A project financed in the frame of Fuel Cells and Hydrogen Joint Undertaking

Work package 5

28.11.2013 Brussels

Marjut Suomalainen

VTT Technical Research Centre of Finland

Conceptual and Techno-economic study of combined gasification plant and SOFC system

(100 kWth – 1 MWth)

THE AIM OF THE WP5

Conceptual and Techno-economic study of a combined gasification plant and a SOFC system

Analysis of the best structure and best operating conditions of the plants

Technical, economic and environmental evaluation

Partners: VTT, TUM, EPFL

TASKS AND MILESTONES UNTIL MID-TERM

• Task 5.1: GASIFICATION PLANT AND SOFC SYSTEM

Deliverable 5.1 Optimal process concepts for gasification combined SOFC processes

SUBMITTED IN DUE TIME M14

Results will be presented here

Deliverable 5.2 rescheduled from M12 to M30

MS3 rescheduled M12 to M30

Task 5.1: Gasification plant and SOFC system

Technical analysis carried out with ASPEN PLUS simulation software = > Output to WP7 (Demo /Helsinki)

Economical input data from commercial gasifier manufacturers will be used in the models and evaluation work Volter Oy

Hs Energieanlagen

• Techno-economical evaluation will be finalised for case studies in different EU countries

GASIFICATION TECHNOLOGIES Air gasification

1. Viking gasification

2. Downdraft gasification

Indirectly heated steam gasification

1. Heat pipe reformer (HPR)

2. Fast Internal Circulating Fluidised Bed (FICFB)

Downdraft gasification

DISTRICT HEATING

SOFC

POST-COMBUSTION

Flue gases

Air

Air

Electricity

Biomass

DOWNDRAFT GASIFICATION

GAS COOLER

FILTER

H2S ADSORBER

GAS HEATERFILTER

Biomass

FARM DIGESTION PLANT

GAS COOLERAIR

HEATER

Viking gasifier

Heat pipe reformer

Fast internally circulating fluidised bed gasifier (FICFB)

Comparison of gasification technologies

Operation and performance data

Air blown gasification Indirect steam gasification

Viking gasifier Downdraft

gasifier FICFB BioHPR gasifier

Economically and technically feasible in stand alone operation

MWth 0.6 - 3 < 2 8 - 20 0.5 - 8

Typical main producer gas composition

% (vol dry) H2 23 15 26 44

% (vol dry) CO 19 22 9 20

% (vol dry) CO2 12 10 15 19

% (vol dry) N2 33 51 0.07 7

% (vol dry) CH4 0.3 2 6 7

Lower heating value of producer gas

MJ/m3n 7 3-7 9-10 approx. 11

Maximum operation pressure

bar atmospheric atmospheric 1-7 1 - 5

Typical tar content g/m3n 1

low (around 1 or below)

10 2-20

Mature of the technology - New technology Old technology New technology New technology

Developer - University of

Denmark

Old technology. different

developers. different solutions.

commercialised

Vienna University of Technology

TUM

State of commercialising - Not yet Commercialised Commercialised Commercialised

GASIFICATION IMPURITIES

Gasification impurities

Raw gas

SOFC limit

Tars Downdraft < 1 g/m3n

CFB ̴ 10 g/m3n

HPR 2 – 20 m3n

Updraft 50 g/m3n

Not known

Sulphur compounds H2S COS

50 – 200 ppm 10-20 ppm

1 ppm

Alkalimetals Na, K < 50 ppm (max) Not known

Halogens HCl <10-20 (max) 1 ppm

GAS CLEANING OPTIONS

Impurities Gas cleaning methods

Hot Cold

Tars and hydrocarbons

Catalytic reforming high temperature (up to 950 oC)

Scrubbing (for example RME)

Particles Filter up to 500 oC Scrubbing Filter

Sulphur Adsorption (ZnO)

up to 400-450 oC Adsorption (for example metal oxide) Scrubbing (for example with CuSO4)

Alkalimetals Filter below 500 oC Filter

Halogens

Adsorber or Filter with Ca-based sorbent injection

Scrubbing Filter with Ca-based sorbent injection Adsorber

COMPOSITION OF PRODUCER GAS IN DOWNDRAFT GASIFIER

GAS CLEANING SECTION OF HPR

Parameter Before gas cleaning After gas cleaning

PG composition (wet)

H2O vol-% 35.8 33.7

H2 vol-% 27.3 29.3

CO vol-% 14.8 12.7

CO2 vol-% 13.4 15.5

CH4 vol-% 6.8 6.8

N2 vol-% 1.9 1.9

H2S ppm 91.4 1

COS ppm 2.2 0

HCl ppm 84.7 0.1

NH3 ppm 5.2 5.2

Carbon particles kg/h 0.857 9.23*10-4

Ash particles kg/h 0.064 3.85*10-4

Tars g/Nm3 4 0.45

Hot and cold composite curves of FICFB and Viking gasifier

SUMMARY OF DIFFERENT SYSTEMS

Downdraft VK-SMR-SOFC-GT

FICFB-SMR-SOFC-GT

Heat pipe reformer

Thermal energy input kW 235 90 90 500

Net power output kW 64 54 58 180

Net Electrical efficiency of the plant (LHV)

% 27 60 65 36

District heating kW 88 - - -

CONCLUSIONS

• Planned work has been succesfully completed

Deliverable 5.1 submitted in M14

• Further work progressing well and in schedule

– Task 5.1 will be finalised in report D5.2 in M30

MS3 in M30

– Tasks 5.2 and 5.3 (potential impact and LCA) will be based on the results from task 5.1

Deadlines D5.3 and D5.4 in M36

Progress after mid-term

• Task 5.1 will be finalised in report D5.2 in M30

• Progress after mid-term in task 5.1

– Agreement on the common features

– Cases to be studied

– Cost of gasifiers

– Subsidies

• Tasks 5.2 and 5.3 (exploitation and LCA) will be based on the results from task 5.1 and Helsinki demo (WP 7) – D5.3 and D5.4 are due in M36

Cases to be studied

Scale Case ID

Gasification technology

Power

[MWth]

Pressure

[bar]

Hot gas cleaning

Tar removal Particle removal

Sulphur removal

SMALL

1 Downdraft 0.1 Atm Not

required

Ceramic filter

Adsorption (ZnO)

2 Viking 0.1 Atm Steam

reforming

Ceramic filter

Adsorption (ZnO)

3 FICFB 0.1 Atm Steam

reforming

Ceramic filter

Adsorption (ZnO)

MEDIUM

4 FICFB 8 atm – 7 bar Steam

reforming

Ceramic filter

Adsorption (ZnO)

5 Heat pipe reformer

8 atm – 5 bar Steam

reforming

Ceramic filter

Adsorption (ZnO)

6 CFB + O2 8 15 - 30 Steam

reforming

Ceramic filter

Adsorption (ZnO)

Basic subsidies for biomass gasification combined SOFC

0

50

100

150

200

250

300

0 1000 2000 3000 4000 5000 6000 7000 8000

Bas

ic s

ub

sid

y, €

/MW

h

Power kW

Germany Italian Switzerland Finland

THANK YOU FOR YOUR ATTENTION

• Questions?