Present and Future Technologies

for Nutrient Removal

James L Barnard, Ph.D., D.Ing. h.c. BCEE, WEF Fellow, Dist. MASCE

Ohio Water Environment

Association

Contents

Problems relating to Nutrients

Wastewater as Resource

Basics of present nutrient removal and recovery

Future developments

Nutrient Roadmap

Microcystis Poisoning

Dr. Anthony Turton, Keynote Address CSIR RSA November 18, 2008

Fishkill

Photo by Gerald Simons

Ocean life on the brink of mass

extinctions… overfishing, excessive nutrients causing ‘dead zones’…. News Daily Posted 2011/06/21 at 5:50 am EDT

Lee Kuan Yew Water Prize 2011

Olympic Sailing Craft in

Algae at Qingdao

Foreign Policy – May/June 2011

As the new year begins, the price of wheat is setting an all-time high in the United Kingdom. Food riots are spreading across Algeria. Russia is importing grain to sustain its cattle herds until spring

grazing begins. India is wrestling with an 18-percent annual food inflation rate,

sparking protests. China is looking abroad for potentially massive quantities of wheat

and corn. The Mexican government is buying corn futures to avoid

unmanageable tortilla price rises. the U.N. Food and Agricultural organization announced that its food

price index for December hit an all-time high.” Increased cost of Fertilizer

BNR

Possible Resource

Recovery

Cooling TowersPotable Water

Heat Recovery

Composting PelletizationIncineration

Irrigation

Used Water

UrineSeparation

PowerProtein Recovery

Gas

Fertilizer

B&V -

8

Comparative Energy

Requirement

Energy used for kWh/c/a

BNR Wastewater Treatment 40

Average pumping for 21 treatment plants 69

Switching one lamp to low energy fixtures (Saving/lamp/a)

102

Pumping water from Missouri River to Kansas City 60

Pumping water from north to south of California 355

Desalination of brackish water 200

Desalination of seawater 525

Office lights for one person at 12 hours per day 1,750

Household per person (2 persons) 9,600

Heat recovery from

effluent

Community College

Nitrification

Nitrifyingbacteria

Ammonification

The Nitrogen Cycle

Decomposers

(aerobic andanaerobic bacteriaand fungi)

Ammonium (NH4+) Nitrites (NO2

-)

Nitrates (NO3-)Nitrogen-fixing

bacteria inroot nodulesof legumes

Precipitation

Plants

Nitrogen-fixing soil bacteria

Assimilation

Nitrogen in atmosphere (N2)

Denitrifyingbacteria

Nitrifying bacteria

Haber-Bosch

Nitrogen removal

The Nitrogen Cycle

N/DN Uses O2 for NN and Carbon for DN

Can be reduced if not going all the way to Nitrate

Anammox bacteria can eliminate carbon while reducing oxygen to 60%

H-B Process

2.8 gO/gN

1.7 gO/gN

4.77gC/g N

Nitrification by slow growing temperature sensitive autotrophs

Conversion of Nitrates to Nitrogen gas

What is denitrification

Carbon Dioxide + Water

CO2 + H2O

Oxygen O2

Nitrogen gas N2

Nitrates NO3

BacteriumSugar

C12 H22 O11

Suspended growth

systems

MLE

Bardenpho

Channel systems

MBR

SBR

Granular activated sludge

Single Stage

Denitrification

ANOXIC AEROBIC CLARIFIER

MIXED LIQUOR RECYCLE

RETURN ACTIVATED SLUDGE WASTE SLUDGE

Q

4Q

NH3 < 0.5 mg/L

NOx < 6 mg/L

TN < 8 mg/L

MBE (MLE)

Bardenpho Process

Anaerobic

Settled Used Water

Aerobic Anoxic Aerobic

P

PAir

Waste Solids with Phosphate

Methanol Optional

Air

N GasN Gas

Effluent

Anoxic

Optional Carbon

EffluentAmmonia N = 0.5 mg/ℓTN < 3 mg/ℓ TP < 1 mg/ℓ

Anaerobic Aerobic Post Anoxic

Water Sludge

Anoxic

Membrane Tank

The future in BNR

Cauley Creek

Membrane BNR Bioreactor

DeOx/DeNit

Anaerobic

Anoxic

Aerobic

Vienna plant uses SND

- Saves energy

Fixed Film Processes

Nitrification Biological Aerated Filter (Biofor, Biostyr) MBBR Trickling Filter Fluidized Bed

Denitrification Biological Filter (Biofor, Biostyr) MBBR Deep Bed Sand Filter (Tetra) Upflow Fluidized Bed (Envirex)

Multi-stage N/DN

DenitrificationNitrification Carbon

Hi Rate AS

CEPT

BAF

TF

MBBR

BAF

Fluidized bed

Denite Filter

MBBR

BAF

Carbon Source

Add on N/DN Systems

Methanol

BAFTetra

Sand FilterHigh Rate

Activated Sludge

Nitrogen recovery

Only viable if less energy is used than fixing Nitrogen from the atmosphere

Can only be considered from high concentration return streams – Cambi as high as 2,000 mg/ℓ

Methods used Ion ExchangeStripping and capture of ammonia

Haber-Bosch process uses about 12 kWh/kg nitrogen fertilizer

Anammox – Demon – Anitamox make recovery even less viable

`

Clinoptilolite Ion Exchange

for Ammonia Recovery

Ammonia Stripping and capture

from return streams - Oslo Norway From

Evans 2009

HNO3 used

for

absorption

Lower portion of

adsorption column

Final Product 54% NH4 NO3

90% nitrogen removal

1.7 gO/gN

0 gC/g N

Phosphorus removal

Options

Biological or chemical

Chemical Phosphorus

Removal

Add chemical to precipitate soluble phosphorus

Alum, ferric chloride, ferrous chloride, magnesium hydroxide, polyaluminum chloride, etc.

Multiple dosing locations

Increases sludge production, consumes alkalinity

Effluent

Filters

Influent

WAS

RAS

Aeration

Raw PS

SCPC Tertiary P

removal

Alum Dosage vs. Target Effluent Phosphorus

0.0

1.0

2.0

3.0

4.0

5.0

0.0

0.5

1.0

1.5

2.0

2.5

3.0

Effluent OP, mg/L

Al3

+/O

P R

ati

o Median Literature

Dosage

Benefits of Combined

systems

It is practically possible to reduce soluble phosphorus to levels as low as 0.07 to 1.1 mg/L biological means only in phosphorus removal plants

Further polishing with chemicals in tertiary treatment can reduce this to an effluent total P of less than 0.05 mg/L

Durham, OR used 175 mg/L of Alum when operating chemical only, added to primary, aeration and post treatment

Reduced to 25 mg/l when applying biological plus chemical polishing to get 0.07 mg/L as P

Pinery Water achieves LT 0.03 mg/L TP with a biological/chemical sequence

Microbiology

3/12

Bio-P Organisms Store PHB and

Release P in the Anaerobic Zone

PHB

Poly-P

Volatile

Fatty Acids

Phosphate

Energy

Facultative

heterotrophs

RbCOD

Influent

Influent

No dissolved

oxygen or nitrates

These are obligate

aerobes. They can

store but not

process

VFA from outside source

or MLSS fermention

Poly-P

Poly-P

PHB

Electron

microscope –

Poly stains

black, PHB

stains white

Bio-P Organisms Oxidize PHB and Remove P in the Aerobic Zone

PHB

Poly-P

Phosphate

Oxygen

Carbon Dioxide +H2O

Energy

(Nitrate)

Stored in anaerobic

zone.

Consumed in aeration basin

providing energy for storage

of phosphorus

Phosphorus taken

up to <0.1 mg/L

Poly-P

Po

ly-p

ho

sp

ha

te s

tore

d in

th

e a

ero

bic

zo

ne

.

Ph

osp

ho

rus is r

em

ove

d w

ith

th

e W

AS

Biological Phosphorus

Removal

Fuhs & Chen, 1975

Typical

Flow

sheets

When using SND

much simpler

process flow

sheets are

possible

VFA and rbCOD Requirements

for P Removal

0.0

5.0

10.0

15.0

20.0

25.0

0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1

Fraction of rbCOD that is VFA

rbC

OD

/P r

ati

o

Eagle’s Point

w/o fermenter

With Fermenter

Durham

VIP

Reedy Creek SC

McDowell Creek

At this point all rbCOD is VFA

At this point

there is no

VFA

This line is used in BNR

models

These plants are getting

fantastic results

Fermenters

Static Fermenter

to digesters

Anoxic

anaerobic

VFA

Oversized Thickener – retain

sludge for 6 to 8 days

VFA to anaerobic zone

Primary tank

Westbank BC

Grimstad Norway

08/06/08

Primary Anaerob Anoxic 1 Anoxic 2 Anoxic 3 Aerobic 1 Aerobic 2 Aerobic 3

5.36 20.56 2.20 1.84 1.60 0.50 0.20 0.03Bioreactor Profile

Phosphorus by Zone

0.00

1.00

2.00

3.00

4.00

5.00

6.00

7.00

8.00

9.00

10.00

Pri

mary

An

aer

ob

An

oxic

1

An

oxic

2

An

oxic

3

Aer

ob

ic 1

Aer

ob

ic 2

Aer

ob

ic 3

Ph

osp

horu

sm

g/L

Westbank WWTP

Note P uptake in Anoxic Zone

Unconventional

Flow-sheets

Bio-P through

Operations

0

2

4

6

8

10

12

14

1/1

/02

4/1

1/0

2

7/2

0/0

2

10/2

8/0

2

2/5

/03

5/1

6/0

3

8/2

4/0

3

12/2

/03

3/1

1/0

4

6/1

9/0

4

9/2

7/0

4

1/5

/05

4/1

5/0

5

7/2

4/0

5

11/1

/05

2/9

/06

5/2

0/0

6

8/2

8/0

6

12/6

/06

3/1

6/0

7

6/2

4/0

7

10/2

/07

1/1

0/0

8

4/1

9/0

8

7/2

8/0

8

11/5

/08

Eff

lue

nt

To

tal P

(m

g/L

)

Total P 30-day Moving Avg (Total P)

St. Cloud, MN(turning the air down in the first pass)

Fermentation of

Secondary Sludge

Anaerobic Anaerobic Anoxic

OFFONInfluent

RAS

AeratedSettling

Effluent

Stripper

Wasted

Biomass

Return Biomass

Influent

Wastewater

RAS

Anaerobic

AeratedSettling

Effluent

Stripper

Wasted

Biomass

Return Biomass

Influent

Wastewater

Lime

Lime

Sludge

Pinery Water CO

Truckee Meadows NV

Sludge partially settled in this zone

and fermented, providing VFA

Fermenting

portion of RAS

Changed from Pho-strip to this

0

100

200

300

400

500

600

700

800

900

1000

0

2

4

6

8

10

12

14

19811982198319841985198619871988198919901991199219931994199519961997199819992000200120022003

Millio

n G

allo

ns

Flo

w

Me

tric

To

ns

To

tal P

City of KalispellWWTP Yearly Phosphorus Loading

to Flathead Lake

Metric Tons Total P Million Gallons Flow Linear (Million Gallons Flow)

Phosphate

detergent ban;

alum additionBNR Plant

on-line 10-22-92

Improved D.O. Improved D.O.

Control

Flow

Trendline

From Joni Emrick

EBPR Operation at

Kalispell, MT

Future Roadmap

Where are we and where would we like to be

Aerobic Nitrifying treatment

(Rock Media TF or other?)

Recycle Pump with

high DO + nitrate

rich effluent

(Bio-gas powered?!)

Anaerobic

Zone

Biogas to vent or

use?

Flow forced

through settled

sludge by

baffles

High void-space

rock media growing

methanotrophic and

other denitrifying

biomass biofilm

“Lo-Tech” Option

UASB

A-recycle

Blower

?

MBB

R

Air

Gas

Generator/Flare

Biogas

Methanotrophic

Denitrification

using Biofilm

Reactor (Anoxic

MBBR or SAF)

“Hi-Tech” Option

McCarty fluidized bed

membrane reactor

Anaerobic Fluidized Membrane

Bioreactor (AFMBR)

Concerns

Since most all the carbon is removed – how to remove nutrients

Utilize methane remaining in the effluent of the anaerobic process

Convert to methanol and use for denitrification

Use chemicals for phosphorus removal

Alternatively use dedicated Ion Exchange for nitrogen and phosphorus removal with recovery of the nutrients

The Ultimate in SND

Granular activated sludge

SBRs with feed during

decant, leading to SND

and P removal

Nereda TechnologyNereda Websitehttp://www.dutchwatersector.com

Granular activated sludge

Dublin 160 mgd plant

uses same technology

Epe - Netherlands

Present Dublin Plant

Fill during decant

Fill during decant

Fill during decant

Fill during decant

SBR Operation

Four basins operated in series all a the same level with fixed weirs

Two basins aerated at any timeOne basin in sedimentation modeOne basin in fill/decant. Flow automatically goes

where valves are open for decanting Continuous flow Black & Veatch design/operating a plant treating a

maximum flow of 260 mgd Very good settling sludge SVI 60 mℓ/g Could be operated to produce granular sludge.

Anammox for side-stream

and main stream

treatment

Return Stream

Characteristics

Temperature is high, 30‐38° C

Ammonia concentration is high

Typically 800‐1000 mg/L NH4‐N Higher concentrations for high solids digesters

Low alkalinity

Typical side=stream contains 50% alkalinity needed

for nitrification of the ammonia

~3.5 mg Alkalinity as CaCO3/mg NH4‐N Relatively low BOD (or COD)

Recycle nitrogen constitutes 15‐25% of nitrogen in the

influent

1.7 gO/gN

0 gC/g N

Anammox Physiology

Anammox bacteria:

Form biofilms and are often

observed as suspended granules or on the surface of synthetic media.

Are strictly anaerobic - reversibly inhibited by DO concentrations as low as 0.03 mg/L.

Are inhibited by high NO2-, but the

threshold concentration is controversial.

Have a remarkably slow growth rate. Reported doubling times are

often as slow as 10 to 20 days.

Principle One Step Anammox® Pacques presentation

2 NH3

+ 1.7 O2 1.14 NO

2- + 0.86 NH

3 0.88 N

2+ 0.24 NO

3-

NH3

NH3

NH3

NO3

-

NO2

-

N2

O2

DEMON installation

with cyclones for

separating the

Anammox granules for

return to the process

Benefits of One Step

ANAMMOX®

B&V DESIGNING BLUE PLAINS WWTP

FILTRATE TREATMENT FACILITY:

DEMON ® PROCESS

69

Largest Anammox installation in the US designed to: Treat 1 MGD from liquid stream filtrate of sludge

processing facility

Removal rate: 12,400 kg-N/day

Schedule:

Design to be completed by late 2013

Final completion date in 2016

Estimate of Probable Construction Cost

$ 47-53 Million

BLUE PLAINS WWTP

ANAMMOX: DEMON ®

PROCESS

70

Paques Plant - Rijn & IJsel –

Olburgen STW

Performance PHOSPAQ & ANAMMOX - effluent to STW:

COD removal 50 %

P removal 80 %

TKN removal 90 %

P.E. 8,600

Influent PHOSPAQ & ANAMMOX:

UASB Effluent Reject water

Flow 3,000 360 m³/d

COD 2,000 200 kg/d

TKN 1,000 250 kg/d

PO4-P 225 20 kg/d

P.E. 47,500 10,000

Characteristics

CASE STUDY: Rijn & IJsel –

Olburgen STW

Application of Anammox to

Main-stream plant

Full-Plant Deammonification

for Energy Positive

Nitrogen Removal

Joint WERF/WEF Webcast

Thursday, November 7th, 2013

1:00 – 3:00 pm Easter

For more information see

Concept – Energy

efficient nitrogen removal

Grow Anammox bacteria in side-stream at high temperature

Waste surplus Anammox bacteria to main stream plant

Use some selection process such as cyclones to concentrate Anammox bacteria from the waste activated sludge

Feed back to main plant

Hi-rate A-B Process

used in the Strass plant

Plant is energy self-sufficient

Second stage SND plant achieves denitrification with minimal energy

input

Side-stream DEMON process for energy efficient ammonia removal

Successful experiments with main plant nitrogen removal

enhancement with surplus DEMON organisms

Future choices for

Nutrient removal

BNR with MBR with little chemicals

Anaerobic membrane with IE for nutrient reduction and capture

A-B process with chemicals for phosphorus removal but energy self-sufficient

Granular activated sludge with little chemicals and possible phosphorus recovery

Membrane Bioreactor

(MBR)

Developed technology for N and P removal to very low levels

Small footprint

High quality effluent

Replaces final clarifiers, filters and disinfection

Disadvantage

Energy intensive

Anaerobic membrane

reactor

Produces energy

Very little sludge production

Methane in solution could be used for denitrification

Needs further polishing for low levels of N & P

Phosphorus must be removed by chemicals thus no recovery

A-B process with SND

Energy self-sufficient

Established technology

Normal footprint

Applicable to existing high rate plants

Needs further polishing for low levels of N

Phosphorus removal by chemicals –recovery expensive

Granular activated

sludge

New but proven technology

Small footprint

Reduced energy use

Very simple operation – low level of mechanical equipment

SND a biological phosphorus removal

Allow for phosphorus recovery

Needs some filtration to reduce effluent TSS and nutrients

Phosphorus Recovery

Phosphorus is a limited

resource

US produces 25% of world resources

Morocco has 6 times the deposits of the US

Production limited to a few countries

In less than 50 years high grade ore will run out

At the present rate of consumption we may have enough for another 200 years

The USA has stopped exporting phosphorus

We cannot afford to use it once and waste it

It is irreplaceable

Future Scenarios

Towards global phosphorus security: A systems framework for phosphorus recovery and reuse options D. Cordell, A.

Rosemarin, J.J. Schröder , A.L. Smit - Chemosphere 84 (2011) 747–758

North America

Struvite

Mg.NH4.PO4. 6 H2O

Also recovers up to 20% of nitrogen

Incinerator Ash

Deposit in dedicated site for future recovery

Summary

Conventional BNR systems have served us well but uses energy and may have a large footprint

Footprint becomes an issue for larger plants

Energy and chemical use needs to be reduced

Alternatives exist for most starting points

Phosphorus recovery is serious

Personal Information

James L. Barnard, Ph.D., D.Ing. hc., BCEE, WEF Fellow,

Dist MASCE

Global Practice and Technology Leader

Black & Veatch

12869 Cambridge Terrace, Leawood KS 66209

Telephone Work 913-458 3387

Mobile 913-963 9498

Email: barnardjl@bv.com