demonstration of the dmx™ process descripppjtion of the ... pdfs/8_3_pccc2... · demonstration of...

Renewable energies | Eco-friendly production | Innovative transport | Eco-efficient processes | Sustainable resources

Demonstration of the DMX™ processdescription of the Octavius SP3 projectp p j

Ludovic Raynal1, Cristiana La Marca2, Jan Mertens3, Laurent Normand4 and Paul Broutin1Laurent Normand and Paul Broutin

+ other colleagues !1IFPEN, 2ENEL, 3LABORELEC, 4PROSERNAT

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IEA-GHG 2nd Post-Combustion Capture Conference

17th -20th September 2013, Bergen, Norway

Outlook

Octavius project

DMX™ process

SP3 : Demonstration of the DMX™ process

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OCTAVIUS in Brief Optimisation of CO2 Capture Technology Allowing

Verification and Implementation at Utility ScaleFP7 Project (Call DG Energy 2011)FP7 Project (Call DG Energy 2011)

Start-up: 01/03/2012 Duration : 60 Months Coordinator IFPEN

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Total Budget: 13.56 M€ EU Funding: 7 96 M€

Kick-off Meeting on 13-14 March 2012 in Solaize

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EU Funding: 7.96 M€

17 Partners + 1 Sponsor

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Sub-Project SP3 Sponsor: TOTAL (F)

OCTAVIUS Organisation

2 main technical Sub-Projects SP2 dedicated to demonstration of operability and flexibility

aspects of first generation processes to be used for first full scale demo plant (ROAD and Porto Tolle Projects)

SP3 dedicated to the demonstration of the DMXTM process 2 independent Subprojects

a R&D Sub-Project

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a R&D Sub Project SP1 will support SP2 & SP3 and will also include cross-

cutting issues such as benchmarking activities

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Outlook

Octavius project

DMX™ process


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Post-combustion capture@ IFP Energies nouvelles

Development of new PCC processes G1 : industrial pilot tests => commercialization HiCapt+™ : 40 wt.% MEA + additives

G2 : R&D developments => industrial pilot tests DMX™

G3 : laboratory studies – proof of concept

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new chemistry solvents, sorbents, hydrates...

Development of new technologies

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Development of new technologies gas/liquid contacting devices ...

HiCapt+ process Degradation tests

very good performances of the oxidative inhibitor Corrosion tests

MEA 40 wt % after 1000 h mini-pilot test (with and

without inhibitor)

Identification of materials with no corrosion in presence of the oxidative inhibitor (e.g. Duplex steel)

Price difference is very small (higher cost but less material since better mechanical properties) + availability of material is industrialbetter mechanical properties) + availability of material is industrial

20000

25000

30000

on (

ppm

)

250

300

350

400formiate

acetateoxalate20000

25000

30000

on (

ppm

)

250

300

350

400formiate

acetateoxalate

5

6

7

8 NoneU1U2V1V2V3

0.12

0.14

5

6

7

8 NoneU1U2V1V2V3

0.12

0.14

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0

5000

10000

15000

Ani

on C

ance

ntra

tio

0

50

100

150

200

250

U2 V1 V2 Y1

nitratenitrite

0

5000

10000

15000

Ani

on C

ance

ntra

tio

0

50

100

150

200

250

U2 V1 V2 Y1

nitratenitrite

1

2

3

4

5N

H3

mM

/hV3W1W2W3Y1Y2

0.00

0.02

0.04

0.06

0.08

0.10

0 50 100 1501

2

3

4

5N

H3

mM

/hV3W1W2W3Y1Y2

0.00

0.02

0.04

0.06

0.08

0.10

0 50 100 150

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0none U2 V1 V2 Y1

Inhibitors (0,25%-wt)

MEA 40% at 80 C under air + CO2 during 12 days

0none U2 V1 V2 Y1

Inhibitors (0,25%-wt)

MEA 40% at 80 C under air + CO2 during 12 days MEA 30% at 80 C under air + CO2 during 7 days

00 20 40 60 80 100 120 140 160 180

Time (h)

MEA 30% at 80 C under air + CO2 during 7 days

00 20 40 60 80 100 120 140 160 180

Time (h)

Pilot plant presentationMain Characteristics

CCS unit – Main equipments

Absorber1 / 4 Фi = 1.5 m / HLT = 45 m

3 stages solvent inlet Stripper

Фi = 1.3 m / HLT = 31 m Reboiler : Kettle type ~ 1 to 3 MWth

Solvent / Solvent cross heat exchanger

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Plates type

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HiCapt+ main conclusionsLong run industrial pilot test main results (Enel – Brindisi)

Test duration : 380 h CO2 prod. : 2 327 kg/h Efficiency : 89,7 % Loadings : αL = 0,23 αR = 0,48 Energy : ~ 3,02 GJ/tCO2 in good agreement with process simulations ready for in good agreement with process simulations

Lab and mini-pilot test main results (IFPEN)

ready for commercialization

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no or little degradation much lower emissions

i ith D l ( i h t i )

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no corrosion with Duplex (even in hot regions)

Gas Treated

CO2 lean amine

LP CO2 HP CO2

DMX™ ABSO

STRI

DecanterLean amine

CO2 richi

ORB

ER

IPPER

Flue Gas

amine

CO2

Rich amineReboiler

Leanamine

DMX-1™ : a low stripping low heat ofDMX 1 : a low stripping, low heat of reaction, high capacity demixing solvent

+ lower degradation (and further lower emissions => interest in HP stripper) //

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CO2 lean phase

emissions > interest in HP stripper) // no corrosion

2.5 – 2.1 GJ/ton CO2

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CO2 rich phase -20-30 % in CO2 total cost

Scientific & Technical information VLLE data + adapted thermodynamic model Degradation / Emissions / Corrosion Operational issues Kinetics & Mass transfer performances Laboratory and mini-pilot testsy p Process simulations / cost evaluations

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DMX-1 Process – Full Scale Unit PFD23

20

11E104

21

22

E105V102

24

K201ACOMP

14

25

E102

11

10T101

Amine makeup

17

18

12

V103E102

6bP102

P101

Water makeup

To Water makeup

V1

7

C102

E101E

2

V101A

C101

V2

3

E101A

6

14

16P104

C1004

5b

V101C

P102

4.6 bar

V3

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1

E106

13

3

5

P101

K101

C100

E301

P301

P302

P102

P303

7.97.7

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P303

P304

Steam Cycle Simulation: IFPEN model Temperature and pressure levels available

T=602°CP=278 bar

T=410°CP=90 bar

T=600°CP=56.8 bar

T=462°CP=24.3 bar

T=377°CP=13.4 bar

T=355°CP=61.4 bar

T=285°CP=6.5 bar

T=189°CP=2.7 bar

T=105°CP=1.09 bar

T=67°CP=0.27 bar

T=27°CP=0.035 bar

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Thermodynamic model: ASME 1967 steam table correlationsHeat Exchanger pinch: 5 °C, pressure drop neglected

Outlook

Octavius project

DMX™ process


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Methodology

Full scale -feasibility study

PilotLab

MethodologyFrom lab to Pilot demonstration

- Process testing- Analytical methodologies

development

Flue gases : 10.000 Nm3/hCO2 : 2500 kg/hProcess modeling - Process Design

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- Validation of design- Emissions measurement and

waste characterization- Development and testing

modeling tools

• Criteria for technology scale-up• Full scale application Capex and

Opex evaluation (cost of CO2 avoided)

• Basic engineering

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modeling tools • Basic engineering

SP3 Structure & Objectives

SP3 Objectives

The main objective of SP3 is to demonstrate the DMX TM process on pilot scale and study its application to coal power station and NGCC units with industrial pilot test on the Enel’s coal fired power plant of Brindisi.

SP 3: Demonstration of the DMXTM process

p p

WP 3.1Definition of the Brindisipilot plant revamping

WP 3.2Retrofit of the Brindisi pilot

plant

WP 3.3Demonstration of the DMX process

WP 3.4DMX

Evaluation for PC case

WP 3.5DMX

evaluation for NGCC case

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Go / No Go decision11th Dec. 2013

Technical Criteria :energy consumptionsolvent degradation and emissionmain component design criteria

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HSECapex and Opex of full scale application

Financial Criteria : cost of retrofit (budget !)

SP3 Work Packages Description – WP3.1WP 3.1: Definition of the Brindisi pilot plant revamping

Participants: IFPEN, Enel, Laborelec/GDF SUEZ, Prosernat

Objectives

• Define modifications to be carried out on Enel Brindisi CO2 capture pilot plant to test DMX• Design and Estimate the cost of the pilot revamping

TaskTask

• 3.1.1 Experimentation of DMX on Enel minipilot at Brindisi lab facilities and at IFPENresearch centre• 3 1 2 Experimentation at IFPEN on decantation rate on a representative cold mock-up

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3.1.2 Experimentation at IFPEN on decantation rate on a representative cold mock up• 3.1.3 Preliminary process study– full scale case• 3.1.4 FEED for Enel CO2 capture pilot plant revamping• 3.1.5 Cost estimation of revamping

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Minipilot activities - Enel mini-pilot

Brindisi pilot:

Sensitivity test: to optimize the mini-pilot plant

operating conditionsp g

Long run test: focused on the study of solvent’s

degradation / emissions in the optimized g p

conditions.

Flue gas condition Brindisi pilot:

E i i t ti i ti f

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Laborelec via FTIR measurements (with

calibration at IFPEN)

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Lab & Minipilot activities – IFPEN

Target :Bottle-tests decantationUltaturrax – 11,000 rpm

dmax (mm)

fresh case 3.9

degraded 2.5

Demixing test to decanter design

Capture efficiency (lean and reach loadings)

Solvent degradation g

Semi-open batch reactor degradation testsT = 80°C, Patm

Emission

Corrosion

IFPEN Lab test

VLE data + adapted thermodynamic model

Degradation / Corrosion and other % amine lossa [formiate]

T 80 C, PatmPO2 = 200mbar PCO2 = 4.6mbarVsolvent = 130 ml1 week

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Degradation / Corrosion and other

operational issues

Kinetics & Mass transfer performances

L/L decantation – effect of degradation

[ ]ppmb

DMX-1 6% 100

MEA 58% 19000

Ratio 0.10 0.005

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L/L decantation effect of degradation

a : GC analysisb : IC analysis

Lab & Minipilot activities – IFPEN

Target :

Demixing test to decanter design

Capture efficiency (lean and reach loadings)

Solvent degradation

Emission

Corrosion

IFPEN mini-pilot

Mechanical/validation tests : T1 2013

Operation on a 24/7 basis

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Operation on a 24/7 basis

Long run tests on MEA (reference case) : 1000 hrs

Long run tests on DMX : in progress

Operation on representative synthetic gas (SOx/NOx)

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Operation on representative synthetic gas (SOx/NOx)

Full scale application and costing

Preliminary process study for application on a 660 MWe power plant, comparison between two cases:

Assessment of the energy consumption :

comparison between two cases: MEA 30% (benchmarking) DMX

Assessment of the energy consumption : Process scheme definition (steam turbine and capture process):

Definition of the steam turbine scheme and optimization for the two cases Simulation and evaluation of the impact on the thermal cycle for each capture Simulation and evaluation of the impact on the thermal cycle for each capture

process CAPEX and OPEX estimation:

Definition of the method

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Final comparison based on : LCOE

C t f CO2 id d

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Cost of CO2 avoided

FEED study for Enel’s pilot revamping

Pre-FEED in 2012 with strong interaction betweenENEL / IFPEN / PROSERNAT teams

FEED : ENEL engineering + PROSERNAT withf IFPENsupport of IFPEN

Kick-Off Meeting in Milan (28th May 2013) basis of design Heat and Mass Bances

PFD PID PFD – PID piping classes list of chemicals Process Data Sheets of main/retrofitted equipments Instrument list + controls

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Operating manual Cost estimation

HAZOP meeting (30th Sept. 2nd Oct. 2013)

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Final documents for November

23

Conclusions & perspectives Conclusions

HiCapt+ : a G1 process (MEA 40wt.% + proprietary oxidation inhibitor + material recommendation) => PROSERNATinhibitor + material recommendation) => PROSERNAT

DMX-1™ : a promising G2 process under development for reducing energy penaltyl d ti i i il t t t FEED t d f E l’ il t long duration mini-pilot tests + FEED study for Enel’s pilot retrofit under progress

Future steps

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Octavius EU project - Go/NoGo milestone Dec. 2013 (technical – financial criteria – budget !)

tests of DMX-1 on Enel's Brindisi industrial pilot for further

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pevaluation on full scale cases – tests in 2015-2016

process ready for commercialization T1 2017

demonstration of the dmx™ process descripppjtion of the ... pdfs/8_3_pccc2... · demonstration of...

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