1 Phase change solvents; can they deliver? · 2014. 11. 17. · DTU TUHH ARMINES PROCEDÉ CSIRO THU...

1

Technoport, April 16 2012

iCapInnovative CO2 Capture, EU 7th FP , Cr. No 241391

Hallvard F. SvendsenDepartment of Chemical Engineering, NTNU

Phase change solvents;can they deliver?

2


Contents

• Objectives• Outline of work programme• Consortium • Phase change solvents

3


Objectives• Reducing the current energy penalty in power plant

efficiency to 4-5% points by introducing a new breed of solvents based on phase change.

• Combined SO2 and CO2 removal, thereby introducing process intensification, reducing capital cost, and energy requirement

• Make low temperature membranes feasible for post-combustion processes, thereby creating a solvent free alternative

• Develop new power cycles that can enable high pressure/high temperature post combustion membrane CO2 capture

4


iCap Project OverviewWork programme organization

5


ConsortiumRTD providers CSLF partners End-Users

NTNU TNO

SINTEFIFP DTU

TUHH ARMINES PROCEDÉ

CSIRO THU

DONG VTF ABVTF AS

VTF R&DEnBW

Project Overview

6


• 15 partners• 8 nationalities • Total Budget 6.3 M€• EC Funding 4.3 M€• Duration 48 Months• Starting Date 01.01.10

iCap Project Overview

7


Phase change solvents

iCap advancements beyond the State of the Art

Systems forming two liquid phases, one lean in CO2 and one rich in CO2 phase, resulting in lower recycle and higher CO2/H2O ratios. This lowers heat duty and creates a possibility for pressurised desorption in smaller and less costly desorbers, and with decreased recompression cost.

8


CO2 capture by liquid/liquid formation

Amine reclaimer

Reclaimer bottoms

Separator

9


Example pictures from one experiment

Before experiment During Experiment After separation

Screening tests

10


Screening tests

11


Equilibrium data converted to loading per mol amine Group, using total alkalinity and LC-MS

Vapour-Liquid-Liquid Equilibrium

12


Vapour-Liquid-Liquid EquilibriumCO2-rich phase vapour pressure as function of temperature

13


Heat of absorption

○ 6 m K+ + 1.2 m Pz; ● 5 m K+ + 3.5 m Pz

0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 110

20

30

40

50

60

70

/molCO2molAm-1

- H

abs/k

Jm

olCO

2-1

precipitation region

Precipitating system

14


Heat of absorption

5M DEEA and 2M MAPA

0

10

20

30

40

50

60

70

80

90

100

0 0,2 0,4 0,6 0,8 1 1,2 1,4 1,6 1,8

ΔHab

s(k

J/ m

ol C

O2)

Loading (mol CO2/ mol amine)

T = 40oC

5M DEEA - 22M MAPA - 25M DEEA + 2M MAPA - 130% MEA (~ 5M)

15


Kinetics, mass transfer rates

0

1

2

3

4

5

6

7

20 25 30 35 40 45 50 55 60 65

T (ºC)

CO

2 Abs

orpt

ion

Rat

e * 1

05 (mol

/s)

MAPA 1M MAPA 2M MAPA 3M MAPA 4M MAPA 5M MEA 5M (30%)DEEA 1 M DEEA 2M DEEA 4M DEEA 5M D5M2

Mass transfer rates in MAPA and DEEA solutions

16


Thermodynamic modeling

Source: http://www.itm.uni-stuttgart.de/research/pso_opt/pso_en.php

Rigorous activity based models are complex and many parameters must be fitted.

17


pKa-values and binaryequlibrium for DEEA

pKa values DEEA

Parity plot vapour pressuresActivity coefficients from binary data

18


Example results, pressures and speciation

5M DEEA 2M DEEA

2M DEEA

19


Implementation of models into CO2SIM

CO2SIM flow sheet of regenerator part

20


Heat exchanger

dP

Rev 1: 07 - 04 - 2011iCAP: Flow diagram LabPilot

FAN

P5

Abso

rber

Col

umn

P

Heater

Des

orbe

r Col

umn

DES

Sum

p

Insp

ectio

n gl

ass

BPV

Lean 2 Sampling

RichSampling

Tgas

Tlq

Tlq

Heat

er

Reboiler

VB

CoolerCooler

FMg

ABS

Sum

p

Wat

er W

ash

Col

umn

W W

Sum

p

P4

VB

VBVB

MFCCO 2

VRed

ReA

BS C

olum

n

Heavy phase

P1

dP

P2

dP

LIC

FMLFMRLIC

T

W W Tank

P

FVg

0

FV lq

0

FIC

LIC

P

TgP

Lean 1 Sampling

Feed tankR

eABS

Su

mp

FIC

FM lq

P3

VRed

FV lq

VB

VB

Ove

rflow

hea

vy p

hase

Ove

rflow

ligh

t pha

se

Disc stack centrifuge

VB

VB

MF3

VBVB MF2

VBVB

MF1

VBVB

Light phaseSampling

Flow diagram Lab Pilot

21


Pressure Temperature Duty lean loading Flow rate mol fraction Flow rate Specific Heat[kPa] [K] [kJ/s] CO2 H2O amine [mol CO2/mol amine] [kmol/h] CO2 [kmol/h] [kJ/kg CO2]

329,96 4 0,1561 0,4633 0,3806 0,410 5,8211 0,9818 0,1789 1863,27 16,18 %337,80 5 0,1501 0,4665 0,3834 0,391 5,7789 0,9818 0,2211 1884,55 19,99 %345,15 6 0,1439 0,4698 0,3863 0,373 5,7364 0,9817 0,2636 1897,04 23,87 %357,46 8 0,1317 0,4764 0,3919 0,336 5,6544 0,9817 0,3456 1929,24 31,32 %367,13 10 0,1197 0,4829 0,3974 0,301 5,5751 0,9817 0,4249 1961,48 38,44 %374,87 12 0,1074 0,4895 0,4031 0,266 5,4971 0,9817 0,5029 1988,71 45,55 %381,11 14 0,095 0,4962 0,4088 0,232 5,4204 0,9818 0,5796 2012,92 52,51 %346,44 6 0,1535 0,4646 0,3819 0,402 5,8022 0,9787 0,1978 2535,86 17,86 %360,57 8 0,1411 0,4715 0,3874 0,364 5,7205 0,9908 0,2795 2363,59 25,56 %372,05 10 0,1287 0,4783 0,393 0,327 5,6382 0,9908 0,3618 2282,42 33,07 %381,34 12 0,1162 0,4851 0,3987 0,291 5,5576 0,9908 0,4424 2239,91 40,44 %388,96 14 0,1036 0,492 0,4044 0,256 5,4784 0,9909 0,5216 2216,21 47,64 %395,33 16 0,0907 0,499 0,4103 0,221 5,4002 0,9909 0,5998 2202,59 54,82 %400,80 18 0,0777 0,5061 0,4162 0,187 5,323 0,9909 0,677 2195,35 61,85 %405,70 20 0,0644 0,5133 0,4223 0,152 5,2468 0,9909 0,753 2193,08 68,83 %410,35 22 0,051 0,5206 0,4284 0,119 5,1719 0,9909 0,8281 2193,61 75,67 %415,11 24 0,0375 0,5279 0,4346 0,086 5,0989 0,9909 0,9011 2199,17 82,37 %348,88 6 0,1576 0,4625 0,3799 0,415 5,8325 0,9841 0,1675 2978,15 15,22 %365,50 8 0,1453 0,4693 0,3854 0,377 5,7499 0,9939 0,2501 2633,20 22,95 %375,61 10 0,1329 0,4761 0,391 0,340 5,6669 0,9939 0,3331 2471,34 30,53 %385,53 12 0,1203 0,483 0,3967 0,303 5,5853 0,9939 0,4147 2382,07 38,02 %393,72 14 0,1076 0,4899 0,4025 0,267 5,505 0,9939 0,495 2328,25 45,37 %400,64 16 0,0946 0,497 0,4084 0,232 5,4256 0,9939 0,5744 2293,05 52,66 %406,63 18 0,0814 0,5042 0,4144 0,196 5,3473 0,9939 0,6527 2270,21 59,86 %412,03 20 0,0681 0,5115 0,4204 0,162 5,27 0,9939 0,73 2255,35 66,89 %417,20 22 0,0545 0,5189 0,4266 0,128 5,1939 0,9939 0,8061 2246,68 73,89 %422,53 24 0,0409 0,5264 0,4327 0,095 5,1196 0,9939 0,8804 2244,08 80,68 %428,64 26 0,0274 0,5337 0,4389 0,062 5,0484 0,994 0,9516 2248,96 87,24 %

200

400

600

Coal ‐ PCO2 = 13 kPaReboiler (U06) Lean Stream (P112) Gas stream (P08)

% CO2

removedmol fraction

Preliminary flowsheeting results

22


Summary: Achievements o Specific solvent systems have the property of forming

two liquid phases, one low in CO2 the other very high in CO2

o Characterization data indicate that very high CO2 partial pressures can be obtained even at low regeneration temperatures

o Kinetic data show rapid absorptiono Calorimetric data indicate that one may operate in a

range with relatively low heats of reactiono Regeneration at elevated pressure achievable o Preliminary feasibility studies show potential for

regeneration heat requirements of about 1.9-2 GJ/ton CO2 with reboiler temperatures of 75-90oC

o Equivalent efficiency penalty loss at 5% points

23


Thank you

Date post:	07-Mar-2021
Category:	Documents
Upload:	others
View:	2 times
Download:	0 times

1 Phase change solvents; can they deliver? · 2014. 11. 17. · DTU TUHH ARMINES PROCEDÉ CSIRO THU...

Documents