
emo
val E
ffic
ien
cy, %
0
20
40
60
80
100
Day 1 Day 3 Day 7
0.1 1 10
Day 5
b) Control unit (biofilter)
0.1 1 10Eff
luen
t C
on
c, p
pm
v
0
100
200
300
400
0.1 1 10 0.1 1 10 Rem
ova
l Eff
icie
ncy
, %
0
20
40
60
80
100
Sequential Time, hr
0.1 1 10
Day 1 Day 3 Day 7Day 5
Effluent, ppmv
Removal, %
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Results: Results: Further ApplicationFurther Application
Reactor volume Reactor volume of a single of a single biofilterbiofilter to achieve the same treatment goalto achieve the same treatment goalas in the integrated systemas in the integrated system
Feeding Condition Type A Type B Type C Type D
Peak concentration (Ci,p), ppmv
(g/m3)
400
(1.53)
700
(2.68)
400
(1.53)
600
(2.30)
Biofilter bed volume required (V), m3 ** 0.00435 0.00761 0.00435 0.00653
V / Vintegrated ** 1.5 2.6 1.5 2.2
* * Volume of the integrated unit = 0.00293 mVolume of the integrated unit = 0.00293 m33
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SummarySummary
The net effect of the 2The net effect of the 2--bed adsorption was VOC concentration bed adsorption was VOC concentration stabilization that makes it amenable for effective stable biodstabilization that makes it amenable for effective stable biodegradationegradation
1.1. The 2The 2--step cycle in the adsorption unit successfully performedstep cycle in the adsorption unit successfully performedparticular functions asparticular functions as
•• A polishing unit to abate the initial acclimation for the A polishing unit to abate the initial acclimation for the biofilterbiofilter;;•• A buffering unit to mitigate the A buffering unit to mitigate the biofilterbiofilter performance; performance; •• A feeding source for the A feeding source for the biofilterbiofilter without any feeding phase without any feeding phase
2. Details of the reactor volume suggest that capital expense ca2. Details of the reactor volume suggest that capital expense can be n be minimized by achieving a careful design and operation of minimized by achieving a careful design and operation of the integrated treatment scheme.the integrated treatment scheme.
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•• National Science Foundation (NSF) Award Number BES 0229135National Science Foundation (NSF) Award Number BES 0229135
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