DANA

D.AN.A

Dynamic

Anaerobe

Aerobe reactor

Antoine Engelaar

Actual high rate reactors: UASB en IC

Bacterial grow on heavy granular sludge:

Mixing energy is necessary to prevent for settling of sludge,

recirculation system needed (high V-up >2-3 m/hr).

•Complex settlers systems necessary for the separation

of sludge, water and biogas.

•Sludge lost during organic overload periods (floating due to high

gas production).

•Special tanks of specific sizes made of concrete, SS, coated steel•Special tanks of specific sizes made of concrete, SS, coated steel

necessary for the installation of the settlers.

•High transport budgets for the transport of tanks and settlers

•Aerobic treatment necessary

•Specific conversion UASB reactor 10-15 kgCOD/m3/d.

•Specific conversion High Rate reactor 25-35 kgCOD/m3/d.

.

Impression UASB

Expensive settlers necessary

Impression High Rate Reactor

SS reactor with internals

Revolutionary high rate reactor: DANA

•Bacterial grown on floating carrier material, floating sludge bed.

Pro’s

•NO potential settling of sludge.

•NO complex settlers internals necessary.

•NO sludge lost caused by high organic loads.

•NO specific tank sizes necessary.•NO specific tank sizes necessary.

•NO specific special transports necessary to the location.

•Aerobic treatment combining in one concrete tank.

•Specific conversion DANA reactor 15-30 kgCOD/m3

DANA total concept

•Anaerobic (under) •Aerobic (top)

•Biogas buffer and biogas flare on top of the tank:•Extremely compact system.•Investment reduction >30%

DANA LOW COST

•Anaerobic (left)

•Aerobic (right)

•Gas buffer integrated in gas roof ..

•Materials from mature/fight market

•Materials proven as long lasting

•Materials global available

•Investment reduction >40%

DANA RETROFIT

•Aerobic reactor transferred into anaerobic reactor.•Reuse of existing concrete structures. •Taylor made gas roof including gas buffers available•Price reduction > 50%

.

DANA Pilot

Potato factory, pilot April 2010 - March 2011 •Inlet 5.000 - 10.000 mgCOD/lit, •Inlet Ntot 100-250 mgN/lit.•Inlet TSS 500-1200 mg/lit•Influent flow 200-350 lit/hr•HRT 6-10 hr

DANA Pilot

Start-up

•Seed sludge End of Pilot trail

15

20

25

50%

60%

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100%

VLR

(k

g/m

3/d

)

COD conversion (%) in relation to the volumetric loading rate (VLR)

DANA Pilot start-up

0

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2 3 5 9 11 14 16 19 24 27 30 31 34 37 39 42 45 47 51 54 60 63 67 70

VLR

(k

g/m

3/d

)

Time (d)

Anaerobic Anaerobic + Aerobic VLR

50%

60%

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80%

90%

100%

% C

OD

co

nv

ers

ion

COD conversion Anaerobic

DANA Pilot results

0%

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% C

OD

co

nv

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25,0

30,0

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45,0

CV

LR k

g C

SB

m3

Ta

g

VLR based on reactor volume

VLR Anaerobe

DANA Pilot results

0,0

5,0

10,0

15,0

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25,0

CV

LR k

g C

SB

m VLR Anaerobe

60%

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CO

D C

on

ve

rsio

n

COD conversion after aerobic polishing (carrier vol. 10 %)

DANA Pilot results

0%

10%

20%

30%

40%

50%

% C

OD

Co

nv

ers

ion

DANA Pilot results

Potato factory, pilot April 2010 - March 2011

•Biogas production 0,4 - 0,43 m3/kgCOD removal•Biogas CH4 78-82 % CO2 18-20 %, H2S <0,25% •Caustic consumption minimized (< 0,01 kg/kgCOD ) due to external (an)aerobic effluent recirculationexternal (an)aerobic effluent recirculation•Anaerobic sludge/biomass growth 0,5-1 %/kgCOD removal.

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