WP1 - Basis for the project studies
Transcript of WP1 - Basis for the project studies
COCATE South Africa Workshop - November 8th , 2012 http://projet.ifpen.fr/Projet/cocate
COCATE
WP1 - Basis for the project studies
COCATE South Africa Workshop -
November 8th
, 2012
http://projet.ifpen.fr/Projet/cocate
WP1 Leader : M. Samuel, LHDPresenter : Y. Le Gallo, Geogreen
COCATE South Africa Workshop - November 8th , 2012 http://projet.ifpen.fr/Projet/cocate
Work Package 1 -
Global capture to storage transport network
WP1 occurs in two distinct phases:
collecting and treating data
in order to build the basis for the rest of the project (provision of input data for each work package).
collecting the results
from the other work packages in order to put together an integrated methodology and strategy for the deployment of such large-scale CCS infrastructures.
Le Havre
Rotterdam
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Flue gas/solvent collection networks
Source 1
Source 2
Source 3
Source 4
Source 5
…
Pooling Centre
#1
Pooling Centre
#2
Hub
Source x
Rotterdam
Hub Rotterdam
Flue Gas/Solvent collection network
Le Havre
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Work Package 1 –
First phase description
The first phase, purpose of this presentation, aims at defining a full network from sources to sinks, taking into consideration the following elements:
flue gas and CO2
pooling networks (D1.1.1, D1.1.2, D1.1.3, D1.1.2b)
two options to export CO2
one by pipeline, another by boats towards a hub located in Rotterdam
for an ultimate storage in the North Sea
(D1.1.5 and D1.1.6) (storage aspects are not included in the project).
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CO2 Breakdown of emissions in Le Havre and Port Jérôme areas - 2009
9%
1%
28%
6%4%
27%
25%
Refinery #1
Refinery #2
Petrochemical industries
Others (Incinerator, car manufacture,glasswork,compressor test platform)Coal Power Plant
Chemical industries (Ammonia & urea production,industrial gases production)Cement Factory
TOTAL CO2 EMISSIONS CONSIDERED: 14.5MTCO2/y
85 point sources Post Combustion
14.5MtCO2
/Year emitted
D.1.1.1 Data Collection and Pooling Scenario Definition
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D.1.1.1 The 85 sources considered
Le Havre Area ~11 MTCO2
Port Jérôme Area ~3.5MTCO2
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D.1.1.1 Distribution of CO2
concentrations
[CO2] distribution
1
9
34
37
31
0
5
10
15
20
25
30
35
40
<1 1<[CO2]<5 5<[CO2]<10 10<[CO2]<15 15<[CO2]<20 20<[CO2] ; max : 55.5
[CO2] (%wet vol)
Num
ber o
f sou
rces
Most of the concentrations are ranging from 5 to 15 % which is the typical concentration coming from combustion processes
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D.1.1.1 Characteristics
of the flue gases
T from
70 to 470°C
Most of the temperature
from
100 to 250°C
P from
below
1 atm
(cement
factory) to 1.1 bara
H2
O from
5 to 30%
O2
~50% of the streams
have composition from
0 to 5%
~50% of the streams
have composition from
5 to 10%
NOx
from
0.0001 to 0.04%
SOx
from
0.001 to 0.6%
CO from
0.0002 to 0.4%
Other
possible components: VOC, N2
O, CH4
, HF, HCl, Ar, Heavy Metals.
Particulate
matters
from
0 to 200mg/Nm3
Some data are not measured thus not available:particles size, pH
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D.1.1.1 5 Pooling
centers
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D.1.1.1 2 alternative solutions in Le Havre
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Main assumptions for the design of the pipelines
Flue gases are sent as they are at the bottom of the stack into the flue gas collecting network;
The design is made for the peak flowrate;
They are just boosted at the level of CO2
sources
The pipeline diameter cannot exceed 80”
(maximal value available in the API 5L standards);
The minimal thickness of the pipeline is calculated using the Maximal Allowable Operating Pressure and taking into account a corrosion allowance;
The change in elevation is taken into account;
A heat transfer is considered (with air when pipelines are aerial and with ground if buried)
D.1.1.2 Design and report on flue gas pooling network
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Flue network:
The routing follows existing networks ;
Pipelines are either aerial or buried (outside of industrial sites)
Total length from 25 to 31 km
Pipeline diameters vary from 2”7/8 to 80”.
Powers required at the blower’s level vary from 0.01 to 175
MWe.
First identification of risks:
Pipeline size;
Transport of hot streams;
Leakage;
Corrosion;
Material defect;
Potential collision.
D.1.1.2 Design and report on flue gas pooling network
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D.1.1.2 Pipeline Design: Example
of results
IGP
R2
IGP
R2
Blower's location Power required at the blower's level (MW)
B5-1 2,3+0,6B5-2 1,1+0,8+0,5B5-3 0,3
B5-4 1,1+0,5B5-5 0,4B5-6 0,3B5-7 1
B5-8 0,2B5-9 2,2
B5-10 0,9+0,6 B5-11 4,6+2,3B5-12 4,2+0,2B5-13 0,7
B5-14 (Inter 1) 1,2 B5-15 3,8+1,4+1+1,2+1+1
B5-16 (Inter 2) 2,4B5-17 0,3
Legend D (")806056524032282620
12 3/48 5/8
Blowers
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D.1.1.2 Conclusion
Required power is unrealistic for some sources.
Proposal are considered: 1. Either change the assumptions and work on average flow rate
and not on maximal flowrate, or take into account the velocity limit (number of pipelines in parallel / higher power)
2. Study feasibility of local absorption, and transport the solvent (liquid) up to a regenerator
a new deliverable: D.1.1.2B
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Re-design the flue gas collecting network considering the following assumptions
Flowrates
considered in this study are the maximal flowrates
on a monthly basis and not the instantaneous maximal flowrates
To cope with the velocity limitation specified in D.2.2.1, there are
two options:
The Low pressure option
Increase the pipe diameter and/or lay some pipelines in parallel
The High pressure option
Increase the pressure of the flue gas at the inlet of the network.
For high
flue gas
flowrates, study
of the amine transport instead of the flue gas
Absorption units
located
close to the emission points
Transport of the CO2 amine rich flue from the absorber to the regenerator located at the pooling centre level
Recycle of the “clean”
amine stream to the absorption site.
D.1.1.2b Alternative flue gas/amine collecting network design
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D.1.1.2b Flue gas collecting Network –
Options compared
FG Blower
FG Blower
FG Compressor
FG Treatmentbefore Absorption
CO2Absorption
Amine Regeneration
CO2Absorption
CO2Absorption
Amine Regeneration
CO2Absorption
Amine Regeneration
Pump
Pump
Amine Regeneration
FG Treatmentbefore Absorption
FG Treatmentbefore Absorption
FG Treatmentbefore Absorption
At the pooling centre levelNext to the stackAmine pipelines
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D.1.1.2b Flue gas collecting Network –
Results
Amine transport makes sense as it allows decreasing the dimensions of the pipeline network and the power consumption
Limitation: Space for the absorber
Case #1
From
5 80”-diameter pipelines in parallel and 45MWe (LP) or 1 80”-diameter pipeline and 330MWe (HP)
To
2 pipelines in parallel of 32”
to 60”
diameter and a power consumption of 23MWe
Case #2
From
4 72”-diameter pipelines in parallel and 16MWe (LP) or 1 80”-diameter pipeline and 212MWe (HP)
To
2 pipelines in parallel of 22”
to 32”
diameter and a power consumption 4.5MWe
Other cases
Redesigns of some sections lead to 2 to 3 lines in parallel to cope with the velocity limit. There may be some space-related issues.
Might be interesting to delocalise the absorption units and use an amine network.
These results will be checked from a risk and economic standpoint
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D.1.1.3 Design and report on CO2
collecting network
Links the pooling centres where CO2
is captured to a common hub (13 MTCO2
/y must be collected before their export to Rotterdam)
The hub location depends on the option of transport chosen for the export system (pipeline or ship)
Assessment of different options for transporting the CO2 up to those hubs
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D.1.1.3 Banned areas for pipeline routing
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Objective: store CO2 at the ship hub level at (-50°C, 6.5 bar)
Case #1: Gaseous CO2
Transport (single liquefaction unit)
Case #1a) Low Pressure Transport
Case #1b) High Pressure Transport
Case #2: Liquid CO2
Transport (multiple liquefaction units)
D.1.1.3 Transport up to the «
ship
hub »
-
Options compared
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D.1.1.3 Transport up to the «
ship
hub »
-
Results
Energy Steel Insulation
Number of main
equipment pieces
Space @
pooling centre
Space @ hub
Total space Risk Costs
Liquefaction @ hub
Low pressure transport
- - 0 ++ / / /
WP3 WP4High pressure transport
+ + 0 + + - -
Liquefaction @ pooling centre ++ ++ - - - + +
++ Best solution+ Intermediate solution– Least interesting solution0 Not applicable/ Not assessed
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Objective: send CO2 to an onshore pipeline (150 bar)
Case #1: Dense CO2
Transport
Case #2: Gaseous CO2
Transport
D.1.1.3 Transport up to the «
pipeline hub »
-
Options compared
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D.1.1.3 Transport up to the «
pipeline hub »
-
Results
Energy Steel
Number of main
equipment pieces
Space @ the
pooling centre level
Space @ the hub
level
Total space
Risk Costs
Dense transport + + - - + +
WP3 WP4Gas transport - - + + - -
+ Best solution– Least interesting solution
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0
2
4
6
8
10
12
14
2020 2027
MTC
O2/y
Coal power plant AUP-1 Part of R1-17 Part of IGP Rest of Pooling #3 Rest of Pooling #2 Rest of Pooling #5 Pooling #4
4.3
13.1
Preliminary
deployment
strategy Input for D.1.1.5 –
D.1.1.6
A two-step deployment
strategy
2020: capture on the coal
power plant and on the easy
to capture CO2 (4.3MT/y)
2027: capture on other
sources (13.1MT/y)
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D.1.1.5 Export of CO2
from
Le Havre to Rotterdam by pipeline
Send
the CO2
by onshore/offshore pipeline from
Le Havre to Rotterdam
Pipeline routing
Pipeline design
For both
onshore
and offshore1.
Design a pipeline for 13.1MT/y from
20202.
Design a pipeline for 4.3MT/y from
2020 then
a pipeline of 8.8 MT/y from
2027
For onshore
option1.
Third
party access
at
the level
of Antwerp
(captured
CO2
from Antwerp: 10 MT/y)
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D.1.1.5 Pipeline routing
Assumptions for both onshore and offshore options
following existing pipeline routes,
avoid natural reserves,
minimize length
Specific assumptions for onshore routing
avoid densely populated areas,
avoid geographic depressions,
minimize height difference…
Specific assumptions for offshore routing
avoid shipping lanes,
avoid shipwrecks,
maintain constant depth for pipelines…
Data were gathered for France, Belgium, the Netherlands and the English Channel and the North Sea.
Resulting routes are suggested corridors and are by no means final routings considering the state of the study.
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D.1.1.5 Pipeline routing
-
onshore
/offshore variants
Onshore route: 616kmOffshore route: 505km
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D.1.1.5 Pipeline design
Assumptions
Onshore:
Pinlet=150bar;
Some pumping stations can be present along the way
Offshore:
Pinlet=200bar;
No pumping station along the way (prohibitive costs)
For both onshore and offshore:
Transport in dense phase (>80bar)
Design for the peak flowrate
Power requirements assessment considering the flowrate variation over a year.
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D.1.1.5 Onshore
pipeline design , Options to be
compared
Case D (") Number of pumping stations
Building from 2020 a pipeline able to transport
13.1MtCO2 /y
34 1
32 1
30 2
28 2
24 5
Building from 2020 a pipeline able to transport
4.3MtCO2/y
24 1
20 3
18 4
16 7
Building from 2027 a pipeline able to transport
8.8MtCO2/y
28 1
24 2
20 4
18 7
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D.1.1.5 Preliminary
risk
identification
Experience in the field of CO2
transport by onshore pipeline
Risks of failure mainly related to equipment failures and corrosion (considering US statistics on their CO2 network)
Experience is limited to areas with very sparse population (outside force is less an issue than in the natural gas transport field)
Considering offshore CO2
transport by pipeline, a single pipeline exists (Snøhvit) and no failure was reported so far (Pipeline began operation in 2009). But offshore pipelines could be affected by fishing equipment or ship collision. An option to decrease the risk is to cover the pipeline with rocks.
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Send
the CO2 by ships
from
Le Havre to Rotterdam
Boundary: send
the CO2
coming
from
the ship
to an offshore pipeline (200 bar) continuously
Objective: Define
shipping schedules
D.1.1.6 Export of CO2
from
Le Havre to Rotterdam by ship
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Main assumptions for the design of the shipping schedule:
Ship capacity, velocity, routing;
Unloading / loading / approach / mooring procedure;
Buffer Storage capacity;
CO2
capture profile and continuous injection in an offshore pipeline.
Information from literatureFirst identification of risks:
Collision / allision,
Grounding,
Internal event on board ship
Loading / unloading
D.1.1.6 Export of CO2
from Le Havre to Rotterdam by ship
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D.1.1.6 Results
of shipping schedule
Example
for 13.1MT/y –
peak
flowrate
10,000 m3
10,000 m3
5,000 m3
10,000 m3
10,000 m3
10,000 m3
10,000 m3
5,000 m3
Le Havre, 16 hours
Rotterdam, 12 hours
15h 45mn
15h 45mn10,000 m3
10,000 m3
CO2 from the liquefaction
unit
CO2 to the offshore pipeline
Tank being filled / being emptied / emptied
Tank filled30,555 m3 ship
10,000 m3
10,000 m3
Cycle Amount of time (hr)
Corresponding volume of
captured CO2 in Le Havre (tCO2)
Corresponding volume of
captured CO2 in Le Havre
(m3)
Mooring in Le Havre 3 5,291 4,585 Loading 10 17,638 15,284 Departure from le Havre 3 5,291 4,585 Journey Le Havre - Rotterdam 15.76 27,793 24,084 Mooring in Rotterdam 2 3,528 3,057 Unloading 8 14,110 12,227 Departure from Rotterdam 2 3,528 3,057 Journey Rotterdam - Le Havre 15.76 27,793 24,084 Total over a cycle 59.52 104,973 90,964
Hypothesis
30,555m3 ship, (-50.3°C, 6.5bar),
16.5 knots, 260 nautical miles,
Unload in port continuouslyEstimation of
temporary storage,
number of ships,
fuel consumption.
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Conclusion
The results obtained throughout WP1
is the bases for the other WPs
in COCATE
The second part of WP1, the strategy of deployment, will serve as a summary and recommendation for the project. It will recapitulate the results presented here as well as those from the other WPs.
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THANKS FOR YOUR ATTENTION
http://projet.ifpen.fr/Projet/cocate
Contact: Maud [email protected]