New business opportunities based on biogenic carbon dioxide - - PowerPoint PPT Presentation

22.10.2018 VTT – beyond the obvious

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New business opportunities based on biogenic carbon dioxide utilization

Janne Kärki

14th International Conference on Greenhouse Gas Control Technologies, GHGT-14 21st - 25th October 2018, Melbourne, Australia

From IPCC Special Report 15

(Published 8.10.2018)

“CO2 emissions from industry in pathways limiting global warming to 1.5°C are projected to be about 75–90% lower in 2050 relative to 2010.“ “Such reductions can be achieved through combinations of new and existing technologies and practices, including electrification, hydrogen, sustainable bio-based feedstocks, product substitution, and carbon capture, utilization and storage.”

http://www.ipcc.ch/pdf/special-reports/sr15/sr15_spm_final.pdf (page 21)

• Container scale, easy to transport, easy to

connect to gas streams

H2 SOURCES CHEMICALS FUELS

SYNTHESIS REACTORS @VTT

FISCHER-TROPSCH & CO2 METHANATION CO2 SOURCES

Kestäv ävää ää kasvua a ja työtä-oh

• hjel

elma

Outline

• 1. Chemical-looping combustion for a

biomass fueled CHP plant enabling negative emissions

• 2. Polyols from (biogenic) CO2 and

renewable power

• 3. Paraffinic wax production from CO2 via

Fischer-Tropsch (FT) synthesis

• 4. Demonstration of P2X process

technical feasibility

Chemical-looping combustion for a biomass fueled CHP plant enabling negative emissions

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Tomi Thomasson, VTT

Finding the business case in bio-CLC

• The need for negative emissions
• vs. the lack of incentives

22.10.2018 VTT – beyond the obvious

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• Chemical-looping combustion of biomass

(bio-CLC) enables:

• Low operational capture costs

(15-25 €/tonCO2)*

• Relatively low capital costs
• High total efficiency
• Potential for integration

– would combining CLC with CCU increase the feasibility?

* Anders Lyngfelt, Bo Leckner (2015)

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CO2

CHP

Venting Processing Purification Buffer storage Oxy- polishing Cryogenic

• xygen plant

Formic acid

(or methanol, methane, other hydrocarbons)

O2 H2 Electrolysis

FCR

Storage 1) CHP plant for base demand 2) Heat-only boilers (HOB) for peak demand 3) CCS added to the system 4) CCU added to the system

Heat and power from CHP Oxygen from electrolysis

9 MW 3 MW 18 €/MW 1.4 tonO2/h 0.2 tonH2/h 100 €/tonO2 1.9 tonO2/h 0.7 €/kg 0.9 ton/h 1 MW 8 MW 10 €/tonCO2 0-50 €/tonCO2 0 €/tonCO2 30 tonCO2/h

• max. 30 tonCO2/h
• max. 3 tonCO2/h

0-88 MW 0-37 MW 0-88 MW 0-50 €/tonCO2 7 €/tonCO2

HOB

CCS and CCU complement each other

• CHP generates heat and power flexibly
• CCU provides oxygen and load for CHP

Integration of CCU is beneficial…

• Decreases fossil CO2 emissions on

system level

• Notable income from frequency

containment reserve (FCR) … but overall, still not economically sensible

• Investment cost should decrease by 20%
• Feasibility relies on subsidized negative

emissions

Key findings of the bio-CLC study

• 4
• 2

2 4 No subsidy Subsidy Air-fired CLC CLC + formic acid CLC + methanol CLC + methane Net profit (M€/a)

Polyols from (biogenic) CO2 and renewable power

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Kristian Melin, VTT

Background and motivation

• Polycarbonates and polycarbonate polyols have growing markets

with total demand of tens of millions tons annually.

• In technologies based on fossil epoxides the carbon dioxide

content is typically 20 - 40 %.

• With the studied CO2-to-olefins technology, polycarbonates with

100 % carbon originating from CO2 can be produced and on commercial scale millions of tons of CO2 could be used annually!

• Techno-economic (TEA) performance of a suitable process

concept was evaluated for a 30 kt/a polycarbonate polyol plant integrated to a pulp mill environment

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Process Concept and TEA assumptions

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Hydrogen production by electrolysis Combined reforming and rWGS Olefin production by FT Olefin oxidation by peroxides Polymerization

• f epoxides

with CO2 Electricity Water

H2 O2

CO2 from flue gases

Recycle of methane, C5+ and CO2

Peroxide from the market

• r produced on-site

CO2 from flue gases

Polycarbonate polyol

Inputs Price Outputs Price Other parameters Power (produced at pulp mill) 34 eur/MWh Polycarbonate polyols 2500 eur/t Plant capacity 50 MW power input Hydrogen peroxide 1000 eur/t By-product gas from FT- synthesis 45 eur/MWh Annual CO2 use 60 kt Water for electrolysis 0.4 eur /m3 Steam 8 eur/MWh Annual polycarbonate polyol production 30 kt CO2 50 eur/t By-product heat 0 eur/MWh Annual plant operation 8400 h Oxygen 41 eur/t Annuity factor for 20 years investment time and 10 % rate on invested capital 0.117

TRL 9 TRL 5-6 TRL 3-4 TRL 3 TRL 3

Results

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• Estimated investment cost

100 Meur ± 30 Meur

• Payback time approximately

2 years depending on the polycarbonate polyol price

• Note! The estimates are based
• n assumptions of several

low-TRL technologies that need still experimental verification

Paraffinic wax production from CO2 via Fischer-Tropsch synthesis

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Marjut Suomalainen, VTT

Drivers and background

• Paraffinic wax is used as raw material in thousands applications
• Global market demand ~3 Million t/a
• Both demand and price increasing since 2015
• Presently the main raw material is fossil crude oil
• Via FT-synthesis non-fossil originated raw material can be used
• Study focus: Feasibility estimation of a small-scale FT system

producing paraffinic wax as main product

• Located in Finland
• Integrated to a CO2 emitting biobased industrial source

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• By-products
• Pure oxygen 11 500 t/a (50/15 €/t)
• FT-liquid (light paraffinic oil) 1100 t/a (0.6 €/l)
• District heat 36 700 MWh/a (70/55 €/MWh)
• Electricity consumption 11 MWe (39/45 €/MWh)
• CO2 consumption 13 000 t/a

Electrolyser Syngas & FT conversion FT- liquid (C5-C18) CO2 absorption

Water CO2 Electricity H2 O2

Paraffinic FT-wax (C18+)

Heat Raw material to for example candles Replacing heating gas oil O2 CO2 containing gas

Chemical production from CO2 via Fischer-Tropsch synthesis

• Main product paraffinic wax 1500 t/a, utilissed

in a local candle factory

• CO2 rich gaseous emission stream derived

from biobased process

• Electricity from the markets
• Optimistic and realistic price assumptions

Production cost of paraffinic wax

0,0 0,5 1,0 1,5 2,0 2,5 3,0 15 20 25 30 35 40 45 Production cost of paraffinic wax, €/kg Electricity price (inc. taxes and other payments), €/MWh

Production cost of paraffinic wax

Realistic base case Optimistic base case Realistic util. 65% Optimistic util. 65%

Key findings:

• Production cost (1.4 €/kg) in
• ptimistic scenario exceeded

the market price of fossil-based competitor (> 1.1 €/kg)

• Electricity and CAPEX are the

most significant cost factors

• Integrating the concept with

industry both producing CO2 and utilising by-products

• xygen and heat is crucial for

the economic viability

Demonstration of P2X process technical feasibility

Power-to-X (P2X) route for liquid and solid hydro-carbons production. Utilizing biogenic CO2 from bioethanol production which is currently vented out from the fermentation process. Location: St1 biorefinery @ Jokioinen, Finland

Bio-CCU demonstration

See VTT's press release for further info

The demostrated P2X scheme

• Gaseous fraction (C1-C4) ~20%
• Gasoline fraction (C5-C12) ~25%.
• Diesel fraction (C13-C18) ~15%.
• Heavier fraction mainly waxes (C18+) ~40%.
• Small amount of n-alcohols and olefins.

Liquid HC: 3-5 litres/day Solid HC: 6-9 litres/day

Opening event 9th of Oct

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Acknowledgements and further info

European Regional Development Fund (ERDF) for funding Bio-CO2 and Bioeconomy+ projects

janne.karki@vtt.fi

www.vtt.fi/sites/BioCO2/en www.vtt.fi/sites/bioeconomyplus

Negative CO2 research project