Post on 04-Apr-2018
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Control of Volatile Organic Compound
(VOC) and Odorous Emissions usingBiofilters
Dr. Suchismita Bhattacharya
SIES BRSI Workshop on Recent Advances inMedical, Plant and Enviro Biotechnologies
January 13-14, 2006
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Contents
Introduction to Biofiltration
Types of Biofilters and Configurations
Research at the New Jersey Institute ofTechnology
VOC removal methods and comparison
Practical Applications
Case Study
Conclusions
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The problem
Volatile Organic Compounds
Odors
Removal Methods Chemical Scrubbing
Activated Carbon Adsorption
Thermal Oxidation/incineration
Catalytic Oxidation Absorption on Activated Carbon
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Types of Biofiltration
Based on Operational mode Biofilters
Packing contains nutrients
Possibility of clogging of biomass
Accumulation of acidic products
Biotrickling filters Continuous nutrient recycle
Removal of dead biomass
pH control possible
Based on Packing material Organic media
Peat, wood chips, soil
Synthetic media
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Synthetic Packing Media
High Density polypropylene
media 132 ft2/ft3
PVC hollow polymeric spheres
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Biofilter Configurations
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Biotrickling Filter Configurations
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Biotrickling Filter Configurations
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Possible Substrates
Substrate Bio-degradibility
Aliphatic Hydrocarbons (Methane, Propane) Low-Moderate
Aromatic Hydrocarbons
(Benzene, Toluene, Xylene)
Moderate -Good
Chlorinated hydrocarbons
Carbon tetrachloride, Chloroform
Trichloroethylene (cometabolic)
O-Dichlorobenzene, monochlorobenzene
Low
Moderate
LowAldehydes, Esters, Ketones Good
Ammonia
Hydrogen Sulfide
Nitrogen oxide
Good
Good
Poor
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Schematic of BTF Unit at NJIT
S
S2
1
3
45
6
7
8 8
9
1110
MEDIUM WATER
AIR
S
1. Air pump, 2. Rotameter Assembly, 3. Humidification tower, 4. Ethanol tank, 5. o-DCB tank, 6.
Biotrickling Filter, 7. Tank for recirculating medium, 8. Peristaltic pump, 9. Flow meter, 10. pH
Meter, 11. pH Electrode, S=Sampling Port. (Not to scale)
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How it appears
Clean
Packing
Biomass on
Packing
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Biotrickling Filter Model
Assumptions
ED,i,
i
i
LiLi
Gi
G
m
CCK
dh
dCu
O
GO
LOLO
GO
G
m
CCK
dh
dCu
With boundary conditions
;GDiGD
CC
;GEiGE
CC
;GOiGO
CC at 0h
No axial concentration gradients in the gas and liquid filmsNegligible mass transfer resistance from the bulk liquid to thebiofilm.The liquid film is modeled as a CSTR.The density of the biofilm and biomass concentration.At equilibrium, the concentration at the air/liquid interface followsHenrys law.Diffusion and reaction in the biofilm can be described by using abiodegradation effectiveness factor;
Balances In the gas phase
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Model Equations
Balances In the liquid phase
)()0( HhChC LDLD , )()0( HhChC LELE , )()0( HhChC LOLO
)(),(
)(),(
LOLELDE
OE
S
LVLVOE
LOLELDD
OD
S
LVLVODLO
O
GO
LO
LO
L
CfCCY
AXX
CfCCY
AXXC
m
CK
dh
dCu
)(),()(),( LOLDLEEE
SVELOLDLEE
E
SVLLLE
e
GELC
LEL CfCC
Y
AXCfCC
Y
AXC
m
CK
dh
dCu
)(),()(),( LOLDLEDD
SVDLOLDLED
D
SVLLLD
D
GDLD
LDL CfCC
Y
AXCfCC
Y
AXC
m
CK
dh
dCu
Mass Transfer Reaction in liquid Reaction in biofilm
With boundary conditions
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Validation of the Model
Percent Removal Removal Rate
(gm-3
-reactor h-1
)
Inlet
Concentration
(gm-3
) Experimental predicted Experimental Predicted
Error %
(Rpred-
Rexp)/Rexp
t = 4.2 min ; QL = 8.7 Lh-1
o-DCB 0.91 95.88 92.57 12.46 12.14 -2.60
Ethanol 2.51 95.38 98.32 34.20 35.38 3.46
o-DCB 3.35 90.25 90.19 43.19 43.37 0.43
Ethanol 2.35 97.35 98.35 32.68 33.13 1.38
o-DCB 2.11 95.24 91.47 28.71 27.77 -3.27
Ethanol 2.62 95.38 98.27 35.70 36.92 3.43
t = 4.00 min ; QL = 4.2 Lh-1
o-DCB 2.20 85.88 85.62 26.99 27.05 0.22
Ethanol 2.57 94.36 97.19 34.64 35.95 3.77
o-DCB 3.50 81.89 82.30 40.95 41.16 0.51
Ethanol 2.51 92.76 97.19 33.26 35.11 5.55
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VOC Removal Technologies
Technology Air Flow rate Concentration in ppmv
Condensation 200 20,000 m3/h
(120-12,000 SCFM)
50-200 g/m3
(2.8 % - 11.2% by volume)
Cyro-Condensation 30-600 m3/h
(20 -400 SCFM)
5-90 g/m3
(0.28 % - 5% by volume)
Scrubbing 200 20,000 m3/h
(120-12,000 SCFM)
10-40 g/m3
(0.56 % - 2.3% by volume)
Incineration 10,000 100,000 m3/h
(6000-60,000 SCFM)
8-140 g/m3
(0.5 % - 8% by volume)
Catalytic Oxidation 10,000 100,000 m3/h
(6000-60,000 SCFM)
1-10 g/m3
(500 ppmv 6000 ppmv)
Regenerative
Adsorption
100-10,000 m3/h
(60-6,000 SCFM)
1-10 g/m3
(500 ppmv 6000 ppmv)Non-RegenerativeAdsorption
10-60 m3/h
(6-40 SCFM)
0-5.0 g/m3
(
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Cost Comparison
Biofiltration Thermal treatment
with Concentrators
Thermal treatment
without
Concentrators
Capital Cost $1.4 million $1.8 million $0.9 million
Operating Cost for
ten years
$820,000 $7,100,000 $10,955,000
Natural gas Nil $0.65-$0.7 million/year
$1.05-$1.1 million/year
Electricity $42,500/ year
(2000 kWh/day)
$35,000/year (1700
kWh/day)
$20, 500/year (1000
kWh/day)
Water $12,500/year
(1,100 cu.ft./day)
Nil Nil
Bed Replacement $180,000/four years Nil Nil
Removal Efficiency 85% >95% >95%
Cost/Ton of VOC
removed over Ten
years
$5,800 $20,800 $27,700
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Technology Suppliers
Aromatrix Technologies Pte Ltd
Singapore
S&H GmbH (Zeestow/Germany)
PPC Biofilter: Airphase Biofilters & Bioscrubbers
Texas, USA
PRD Tech Inc.
Ohio, USA. Biospeedup
Biorem Technologies Inc
Ontario, Canada Biomix, Biosorbens
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Biotrickling Filter Applications
Air at Effluent, Waste Water Treatment Plants Odor, Hydrogen Sulfide, VOCs
Pseudomonas, Sphingomonas, Mycobacteria,Acetobacteriaceal
Thiobacillus
VOCs from Microelectronics Industry
Toluene, Acetone, Trichloroethylene Forest Products industry
-pinene (55 C), Methanol (70 C) Thermophillic bacteria
Vapors from Bathtub manufacturing facility Styrene
Flue gas from Coal based power Plant SO2 removal
Off-gases from Bakery plant Ethanol
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Biofilter Applications
Printed Circuit Board Manufacturing
Propylene Glycol, Monomethyl Ether Acetate
Vinyl Resin Production
MEK, Toluene
Animal Rendering Plant
H2S, VOC
Waste Water Pumping Station
H2S, Dimethyl Sulfide, Methyl Mercaptan, Dimethyl
Disulfide
Sludge Conditioning process
Odor Treatment
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Feasibility of Biofiltration
Gas Stream Specification VOC specification. Use of flame ionization detector (FID) or GC/MS
Temperature.
Relative humidity
Particulate loading, including condensables.
Air flow and volume to be treated
Applicability of Biofiltration Mixture or single substrate
Production of acid during biomass metabolism
Temperature: For mesophilic bacteria 10-40 C.
Humidity of Air should be close to saturation
If the particulate loading is water soluble and biodegradable, 0.034 g/std.m3
may be allowed. If the particulate loading is not water soluble and notbiodegradable, a maximum of 0.009 g/std.m3 is allowed.
Pretreatment may be required for warmer air or air containing particulates
Pilot Studies and Data analysis
Economic analysis
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Case Study: Conversion of ChemicalScrubber to Biotrickling Filter
Treatment of odorous emissions from waste water treatment plant Air flow rate 16,000m3h-1 (9,600cfm)
Inlet H2S concentration 5-35 ppm
Existing chemical scrubbers modified: Random Packing replaced by polyurethane foam packing 4 cm cubes
with 600m2m-3 specific surface area
Existing 7HP recycle pump replaced with 0.5 HP pump for tricklingrate of 77 Lmin-1
Secondary effluent instead of inorganic nutrients pH recycle liquid1.5-2.3
Dimensions/Operational Parameters
Internal Diameter 1.8 m Reactor height 9.7 m
Bed height 3.7m
Empty Bed residence time 2 sec
Start-up time 9 days
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Case Study: Conversion of ChemicalScrubber to Biotrickling Filter
Measurement of Process Variables Online H2S Concentrations at inlet/outlet
Inline pH sensor
Bed pressure drop with U-tube manometer
Gas chromatography of grab samples for Carbonyl sulfide,SO2, Methyl Mercaptan, etc
VOC using portable Scentograph
Water samples for CO2, NH3, foul airflow
Economic Analysis
Conversion cost $40,000-$60,000
Chemical costs for removing 3,000 kg of year H2S= $30,000.
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Conclusions
Biofilters and Biotrickling filters are anestablished technology in USA, Canada and inEurope
Biotrickling filters may be more suitable forrecalcitrant compound removal
Biofilters with synthetic packing media havesolved some of the problems with organic media
Both technologies have enormous odor/VOCcontrol potential
Can these work in India?