Nitrogen Removal 1.0 to 3.0 NO Anammox NH Charles B. … Removal 1… · Nitrogen Removal 1.0 to...
Transcript of Nitrogen Removal 1.0 to 3.0 NO Anammox NH Charles B. … Removal 1… · Nitrogen Removal 1.0 to...
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Nitrogen Removal 1.0 to 3.0
Charles B. Bott, Ph.D., P.E., BCEE
Hampton Roads Sanitation District
Denitrification
NH4+
N2
NO2-Anammox
Nitrification
NO3-
N-fixation
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Hampton Roads Sanitation District
• Created in 1940
• Serves 1.6 million people
• Includes 17 jurisdictions – 3,100 square miles
• 9 major plants, 4 small plants
• Capacity of 249 MGD
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HRSD’s Bubble Permit - 2011
• James River
– 6,000,000 lbs/yr TN
– 573,247 lbs/yr TP
• York River
– 288,315 lbs/yr TN
– 33,660 lbs/yr TP
• Rappahannock River (one plant)
– 1,218 lbs TN
– 91 lbs/yr TP
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Chesapeake Bay TMDL & VA WIP
• Nitrogen – James River– 2011 – 6.0 million pounds/year
• Major upgrades ongoing at Nansemond, James River, Williamsburg, Army Base,
• Upgrade at Boat Harbor (minimal N removal)
– 2017 – 4.4 million pounds/year• VIP - biological process upgrade for improved denitrification
• Small upgrade at Williamsburg possible
– 2021 – 3.4 million pounds/year • Upgrade Chesapeake-Elizabeth (full plant)
• Nitrogen – York River ---- No change?– Rapid upgrade to add denite filters for 2011 compliance
– Additional upgrade needed for cost-effective BNR and reliability
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HRSD R&D Program Focus• Resource utilization:
– Energy
– Chemicals
– Labor (operations, maintenance, instrumentation…)
– Concrete
• Resource recovery– Water
– P
– N (maybe)
– CH4 - biogas
– Heat
– Hydraulic energy
– Chemicals of interest (maybe)
– Biosolids (N, P, organics)
– Etc, etc, etc 5
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The VIP Process
• It was developed and patented by HRSD and CH2M Hill
• Biologically removes Phosphorus and Nitrogen
• Its free for any one to use…
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Current HRSD R&D Efforts in BNR:• Supplemental carbon for denitrification (chemicals)
– AOB conversion of methane to methanol
– Reduced S compounds
– Ethanol used for fuel blending• Ammonia-based DO control systems (energy, chemicals)
• Cost-effective Chemically Enhanced Primary Treatment (chemicals, energy)
• Algae-based nutrient removal (chemicals, energy)
• Centrate treatment – anammox (chemicals, energy)
• Nitrite accum. and excessive chlorine demand (chemicals)
• IFAS process development and modeling (concrete, energy)
• Nitrification inhibition (concrete)
• BNR process reliability and stochastic methods (concrete)
• Improvement of BNR process models (chemicals, energy, concrete)
• Organic nitrogen sources and fate (issue)
• Urine separation (???)7
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Some Motivation for Pilot Work…• Nitrogen removal upgrade required by 2021 to meet TN
of approximately 5 mg/L
• Capital Cost = $125-150M (conventional process)
• Operating costs will increase dramatically:
– Incremental Energy for aeration and pumping = $1.0 M/yr
– Incremental chemicals (caustic and carbon) = $1.0 to 2.0 M/yr
– Labor & supplies?
• Limited land available– Nutrient Removal– Biosolids
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Chesapeake-Elizabeth Treatment Plant
• 24 MGD design, 15-20 MGD operating
RawWastewater
ScreeningFeCl3
GritRemoval
High Rate Aeration Tanks
(SRT=1.5 to 2 days)
FeCl3
RAS
Chlorine Contact
Discharge to Chesapeake Bay
GravityThickener
WAS
Centrifuge
Multiple Hearth Incinerators
CH4
ASH
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Traditional BNR Alternative by 2021• Construct primary clarifiers• Construct:
– 5-stage Bardenpho (+9 MG) & Filters– MLE or VIP + Denite Filters
• Incinerator scrubber blowdown treatment– Sidestream biological treatment of cyanide
• Thickening improvements• Full Distributed Control System (DCS)
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Pilot Program– 4 year study
– Collaboration through Water Environment Research Foundation (WERF) project:
• DCWater & HRSD
• Austrian (Strass) and Swiss wastewater utility
• Developers of the DEMON process (Wett, et al)
• ODU, Virginia Tech, Columbia University (NY), University of Innsbruck (Austria)
• Three US engineering firms – HDR, Black & Veatch, AECOM
• Several other interested US wastewater utilities
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Agenda• Reactions 1.0, 2.0, 3.0• Sidestream Treatment of Anaerobically Digested Sludge
Dewatering Liquor – 1.0, 2.0, 3.0 (All established)• Mainstream Treatment 1.0 (established)• Mainstream Treatment 2.0 (established with caveats)
– SND (es– A/B Process– HRSD Pilot A/B Process– NH4-based Aeration Control– NOB Repression
• Mainstream Treatment 3.0 (emerging)– Alternative configurations– Carbon Flow– HRSD Pilot 3.0 – separate stage without bioaugmentation
• Several other emerging ideas (3.1)12
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Conventional Nitrification-Denitrification (1.0)
1 mole Ammonia
(NH3 / NH4 +)
½ mol Nitrogen Gas
(N2 )
1 mole Nitrite
(NO2-)
1 mole Nitrite
(NO2-)
1 mole Nitrate
(NO3-)
Autotrophic Bacteria
Aerobic Environment
Heterotrophic Bacteria
Anoxic Environment
75% O2 (energy)
~100% Alkalinity
25% O2 (energy)
40% Carbon (BOD)
60% Carbon (BOD)
Ammonia Oxidizing Bacteria (AOB)
Nitrite Oxidizing .Bacteria (NOB)
13DENITRIFICATIONNITRIFICATION
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Some New Vocabulary….
1 mole Ammonia
(NH3 / NH4 +)
½ mol Nitrogen Gas
(N2 )
1 mole Nitrite
(NO2-)
1 mole Nitrite
(NO2-)
1 mole Nitrate
(NO3-)
Autotrophic Bacteria
Aerobic Environment
Heterotrophic Bacteria
Anoxic Environment
Ammonia Oxidizing Bacteria (AOB)
Nitrite Oxidizing .Bacteria (NOB)
DENITRIFICATIONNITRIFICATION
Nitritation
Nitratation Denitratation
Denitritation
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Nitritation-Denitritation = “Nitrite Shunt” (2.0)
1 mole Ammonia
(NH3 / NH4 +)
½ mol Nitrogen Gas
(N2 )
1 mole Nitrite
(NO2-)
1 mole Nitrite
(NO2-)
1 mole Nitrate
(NO3-)
Autotrophic Bacteria
Aerobic Environment
Heterotrophic Bacteria
Anoxic Environment
75% O2 (energy)
~100% Alkalinity
25% O2 (energy)
40% Carbon (BOD)
60% Carbon (BOD)
Ammonia Oxidizing Bacteria (AOB)
Nitrite Oxidizing .Bacteria (NOB)
Advantages:
• 25% reduction in oxygen demand (energy)
• 40% reduction in carbon (e- donor) demand
• 40% reduction in biomass production 15
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The N-Cycle
Denitrification
NH4+
N2
NO2-Anammox
Nitrification
NO3-
N-fixation
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Partial Nitritation-Anammox = “Deammonification” (3.0)
1 mole Ammonia
(NH3 / NH4 +)
½ mol Nitrogen Gas (N2 ) +
a little bit of nitrate (NO3-)
0.5 mole Nitrite
(NO2-)
Autotrophic Bacteria
Aerobic Environment
Autotrophic Anoxic
Environment37% O2 (energy)
~50% Alkalinity Ammonia Oxidizing Bacteria (AOB)
Advantages:
• 63% reduction in oxygen demand (energy)
• Nearly 100% reduction in carbon demand
• 80% reduction in biomass production
• No additional alkalinity required
ANAMMOX“Anaerobic” Ammonia Oxidation - (New Planctomycete - Strous et al, 1999)
NH4+ + 1.32 NO2
- + 0.066 HCO3- + 0.13 H+
0.26 NO3- + 1.02N2 + 0.066 CH2O0.5N0.15 + 2.03 H2O
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Agenda• Reactions 1.0, 2.0, 3.0• Sidestream Treatment of Anaerobically Digested Sludge
Dewatering Liquor – 1.0, 2.0, 3.0 (All established)• Mainstream Treatment 1.0 (established)• Mainstream Treatment 2.0 (established with caveats)
– SND (es– A/B Process– HRSD Pilot A/B Process– NH4-based Aeration Control– NOB Repression
• Mainstream Treatment 3.0 (emerging)– Alternative configurations– Carbon Flow– HRSD Pilot 3.0 – separate stage without bioaugmentation
• Several other emerging ideas (3.1)18
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• 1% of Total Plant Influent Flow
• Rich in Nitrogen & Phosphorus
• 15 to 25% of the Total Plant TN load
• Ammonium Conc. 800 to 1,500 mg-N/L
• Temperature 30 - 38C
• Alkalinity insufficient for complete
nitrification
• Insufficient carbon for denitrification
• For a Bio-P plant with no iron addition:
• Centrate TP = 200-800 mg/L
InfluentPrimary
Clarifier Secondary
Clarifier
Effluent
Centrate
Primary Sludge WAS
Dewatering
Thickening
RAS
Anaerobic
Digestion
Biosolids
Aeration
Tank
Recycle Streams with High Ammonia - Sidestream
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Sidestream Treatment Options
Biological - N Physical-Chemical – N&P
Ion-Exchange• ARP
Struvite Precipitation• Ostara Process• PhosPaq Process
Nitrification / Denitrification& Bioaugmentation
• With RAS & SRT Control• With RAS• Without RAS
Nitritation / Denitritation• Chemostat• SBR• Post Aerobic Digestion
Deammonification• Suspended Growth SBR• Attached Growth MBBR• Upflow Granular Process
Ammonia Stripping• Steam• Hot Air• Vacuum Distillation
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1.0
2.0
3.0
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Conventional Nitrification-Denitrification
1 mole Ammonia
(NH3 / NH4 +)
½ mol Nitrogen Gas
(N2 )
1 mole Nitrite
(NO2-)
1 mole Nitrite
(NO2-)
1 mole Nitrate
(NO3-)
Autotrophic Bacteria
Aerobic Environment
Heterotrophic Bacteria
Anoxic Environment
75% O2 (energy)
~100% Alkalinity
25% O2 (energy)
40% Carbon (BOD)
60% Carbon (BOD)
Ammonia Oxidizing Bacteria (AOB)
Nitrite Oxidizing .Bacteria (NOB)
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InNitri Process was the First Bioaugmentation Concept
PC
Sec. Effluent
Activated Sludge Tank
RAS
WAS
Centrate
(NH3-N)Nitrification
Reactor
~250C
Nitrifiers
NO3-N
Expected bioaugmentation benefit not fully realized
Temperature change
Poor capture of recycle stream nitrifiers
Predation 22
Peter Kos
M2T Tech License
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BABE Process – (SBR Mode of Operation)BioAugmentation Batch Enhanced
AT-3, BAR, CaRRB, Maureen, etc.
PC
Influent Sec. Effluent
Activated Sludge Tank
RAS
WAS
Centrate
(NH3-N)Nitrification
Reactor
~250C
Nitrifiers
NO3-N
Delft U.
DHV
STOWA
Bioaugmentation is better
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Sidestream Treatment Options
Biological - N Physical-Chemical – N&P
Ion-Exchange• ARP
Struvite Precipitation• Ostara Process• PhosPaq Process
Nitrification / Denitrification& Bioaugmentation
• With RAS & SRT Control• With RAS• Without RAS
Nitritation / Denitritation• Chemostat• SBR• Post Aerobic Digestion
Deammonification• Suspended Growth SBR• Attached Growth MBBR• Upflow Granular Process
Ammonia Stripping• Steam• Hot Air• Vacuum Distillation
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1.0
2.0
3.0
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Nitritation-Denitritation = “Nitrite Shunt”
1 mole Ammonia
(NH3 / NH4 +)
½ mol Nitrogen Gas
(N2 )
1 mole Nitrite
(NO2-)
1 mole Nitrite
(NO2-)
1 mole Nitrate
(NO3-)
Autotrophic Bacteria
Aerobic Environment
Heterotrophic Bacteria
Anoxic Environment
75% O2 (energy)
~100% Alkalinity
25% O2 (energy)
40% Carbon (BOD)
60% Carbon (BOD)
Ammonia Oxidizing Bacteria (AOB)
Nitrite Oxidizing .Bacteria (NOB)
Advantages:
• 25% reduction in oxygen demand (energy)
• 40% reduction in carbon (e- donor) demand
• 40% reduction in biomass production 25
Nitritation
Denitritation
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Nitritation - Denitritation
AOBNH4 + O2 NO2
-
NO2 Denite
Methanol or
other carbon sourceAlkalinity
Air
Centrate with low
Effluent NH4 and NOx
Mostly
NO2Centrate NH4
Centrate with high NO2
to headworks for odor control?
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Sidestream Nitritation
• Control
– Elevated temperature (30-35 deg C)
– Low SRT (1-2 days)
– Low DO (~0.5 mg/L)
• NOB Repression Mechanisms (all the possibilities)
– AOB max growth rate > NOB max growth rate at high temp
– Free NH3 inhibition
– AOB DO affinity > NOB DO affinity at high temp
– Nitrous acid inhibition
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Sidestream Treatment Options
Biological - N Physical-Chemical – N&P
Ion-Exchange• ARP
Struvite Precipitation• Ostara Process• PhosPaq Process
Nitrification / Denitrification& Bioaugmentation
• With RAS & SRT Control• With RAS• Without RAS
Nitritation / Denitritation• Chemostat• SBR• Post Aerobic Digestion
Deammonification• Suspended Growth SBR• Attached Growth MBBR• Upflow Granular Process
Ammonia Stripping• Steam• Hot Air• Vacuum Distillation
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1.0
2.0
3.0
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Partial Nitritation-Anammox = “Deammonification” (3.0)
1 mole Ammonia
(NH3 / NH4 +)
½ mol Nitrogen Gas (N2 ) +
a little bit of nitrate (NO3-)
0.5 mole Nitrite
(NO2-)
Autotrophic Bacteria
Aerobic Environment
Autotrophic Anoxic
Environment37% O2 (energy)
~50% Alkalinity Ammonia Oxidizing Bacteria (AOB)
Advantages:
• 63% reduction in oxygen demand (energy)
• Nearly 100% reduction in carbon demand
• 80% reduction in biomass production
• No additional alkalinity required
ANAMMOX“Anaerobic” Ammonia Oxidation - (New Planctomycete - Strous et al, 1999)
NH4+ + 1.32 NO2
- + 0.066 HCO3- + 0.13 H+
0.26 NO3- + 1.02N2 + 0.066 CH2O0.5N0.15 + 2.03 H2O
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Partial Nitritation – Anammox• Two Step Anammox Process
– Dokhaven, Rotterdam (NL)
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One-Step Sidestream Deammonification• SBR + Hydrocyclone Granular Sludge
(DEMON)
– Strass, Austria + ~18 others
• Upflow Granular Sludge (CANON)
– Olburgen, Netherlands
• Biofilm process (MBBR-style)
– AnoxKaldnes - Malmo, Sweden• AnitaMox
– Hattingen, Germany & Stockholm• Deammon (Purac)
Centrate
NH4+
31
Partial Nitritation and Anammox- combined in a single reactor
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32
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Cyclone for selecting for DEMON® Granules
Mixed Liquor Overflow Underflow
33
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Einleitung
Apeldoorn (NL)
Thun (CH)
Heidelberg (D)
Deammonification Experience: DEMON® Process
Operational:
• Strass, Austria
• Glarnerland, Switzerland
• Thun, Switzerland
• Plettenberg, Germany
• Heidelberg, Germany
• Apeldoorn, Netherlands
Several under construction;
• Croatia
• Austria
• Germany
• By 2012 more centrate Demon facilities (>20) than
conventional Nitrification/Denitrification
• Cyklar-Stulz & Grontmij providing turnkey services and
now World Water Works, Inc. has US license
Strass (A)
34
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Sidestream Deammonification:What’s the benefit?
• Remove about 20% of the N load to the plant by treating the centrate separately
• Do it with:– No chemicals (caustic & methanol)– < 40% of the energy cost– (as compared to traditional nitrification-denitrification)
• Risks:– Slow process startup (US plant)– Requires robust process control, particularly during startup– Process has been adequately demonstrated in Europe– We need just one in North America (anywhere)…
35
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Sidestream Deammonification Status in North America (3.0)
– DEMON - Alexandria, VA + DCWater Pilot (no cyclone)
– DEMON – New York DEP + DCWater Pilot (no cyclone)
– DEMON – Pierce County, Washington
– Several other DEMON pilot studies pending
– MBBR-style process – New York DEP Pilot
– DEMON – DCWater Blue Plains in design
– DEMON – Alexandria, VA in construction
– DEMON – HRSD York River in construction
36
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HRSD York River Treatment PlantDEMON Under Construction
37
Discharge
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Agenda• Reactions 1.0, 2.0, 3.0• Sidestream Treatment of Anaerobically Digested Sludge
Dewatering Liquor – 1.0, 2.0, 3.0 (All established)• Mainstream Treatment 1.0 (established)• Mainstream Treatment 2.0 (established with caveats)
– SND (es– A/B Process– HRSD Pilot A/B Process– NH4-based Aeration Control– NOB Repression
• Mainstream Treatment 3.0 (emerging)– Alternative configurations– Carbon Flow– HRSD Pilot 3.0 – separate stage without bioaugmentation
• Several other emerging ideas (3.1)38
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Conventional Nitrification-Denitrification (1.0)
1 mole Ammonia
(NH3 / NH4 +)
½ mol Nitrogen Gas
(N2 )
1 mole Nitrite
(NO2-)
1 mole Nitrite
(NO2-)
1 mole Nitrate
(NO3-)
Autotrophic Bacteria
Aerobic Environment
Heterotrophic Bacteria
Anoxic Environment
75% O2 (energy)
~100% Alkalinity
25% O2 (energy)
40% Carbon (BOD)
60% Carbon (BOD)
Ammonia Oxidizing Bacteria (AOB)
Nitrite Oxidizing .Bacteria (NOB)
39DENITRIFICATIONNITRIFICATION
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MLE Process (N Removal)
AerobicSC
Primary
Effluent
BOD + NH4
RASWAS
air
Nitrification &
Residual BOD RemovalAnoxic
BOD Rem. by
Denitrification
Nitrate/Internal Recycle (IMLR) = Nitrate Recycle (NRCY)
TN ~ 8-12 mg/L
40
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4-Stage Bardenpho(Better N Removal)
Aerobic
SC
RASWAS
air
Anoxic
Ae
rob
ic
air
Anoxic
Carbon
(Methanol?)TN ~ 3-5 mg/LPrimary
Effluent
BOD + NH4
Nitrate Recycle (NRCY)
41
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Agenda• Reactions 1.0, 2.0, 3.0• Sidestream Treatment of Anaerobically Digested Sludge
Dewatering Liquor – 1.0, 2.0, 3.0 (All established)• Mainstream Treatment 1.0 (established)• Mainstream Treatment 2.0 (established with caveats)
– Relationship to SND – A/B Process– HRSD Pilot A/B Process– NH4-based Aeration Control– NOB Repression
• Mainstream Treatment 3.0 (emerging)– Alternative configurations– Carbon Flow– HRSD Pilot 3.0 – separate stage without bioaugmentation
• Several other emerging ideas (3.1)42
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Can we implement this in the mainstream BNR Process?
Process has not been purposefully implemented in larger plants…– Large aeration tank volume required (perception)– Sophisticated instrumentation & controls– Uncertain design– Uncertain operation– Risk of poor mixed liquor settling– VERY DIFFICULT TO CONFIRM 2.0
Orbal® Oxidation Ditch
Source: Siemens
“Simultaneous Nitrification/Denitrification(SND)”
43
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Current Thinking on SND…• Focus is low DO operation (energy savings)• NOB repression (2.0) rarely if ever confirmed• Sludge settling characteristics are a real concern for
medium/large plants• Mechanisms:
– Micro environment that affects oxygen diffusivity inside the floc– Macro environment that is related to mixing (tank configuration)– Bulk DO concentration & carbon availability
• Needs:– Control strategy– NOB repression confirmed and controlled – Demonstration in medium/large plants– Combine with Bio-P?
• Opportunity is significant, especially if NOB can be repressed
44See talk by Jose Jimenez tomorrow
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New Tools for SND-Style Processes (2.0)
• Ammonia-based Aeration Control– Allows stringent control over DO provided– See talk by Leiv Rieger tomorrow
• NOB Repression– Rapid transient anoxia seems to be the key– Mechanisms?
• AOB always at maximum growth rate (aerobic SRT control with excess NH4 available)
• NOB enzyme expression delay• Aerobic SRT controlled• Nitrite availability delay• Oxygen affinity• Free ammonia (NH3) inhibition of NOB
45
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Concepts for Pilot Testing1. Two stage “A/B” process:
– A stage – high rate activated sludge for 60-70% COD removal (40-50% sCOD removal)
– B stage – MLE in SND mode (N removal 2.0)
46
RawWastewater
ScreeningFeCl3
GritRemoval
FeCl3
RAS
Chlorine Contact
Discharge to Chesapeake Bay
WAS
A-Stage
(Aerobic)SRT=0.5d
WAS
High-RateAeration
Tank
B-Stage (MLE)
IMLR
Aerobic
WithinExisting Tanks
MethanolDenite Filter
RAS
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Pilot System Schematic
Hampton Roads Sanitation District Chesapeake Elizabeth Pilot Study
NRCY
RAS
RAS (0.75 gpm)
RAS
RAS
WAS
Ammonia Bypass
WAS
AN OX OXNitritation Anammox
HRAS
TCOverflow Overflow
B-Stage MLE B-Stage Deammonification
A-stage HRAS
Cyclone
WAS
~3 gpm ~2 gpm 1 gpm
0.5 gpm
0.5 gpm
0.25 gpm
Optional NPW Feed
Emergency Clarifier
WAS
TC
Legend
OX Aerated
AN Un-aerated (presence of NO3-)
HRAS High Rate Activated Sludge
RAS Return Activated Sludge
WAS Waste Activated Sludge
NRCY Nitrate Recycle
TC Temperature Control Tank
47
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Influent COD
480
100
200
300
400
500
600
700
800
12-Feb 26-Feb 4-Mar 11-Mar 18-Mar 1-Apr 8-Apr 15-Apr 22-Apr 29-Apr 6-May
Inf
CO
D (
mg/
L)
pCOD
cCOD
ffCOD
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Influent Nitrogen
490
10
20
30
40
50
60
70
23-Dec 12-Jan 1-Feb 21-Feb 12-Mar 1-Apr 21-Apr 11-May
Nit
roge
n S
pec
ies
(mg
N/L
)
TKN
ON
TAN
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A-stage High-Rate Activated Sludge (HRAS)
• 10 inch diameter pipe reactor at 30 minute HRT
• Single 7 inch high capacity disc diffuser
• SOR = 420 gal/ft2·day
• SLR = 22 lbs/ft2·day at 3000 mg/L
• Fixed all Hach LDO probe and MOV/PID issues
50
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Current HRAS Operation
• HRT = 30 min
• MLSS = 2000-3500 mg/L
• DO = 0.5 mg/L
• Influent Temp = 25°C
• Aerobic SRT = 0.20-0.25 days
51
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COD Removal
520.0
0.2
0.4
0.6
0.8
1.0
1.2
0
10
20
30
40
50
60
70
80
90
100
17-Apr 19-Apr 22-Apr 24-Apr 25-Apr 26-Apr 29-Apr 30-Apr 1-May 2-May 3-May 6-May 7-May
Ave
rage
DO
(m
g/L)
% C
OD
Rem
ova
l
COD
sCOD
pCOD
DO
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B-Stage MLE
53
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MLE Operational Parameters
• Total SRT = ~10 days
• HRT= 4 hr
• Influent Flow = 0.50 GPM
• Nitrate Recycle = 400%
• RAS = 100%
• Temperature = 24 C
• MLSS = (3500 +/- 750) mg/L
54
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Ammonia Based DO control
TK-202
Anoxic
TK-203
Aerobic
TK-204
Aerobic
0.5 gpm
NRCY (2.0 gpm)
WAS
RAS (0.5 gpm)
NH4+-N
TK-204
DO
TK-203 &TK-204
Simultaneous Nitrification
and Denitrification (SND)
Nitrite Shunt?
55
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Ammonia-Based D.O. Control
TK 204 High NH3-N = 2 mg/L
TK 203 LDO = 0.1 mg/L
TK 203 Min HDO = 0.3 mg/L
TK 203 Max HDO = 4 mg/L
Time
TK 204 Low NH3-N = 1 mg/L
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Ammonia-Based DO control
• Ammonia Set Points 3-5 mg-N/L
0
1
2
3
4
5
6
0
0.1
0.2
0.3
0.4
0.5
0.6
0.7
0.8
23:45 11:45 23:45 11:45 23:45
Tank 202 NO3-N Tank 204 DO Tank 204 NH4-N
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Ammonia Based DO Control in Action
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2nd Aerobic pH, Ammonia and Nitrate Trends
mgNH4-N/L pH
mgNOx-N/L mgNH4-N/L
59
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0
2
4
6
8
10
12
14
16
18
20
12/23 1/12 2/1 2/21 3/12 4/1 4/21
mg-
N/L
MLE Effluent 2012
TIN
NH3-N
NOx-N
pH Overdose
Washout
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Period of Best MLE Performance
0
1
2
3
4
5
6
7
8
0
20
40
60
80
100
120
140
160
180
3/24 3/25 3/26 3/27 3/28 3/29 3/30 3/31 4/1 4/2 4/3
mg-
N/L
mg/
L Influent sCOD
Effluent NOx-N
Effluent TIN
•Influent sCOD between 118 – 160 mg/L
•MLSS between 4000 – 4500 mg/L
•Effluent TIN under 7 mg-N/L
•Effluent NOx as low as 2.83 mg-N/L
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DO Control System Led to NOB Repression
Jan 23 – Feb 2 Mar 11 – Mar 25
3.01
3.57
0.50
0.00
1.00
2.00
3.00
4.00
5.00
6.00
7.00
8.00
MLE Effluent
mgN
/L
NO3-N
NO2-N
NH3-N4.16
0.47
1.76
0.00
1.00
2.00
3.00
4.00
5.00
6.00
7.00
MLE Effluent
mgN
/L
NO3-N
NO2-N
NH3-N
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NOB Repression
0
2
4
6
8
10
12
1/7 1/17 1/27 2/6 2/16 2/26 3/7 3/17 3/27
mg-
N/L
NO2-N
NO3-N
Washout
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Influent COD and MLSS (OUR?) were hypothesized to be critical parameters in
sustaining NOB repression
0.5
0.55
0.6
0.65
0.7
0.75
0.8
0.85
0.9
0.95
150
200
250
300
350
400
450
500
3/2 3/7 3/12 3/17 3/22 3/27 4/1 4/6 4/11 4/16 4/21
NO
2/N
Ox
Frac
tio
n
mg/
L
Influent COD
NO2/NOx
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0
1000
2000
3000
4000
5000
0
1
2
3
4
5
6
7
2/26/2012 3/17/2012 4/6/2012 4/26/2012 5/16/2012
mgM
LSS/
L
mgN
Ox-
N/g
MLS
S.h
r, m
gNO
3-N
/gM
LSS.
hr
AOB rate NOB rate MLSS
AOB and NOB Specific Nitrogen Processing Rates
Low inf COD
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MLE
TK 202
Anoxic
TK 203
Aerobic
TK 204
Aerobic
NOx-N Recycle
WAS
RAS
TK 202
(pro-denitritation)
TK 203
(pro-nitritation)
TK 204
(pro-SND)
NOx-N Recycle
WAS
RAS
Staged Anaerobic
Selector
Nitritation-Denitritation through Modulating Aeration (NiDeMA)
• Reactors sized based on Ches-Liz aeration tank volume
• HRT = 4.4 hr (1 aeration tank out of service)
• SLR = <25 lb/ft2·day
• Target MLSS = 4000 mg/L (maximum 4800 mg/L)
• Anaerobic tank = 16 gallons (separated by baffle)
• Need of NOx-N Recycle to be determined
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Primary Clarifier
• Independent feeds for each B-stage
• PCE is temperature controlled
• Have the ability to optimize COD concentration and fractions for each B-stage influent
• SOR = 165 gal/ft2·day
• HRT = 4-5 hrs
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Agenda• Reactions 1.0, 2.0, 3.0• Sidestream Treatment of Anaerobically Digested Sludge
Dewatering Liquor – 1.0, 2.0, 3.0 (All established)• Mainstream Treatment 1.0 (established)• Mainstream Treatment 2.0 (established with caveats)
– Relationship to SND – A/B Process– HRSD Pilot A/B Process– NH4-based Aeration Control– NOB Repression
• Mainstream Treatment 3.0 (emerging)– Alternative configurations– Carbon Flow– HRSD Pilot 3.0 – separate stage without bioaugmentation
• Several other emerging ideas (3.1)68
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Objectives for 3.0
• Redirect Carbon/COD to Anaerobic Digestion/Treatment– A-stage HRAS– CEPT– Anaerobic Treatment (UASB, AnMBR)– Primary Clarifier
• Repress NOBs – Low temp– Low NH4
• Retain Anammox (high SRT for Anammox)
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Mainstream Deammonification????
• Very challenging….– Lower temperature– Lower NH4 concentration
• Primary objective: Eliminate competition for NO2-
– NOB and Heterotrophs
• Selective retention of Anammox is critical• Risk is high that this process will not work, but reward is very
high…– Reduce capital cost by ~$20-40M– Reduce chemical cost by $1-2M/yr (no increase above current
conditions)– Reduce energy cost by ??? (depends on COD redirection)
• This is the clear path to Energy Neutral/Positive treatment…
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Several Possible Approaches
A. Bioaugment Anammox and AOB from sidestream deammonification process
– One step – AOB + Anammox in same reactor
– SND type reactor with selective Anammox retention
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Full-scale experiments at WWTP Glarnerland
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Several Possible ApproachesA. Bioaugment Anammox and AOB from sidestream
deammonification process– One step – AOB + Anammox in same reactor– SND type reactor with selective Anammox retention
B. One step process without bioaugmentation– Granular sludge process– Dutch DHV/TU Delft Nereda Research Program
C. Two step process without bioaugmentation– Separate stage partial nitritation– Anammox
• MBBR• MBR• Granular sludge – cyclone or upflow reactor
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B-stage Nitritation/Anammox
RAS
A-stage Eff
TK-305
Anammox
MBBRTK-302
Nitritation
0.5 gpm
WAS
40 gal60, 90, 120 gal
Temp
Control
Alkalinity
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DO, pH,
Temp, N
O3, NO2
,
NH4,
TSS
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B-Stage Deammonification
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Operational w/o Seed Sludge
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Nitritation Operational Parameters
• SRT = 7 days
• HRT = 3 hr
• Influent Flow = 0.50 GPM
• RAS = 100 %
• Temperature = 24 C
• pH 6.8-7.0 (Sodium Bicarbonate)
• MLSS = 3000 mg/L (current)
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DO controller for Nitritation
[NH3-N] ≥ [NO2-N] + [NO3-N]
Increase High DO by 0.1 mg/LLow DO = 0.1 mg/L
Wait 60 secs(Max DO = 1.4 mg/L)
Decrease High DO by 0.1 mg/LLow DO = 0.1 mg/L
Wait 60 secs(Min DO = 0.9 mg/L)
YES
NO
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Illustration of NH3-N vs Nox-N (AVN) Control
NH3-N - NOx-N = 0
LDO = 0.1 mg/L
Min HDO = 0.9 mg/L
Max HDO = 1.4 mg/L
Time
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AVN Control in Action
0.20
0.30
0.40
0.50
0.60
0.70
0.80
0.00
2.00
4.00
6.00
8.00
10.00
12.00
14.00
4/9/12 4/11/12 4/13/12 4/15/12 4/17/12
mgO
2/L
mgN
/L
NH3-N NO2-N NO3-N DO
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0
5
10
15
20
25
30
35
40
0
5
10
15
20
25
30
2/1/12 2/21/12 3/12/12 4/1/12 4/21/12 5/11/12
Inf
NH
3-N
, m
gN/L
mgN
/L
NO3-N NO2-N NH3-N Inf NH3-N
Low infCOD
PCE
Nitritation Effluent Nitrogen Species and Influent Ammonia
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Nitrite Accumulation Rate
0%
10%
20%
30%
40%
50%
60%
70%
80%
90%
100%
2/1/12 2/11/12 2/21/12 3/2/12 3/12/12 3/22/12 4/1/12 4/11/12 4/21/12 5/1/12 5/11/12 5/21/12
NO
2-N
/NO
x-N
Low inf COD
PCE
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MLSS and SVI
0
50
100
150
200
250
300
350
0
1000
2000
3000
4000
5000
6000
2/1/12 2/21/12 3/12/12 4/1/12 4/21/12 5/11/12 5/31/12
ml/
g
mg/
L
MLSS SVI
Low infCOD
PCE
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0
50
100
150
200
250
0
5
10
15
20
25
30
25-Mar-2012 1-Apr-2012 8-Apr-2012 15-Apr-2012 22-Apr-2012 29-Apr-2012 6-May-2012
mgC
OD
/L
mgN
/L
NH3-N NO2-N NO3-N Inf sCOD
Effect of Inf sCOD on Nitrogen Removal and Species distribution
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AOB and NOB Specific Nitrogen Processing Rates
0
1000
2000
3000
4000
5000
6000
0
1
2
3
4
5
6
2/26/2012 3/17/2012 4/6/2012 4/26/2012 5/16/2012
mgM
LSS/
L
mgN
Ox-
N/g
MLS
S.h
r, m
gNO
3-N
/gM
LSS.
hr
AOB rate NOB rate MLSS
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Potential Implication of Nitritation DO Control
Maximum Nitrogen RemovalMaximum NOB Repression
Minimum AerationNitritation Denitritation
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Ideal Configuration…
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3.1 Ideas….
• Nitrite + Methane – Methanotrophic Denitritation
• Sulfide-driven Autotrophic Denitritation/Denitratation
• Nitritation
• Is Anammox required??
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RawWastewater
Screening
GritRemoval
UV Disinfection
Anaerobic Treatment
Anaerobic MBR or Biofilm Process
N Removal 3.1CH4
Discharge to Chesapeake Bay
WasteSludge
FeCl3
TertiaryFiltration
WAS
EnergyGeneration
RAS
WAS
NO2 recycle
Nitritation