Perovskite oxide based composite hollow fiber membrane for CO2 transport

Journal Pre-proof Perovskite oxide based composite hollow fiber membrane for CO2 transport Shujuan Zhuang, Ning Han, Ruofei Chen, Zhengxin Yao, Qingchuan Zou, Feng Song PII:

S0272-8842(19)32588-X

DOI:

https://doi.org/10.1016/j.ceramint.2019.09.059

Reference:

CERI 22826

To appear in:

Ceramics International

Received Date: 9 July 2019 Revised Date:

20 August 2019

Accepted Date: 6 September 2019

Please cite this article as: S. Zhuang, N. Han, R. Chen, Z. Yao, Q. Zou, F. Song, Perovskite oxide based composite hollow fiber membrane for CO2 transport, Ceramics International (2019), doi: https:// doi.org/10.1016/j.ceramint.2019.09.059. This is a PDF file of an article that has undergone enhancements after acceptance, such as the addition of a cover page and metadata, and formatting for readability, but it is not yet the definitive version of record. This version will undergo additional copyediting, typesetting and review before it is published in its final form, but we are providing this version to give early visibility of the article. Please note that, during the production process, errors may be discovered which could affect the content, and all legal disclaimers that apply to the journal pertain. © 2019 Published by Elsevier Ltd.

1

Perovskite oxide based composite hollow fiber membrane for CO2

2

transport

3

Shujuan Zhuang,a,‡ Ning Han,b,* Ruofei Chen,b Zhengxin Yao,b Qingchuan Zou,c Feng Songa,**

4

a

5

China

6

b

7

University, Perth, WA 6845, Australia

8

c

9

‡ S. Zhuang and N. Han contributed equally.

Department of Chemical Engineering, Shandong University of Technology, Zibo 255049,

WA School of Mines: Minerals, Energy and Chemical Engineering (WASM-MECE), Curtin

School of Metallurgy, Northeastern University, Shenyang 110004, PR China

10

*Corresponding author.

11

[email protected] (N. Han)

12

[email protected] (F. Song)

13

Abstract

14

Membrane technologies have been widely investigated for CO2 separation, especially

15

inorganic membranes which could overcome the barrier of low melting point, and then been

16

applied for combustion activities. Compared with molecular sieving membranes (MSMs), the

17

mechanism during CO2 separation process on electrolyte membranes (EMs) is more complicated.

18

Mixed ionic and electronic conductors, such as perovskite oxides, has been proved with superior

19

activity than oxygen ion conductors because of the additional surface reaction path. To further

20

demonstrate the applicability of perovskite oxides contained membrane for CO2 separation, in

21

this work, CO2 transport via La0.6Sr0.4Co0.2Fe0.8O3-δ and carbonates composite membrane with

22

hollow fiber microstructure was thoroughly investigated under various gas flow directions. This

23

membrane presents the best permeability when CO2+N2 (feed gas) flows at shell side and He

24

(sweep gas) flows at tube side in parallel model. In addition, it also presents excellent thermal

25

shock resistance after six times rising and cooling operation with almost no performance

26

degradation.

27

Keywords: Thermal shock resistance, Ceramic composites, CO2 transport, perovskite

28

1. Introduction

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Fossil fuel combustion is the fundamental energy source supplying for modern industry and

30

daily use, which leads to CO2 emission causing global warming. Seriously, this structural system

31

would not be replaced for at least the next decades. However, it’s urgent to mitigate CO2

32

emission to solve the issue on the changing of climate. Considering the ever-increasing energy

33

demand, the best strategy for reducing CO2 release is to develop novel clean energy technologies.

34

Thus, advances in CO2 capture and storage (CCS) technology for the treatment of emitted flue-

35

gas from traditional power plants are necessary. The major three promising schemes, including

36

oxyfuel, pre-combustion, and post-combustion, have already been widely developed for CO2

37

capture from fossil fuel combustion [1-6].

38

CCS schemes usually involve gas separation process such as air separation for oxyfuel and

39

integrated gasification combined cycle (IGCC), CO2/N2 separation for post-combustion and

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CO2/H2 separation for IGCC [5-9]. Noteworthy that these separation projects are usually

41

operating at high temperatures ranges over 400 oC, while conventional chemical absorption

42

method with the monoethanolamine solvent requires the flue gas to be cooled down before

43

separating. From the perspective of application, CO2 capture plants under high temperature are

44

much more practical and able to lower the separation cost. In this case, membrane separation

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would be a promising direction to achieve CCS under high temperature and even combine with

46

further utilization as an energy conservation and environmental protection method [10-13].

47

Unfortunately, up to now, the CO2 separation via membrane technology still mainly relies on

48

organic membranes that own a low melting point. To overcome this barrier, inorganic

49

membranes for instance electrolyte membranes (EMs) and molecular sieving membranes (MSMs)

50

have been developed especially for combustion activities in view of their high temperature

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tolerance. For MSMs (e.g. zeolites), the gas separation involving surface adsorption and size

52

exclusion is merely a physical process based on the preferred size of molecular sieve [14].

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Whereas for EMs (e.g. perovskite oxides based), the separation mechanism is relatively

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complicated, which includes surface reaction (adsorption/desorption and disassociation) and bulk

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diffusion process of atoms or ions [15-17]. Thus, surface disassociation process, transferring

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reaction from molecular to corresponding ions or the opposite, as well as bulk diffusion process

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all may be the rate-determining steps during separation [16].

58

Recently, Lin et al. has developed carbonate-EM composite membrane for CO2 separation

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at high temperature [2, 10, 13, 18]. CO2 was firstly changed into CO32- via the surface reactions

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(2CO2 + O2-↔ 2CO32-). During bulk diffusion process, the solid oxide electrolyte phase mainly

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oxygen ion conductor, like samaria doped ceria (SDC) [13], gadolinia doped ceria (GDC) [17,

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19], and yttria doped zirconia (YSZ) [18], is controlling the transportation of O2-, while

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carbonates can give rise to the diffusion of CO32-. In addition, we have reported that mixed

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oxygen ionic and electronic conductor (MIEC), such as perovskite oxide [20-21], would

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facilitate the CO2 transportation because of the extra electrical conductivity which

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simultaneously brings about another possible surface reaction path: 2CO2 + O2 + 4e ↔ 2CO32-

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[22]. Considering the potential for practical application, the high selectivity, good permeability,

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strong mechanical strength and other physical parameters of perovskite oxide should be further

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investigated.

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Based on the nature excellent joint-conductivities on ionic and electronic of perovskite oxide

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and great mechanical properties of hollow fiber structure [23-44], La0.6Sr0.4Co0.2Fe0.8O3-δ (LSCF)

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based carbonate composite membrane with hollow fiber morphology was developed. CO2

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transport via this membrane was detailly investigated from various gas flow directions.

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Moreover, thermal shock resistance, one of the most important factors, was also studied in this

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work.

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2. Experimental section

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2.1 Material preparation

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Powders of perovskite LSCF was synthesized through sol-gel route following with

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calcination at 800 oC for 4 hr [38]. The LSCF hollow fiber membrane as supporter was then

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prepared with the calcined LSCF powders mixed with organic solvents via phase inversion-

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sintering process (1300 oC, 4 hr) [38]. Detail of spinning process was given in supporting

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information. Ternary carbonate composite (LiCO3/ Na2CO3/ K2CO3) was mixed by eutectic

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mixing process [22]. The LSCF hollow fiber membranes were put into carbonate mixture at

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molten state for 15 min, and then taken out, treated with sandpaper to remove the excess

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carbonates. Thus, the carbonated dual-phase LSCF hollow fiber membrane was obtained.

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2.2. Carbon dioxide permeability test

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Schematic 1. Home-made test model for CO2 separation.

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The CO2 permeation performance of this composite membrane was measured by gas

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chromatography [22, 38]. The schematic diagram of home-made test model was given in

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Schematic 1. CO2 permeation fluxes were carried out by helium (He) gas with flow rate between

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30 and 120 mL min-1 from 650 to 800 oC. CO2 permeation fluxes were calculated as below:

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CO

CO

=

CO

=

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CO

95

CO

=2

96 97

=

Where

He

He

(1)

(2)

CO

(3)

ln

(4)

is the concentration of CO2 detected by the chromatographic detector,

is the

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N2 content in the exhaust gas, it was detected as an indication of the physical gas leakage , it can

99

be used to correct the exact flux of CO2,

is the volume of the exhaust gas, and

is the

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volume of CO2 in the purge gas tail including permeation and physical leakage, S represents the

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membrane surface area (cm2), R represents the outer radius of membrane (cm), r represents the

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inner radius (cm).

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2.3. Characterization

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The phase composition of the LSCF powders and membranes was analyzed using X-ray

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diffraction (XRD) with a Cu-Kα radiation. The morphology and microstructures of LSCF

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supporter and LSCF based carbonate composite membranes were observed by scanning electron

107

microscope (SEM).

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3. Results and discussion

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3.1 Membrane morphology

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SEM images of the fresh LSCF hollow fiber membrane are presented in Figure 1. It

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displays an asymmetrical microstructure with longer finger pores near external surface and

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smaller capillary pores near internal surface, as shown in Figure 1A&B. The microstructure

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formation is mainly determined by the exchange rate of solvent-nonsolvent during phase

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separation process when coagulant meets polymer solution. In this work, since EtOH-NMP was

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chosen as the internal coagulant, the exchange rate of nonsolvent-solvent might be retarded at the

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internal side, resulting in the generation of longer finger-like pores near the internal surface

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(Figure 1B) [45]. Meanwhile, plenty of microchannels may be observed round external circle

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ascribed to the back flow of the solvent (Figure 1C). Noteworthy that numerous pores could be

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observed on the inner surface with diameter of 20 µm (Figure 1D), which extends to the fiber

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body (Figure 1B) and may give rise to the enhancement of CO2 permeability.

121 122

Figure 1. SEM graphs of fresh LSCF hollow fiber. (A) Cross section; (B) Wall; (C) External surface; (D) Internal

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surface.

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The LSCF based composite membrane was prepared through high temperature dip-coating

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process in molten carbonates for 15 min. The SEM images of this composite membrane are

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displayed in Figure 2. Carbonates could successfully bond with the support (LSCF), and even

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diffuse into the membrane bulk (Figure 2B) via the capillary force. As the pores from the inner

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surface to the outer surface film become larger and larger, the carbonates are gradually reduced,

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so that a dense carbonate-filled layer is formed only near the outermost surface. This composite

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membrane shows significantly enhanced bending strength from ~20 M pa of fresh LSCF up to

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over 60 M pa. Details of measuring method of bending strength are described in supporting

132

information. From external and internal surface image shown in Figure 2C & D, the

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heterogeneous particles (needle-like, block-like) are widely dispersed on the membrane surface.

134 135

Figure 2. SEM graphs of LSCF-carbonate hollow fiber. (A) Cross-section; (B) Wall; (C) External surface; (D)

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Internal surface.

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3.2 Phase structure

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SEM-EDX was introduced here to help detect the element distribution especially carbonates

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(K and Na). The EDX line scan from cross section of this membrane was displayed in Figure 3a.

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Potassium and sodium were successfully melted into the micropores of LSCF membrane. Details

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of the EDX line scan was given in Figure S1. Moreover, SEM elemental mapping was also

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given here, and the resultants were shown in Figure 3B & S2. The elemental composition of La,

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Sr, Co and Fe agrees well with its formula (Table S1). Lithium could not be detected by SEM-

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EDX, thus, the existence of element lithium was also determined via ICP with ratio round 1: 2: 2

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of Li: Na: K. Powder XRD patterns of this composite membrane are also given in Figure 3C.

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The characteristic peaks of (101), (110), (111), (200), and (211) of LSCF agree well with the

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stick patterns of cubic phase with space-group of Pm3m (JCPDS: 75-0279) (Figure 3C). The

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characteristic peaks of carbonates marked as “ • ” are clearly observed for the composite

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membrane. Dip-coating brings little impact on the phase structure of perovskite LSCF.

150 151

Figure 3. SEM-EDX images (A & B) of LSCF hollow fiber after impregnation process, and powder XRD patterns

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(C) of LSCF hollow fiber before and after impregnation process.

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3.3 Effect of gas flow direction on CO2 transport

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The effect of gas flow direction on CO2 permeation performance was shown in Figure 4A.

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There are four cases (Figure 4B): a. Sweep gas at shell side and feed gas at tube side of hollow

156

fiber, adverse current (shell side adverse current); b. Sweep gas at shell side and feed gas at tube

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side of hollow fiber, parallel current (shell side parallel current); c. Sweep gas at tube side and

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feed gas at shell side of hollow fiber, adverse current (tube side parallel current); d. Sweep gas at

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tube side and feed gas at shell side of hollow fiber, parallel current (tube side parallel current).

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Overall, sweep gas at tube side gives rise to a superior CO2 permeation performance. This could

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be attributed to the difference in driving force as the external surface is denser than the internal

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surface but offers more effective surfaces (1.8 times). Since the gas flow rate in the tube is larger

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than the outside of the tube, when the CO2 reaches the tube side, the sweep gas can quickly carry

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away the CO2, so that the CO2 concentration inside and outside the tube becomes larger, which is

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favorable for diffusion. Excessive Carbonates at external surface would facilitate the CO2

166

separation process.

167 168

Figure 4(A) Effect of gas flow direction on CO2 transport rate; (B) Schematic diagram.

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As LSCF is a kind of mixed oxygen ionic and electronic conductor, the existence of lattice

170

O2- gives rise to the formation of CO32- through 2CO2 + O2-↔ 2CO32-. The mechanism on CO2

171

transport through this LSCF-carbonate membrane involves the surface reaction process

172

(generation of CO32-) and bulk diffusion process (CO32-). With the existence of surface

173

carbonates, the generated CO32- would be easily to incorporate into coating layer, especially shell

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side with larger surface area compared to that of tube side. Thus, feed gas flowing through shell

175

side would be easier for the surface reaction at beginning to form CO32-, which could help to

176

understand the phenomenon that sweep at tube side leads to a better CO2 permeation

177

performance.

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3.4 Thermal shock resistance test and durability test

179 180

Figure 5. Thermal shock resistance test, effect of temperature cycling on membrane CO2 permeability. (Feed gas,

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N2+CO2=100 mL min-1; sweep gas, He=100 mL min-1)

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During practical application process, the separation reaction may be shut down for machine

183

correction. Even for ceramic material with high heat resistance, the poor resistance to thermal

184

shock would be the biggest obstacle. Thus, this LSCF composite membrane was further

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evaluated through the thermal cycle test from 600 to 850 oC, and the resultants are displayed in

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Figure 5. Before data collection, each test temperature point was balanced for at least 1 hr. This

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composite membrane presents good thermal shock resistance with stable CO2 permeation

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performance.

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Figure 6. SEM of a spent LSCF composite hollow fiber membrane (A) external surface; (B) internal surface.

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SEM images of this composite membrane after thermal shock resistance experiment are

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given in Figure 6. It can be seen from the electron micrograph that both the inner and outer

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surfaces of the membrane are still covered with a large amount of carbonate, but the morphology

194

of the carbonate has changed, which is caused by the redistribution of carbonate at high

195

temperature. This also shows that the structure of the two-phase film does not change much after

196

the thermal shock resistance test.

197

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Figure 7. Durability experiment (a); and elemental mapping of the corresponding membrane (b). Condition:

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sweep gas rate= 100 mL/min; feed gas rate= 100 mL/min; operating temperature= 700 oC.

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Figure 7 displays the durability experiment of this composite membrane and elemental

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mapping before and after long-time test. From Figure 7A, CO2 fluxes of this composite

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membrane keeps stable round 0.3 mL min-1 cm-2 at 700 oC for 55 hr. Then the CO2 permeation

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flux decreased greatly. Moreover, elemental mapping further detected the distribution of

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carbonates (Figure 7B), as shown in the figure, after a long period of stability test, the

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distribution of carbonate on the cross section was significantly reduced, because the carbonate

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was in a molten state at high temperature with good fluidity, and easily taken away by the purge

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gas. Therefore, a long purge will significantly reduce the carbonate, resulting in a decrease in

208

transmittance.

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3.5 Comparison of CO2 permeability with other ceramic membranes

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Figure 8. Comparison of CO2 permeability. Black-line: LSCF composite hollow fiber; Red-line: YSZ-

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supported composite hollow fiber membrane; Blue-line: LSCF composite disk membrane. Condition: sweep

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gas rate= 100 mL/min; feed gas rate= 100 mL/min.

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The CO2 permeation fluxes of this membrane were further compared with those of disk

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(LSCF) membrane from morphology aspect and oxygen ionic conductive hollow fiber composite

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membrane (Y0.08Zr0.92O2−δ (YSZ)) from material aspect (Figure 8). Obviously, temperature

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display positive relationship with CO2 permeability for all these membranes. For example, the

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CO2 fluxes of disk LSCF and YSZ-supported hollow fiber membranes increase from 0.022 to

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0.222, and 0.030 to 0.230 mL min-1 cm-2, while LSCF based carbonate composite hollow fiber

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membrane increases from 0.082 to 0.876 mL min-1 cm-2 with the temperature varying from 550

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to 850 oC. It displayed superior CO2 permeability compared with that of LSCF disk membrane

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and YSZ-supported composite membrane with hollow fiber microstructure, indicating that the

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LSCF composite membrane with hollow fiber microstructure owns a good structure superiority

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and inherent advantages of mixed conductivity. Moreover, the excellent permeation performance

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on CO2 of this membrane was also compared with previous reported ceramic membranes, such

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as Bi1.5Y0.3Sm0.2O3−δ [46], Y0.16Zr0.84O2−δ [22], La0.6Sr0.4Co0.8Fe0.2O3-δ [47], Ce0.8Sm0.2O1.9 [48],

227

Ce0.85Sm0.15O2-Sm0.6Sr0.4Al0.3Fe0.7O3 [49], and La0.85Ce0.1Ga0.3Fe0.65Al0.05O3-δ [50], in Table S2.

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4. Conclusions

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La0.6Sr0.4Co0.2Fe0.8O3-δ-carbonate composite membrane with hollow fiber microstructure

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was prepared here. It displays excellent CO2 permeation performance up to 3.8 times compared

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to that of the parent disk membrane. Based on the inherent mixed ionic electronic conductivity, it

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also displays 3.0 times higher than that of oxygen ionic conductor (YSZ) composite membrane at

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same morphological structure. Furthermore, sweep gas at tube side gives rise to better CO2

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permeation performance for this hollow fiber composite membrane after detailed investigation.

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This composite membrane also exhibits good thermal shock resistance after three circles test

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from 600 to 850 oC with CO2 permeation flux keeps stable.

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Acknowledgement The authors acknowledged National Natural Science Foundation of China (21476131, 21376143) for the financial support.

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References

241

[1] M. Pérez-fortes, A.D. Bojarski, E. Velo, J.M. Nougués, L. Puigjaner, Conceptual model and

242

evaluation of generated power and emissions in an IGCC plant, Energy 34 (2009) 1721–1732.

243

[2] Z. Rui, J. Y. Lin, Highly CO2 perm-selective metal-organic framework membranes through

244

CO2 annealing post-treatment, J. Membr. Sci. 555 (2018) 97-104.

245

[3] J. Xue, L. Chen, Y. Wei, H. Wang, CO2-stable Ce0.9Gd0.1O2−δ-perovskite dual phase oxygen

246

separation membranes and the application in partial oxidation of methane to syngas, Chem. Eng.

247

J. 327 (2017) 202-209.

248

[4] Y. Wei, W. Yang, J. Caro, H. Wang, Dense ceramic oxygen permeable membranes and

249

catalytic membrane reactors, Chem. Eng. J. 220 (2013) 185-203.

250

[5] N. MacDowell, N. Florin, A. Buchard, J. Hallett, A. Galindo, G. Jackson, C.S. Adjiman, C.K.

251

Williams, N. Shah, P. Fennell, An overview of CO2 capture technologies, Energy Environ. Sci. 3

252

(2010) 1645–1669.

253

[6] R. Kneer, D. Toporov, M. Förster, D. Christ, C. Broeckmann, E. Pfaff, M. Zwick, S. Engels,

254

M. Modigell, OXYCOAL-AC: towards an integrated coal-fired power plant process with ion

255

transport membrane-based oxygen supply, Energy Environ. Sci. 3 (2010) 198–207.

256

[7] Z. Wang, U. Oemar, M. Ang, S. Kawi, Oxidative steam reforming of biomass tar model

257

compound via catalytic BaBi0.05Co0.8Nb0.15O3-δ hollow fiber membrane reactor, J. Membr. Sci.

258

510 (2016) 417-425.

259

[8] Bouchra Belaissaoui, Yann Le Moullec, Hayato Hagi, Eric Favre, Energy efficiency of

260

oxygen enriched air production technologies: cryogeny vs membranes, Sep. Purif. Technol. 125

261

(2014) 142–150.

262

[9] Z. Wang, Y. Kathiraser, T. Soh, S. Kawi, Ultra-high oxygen permeable BaBiCoNb hollow

263

fiber membranes and their stability under pure CH4 atmosphere, J. Membr. Sci. 465 (2014) 151-

264

158.

265

[10] Z. Rui, M. Anderson, Y. Lin, Y. Li, Modeling and analysis of carbon dioxide permeation

266

through ceramic–carbonate dual phase membranes, J. Membr. Sci. 345 (2009) 110–118.

267

[11] S. Zhuang, N. Han, T. Wang, X. Meng, B. Meng, Y. Li, J. Sunarso, S. Liu, Enhanced CO

268

Selectivity for Reverse Water-Gas Shift Reaction Using Ti4O7-Doped SrCe0.9Y0.1O3-δ Hollow

269

Fiber Membrane Reactor, Can. J. Chem. Eng. 9999 (2018) 1-8.

270

[12] R. Baker, Membrane technology and applications, 2nd ed., Wiley, New York, 2004.

271

[13] Z. Rui, H. Ji, Y. Lin, Modeling and analysis of ceramic–carbonate dual phase membrane

272

reactor for carbon dioxide reforming with methane, Int. J. Hydrogen Energy 36 (2011) 8292–

273

8300.

274

[14] M. Nabavi, T. Mohammadi, M. Kazemimoghadam, Hydrothermal synthesis of hydroxy

275

sodalite zeolite membrane: Separation of H2/CH4, Ceram. Int. 40 (2014) 5885- 5896.

276

[15] N. Han, B. Meng, N. Yang, J. Sunarso, Z. Zhu, S. Liu, Enhancement of oxygen permeation

277

fluxes of La0.6Sr0.4CoO3−δ hollow fiber membrane via macrostructure modification and

278

(La0.5Sr0.5)2CoO4+δ decoration, Chem. Eng. Res. Des, 134 (2018) 487-496.

279

[16] J. Sunarso, S. Baumann, J. Serra, W. Meulenberg,S. Liu, Y. Lin, J. Diniz da Costa, Mixed

280

ionic–electronic conducting (MIEC) ceramic-based membranes for oxygen separation, J. Membr.

281

Sci. 320 (2008) 13–41.

282

[17] N. Han, Q. Wei, H. Tian, S. Zhang, Z. Zhu, J. Liu, S. Liu, Highly stable dual-phase

283

membrane based on Ce0.9Gd0.1O2-δ-La2NiO4+δ for oxygen permeation under pure CO2 atmosphere,

284

Energy Technol. 7 (2019) 1800701. doi:10.1002/ente.201800701

285

[18] B. Lu, Y. Lin, Synthesis and characterization of thin ceramic-carbonate dual-phase

286

membranes for carbon dioxide separation, J. Membr. Sci. 444 (2013) 402–411.

287

[19] J. Wade, C. Lee, A. West, K. Lackner, Composite electrolyte membranes for high

288

temperature CO2 separation, J. Membr. Sci. 369 (2011) 20–29.

289

[20] J. Ortiz-Landeros, T. Norton, Y. Lin, Effects of support pore structure on carbon dioxide

290

permeation of ceramic-carbonate dual-phase membranes, Chem. Eng. Sci. 104 (2013) 891-898.

291

[21] O. Ovalle-Encinia, H. Pfeiffer. J. Ortiz-Landeros, CO2 Separation Improvement Produced

292

on a Ceramic–Carbonate Dense Membrane Superficially Modified with Au–Pd, Ind. Eng. Chem.

293

Res. 57 (2018) 9261–9268

294

[22] S. Zhuang, N. Han, M. Xing, B. Meng, S. Liu, Perovskite oxide and carbonate composite

295

membrane for carbon dioxide transport, Mater. Lett. 236 (2019) 329–333.

296

[23] J. Song, B. Feng, Y. Chu, X. Tan, J. Gao, N. Han, S. Liu, One-step thermal processing to

297

prepare BaCo0.95-xBi0.05ZrxO3-δ membranes for oxygen separation, Ceram. Int. 45 (2019)

298

12579–12585.

299

[24] W. Wang, J. Qu, P. Juliao, Z. Shao, Recent advances in the development of anode materials

300

for solid oxide fuel cells utilizing liquid oxygenated hydrocarbon fuels: a mini review, Energy

301

Technol. 7 (2017) 33-44.

302

[25] D. Yang, N. Han, D. Han, B. Meng, G. Wang, S. Liu, Novel SrCo0.9W0.1O3-δ Hollow Fiber

303

Ceramic Membrane with Enhanced Oxygen Delivery Performance and CO2 Resistance Ability,

304

ChemistrySelect. 3 (2018) 13700-13704.

305

[26] T. Ma, N. Han, B. Meng, N. Yang, Z. Zhu, S. Liu, Enhancing Oxygen Permeation via the

306

Incorporation of Silver Inside Perovskite Oxide Membranes, Processes. 7 (2019) 199.

307

[27] S. Zhang, N. Han, X. Tan, Density functional theory calculations of atomic, electronic and

308

thermodynamic properties of cubic LaCoO3 and La1-xSrxCoO3 surfaces, RSC Adv. 5 (2015) 760-

309

769.

310

[28] Z. Wang, Y. Kathiraser, S. Kawi, High performance oxygen permeable membranes with

311

Nb-doped BaBi0.05Co0.95O3−δ perovskite oxides, J. Membr. Sci. 431 (2013) 180–186.

312

[29] N. Han, Z. Yao, H. Ye, C. Zhang, P. Liang, H. Sun, S. Wang, S. Liu, Efficient removal of

313

organic pollutants by ceramic hollow fibre supported composite catalyst, Sustain. Mater. Technol.

314

17 (2019) e00108.

315

[30] G. Jian, Y. Lun, N. Han, X. Tan, C. Fan, S. Liu, Influence of nitric oxide on the oxygen

316

permeation behavior of La0.6Sr0.4Co0.2Fe0.8O3−δ perovskite membranes, Sep. Purif. Technol. 210

317

(2019) 900-906.

318

[31] Q. Wei, S. Zhang, B. Meng, N. Han, Z. Zhu, S. Liu, Enhancing O2-permeability and CO2-

319

tolerance of La2NiO4+δ membrane via internal ionic-path, Mater. Lett. 230 (2018) 161–165.

320

[32] J. Song, B. Feng, X. Tan, N. Han, J. Sunarso, S. Liu, Oxygen selective perovskite hollow

321

fiber membrane bundles, J. Membr. Sci. 581 (2019) 393–400.

322

[33] N. Han, Q. Wei, S. Zhang, N. Yang, S. Liu, Rational design via tailoring Mo content in

323

La2Ni1-xMoxO4+δ to improve oxygen permeation properties in CO2 atmosphere, J. Alloy. Compd.

324

806 (2019) 153-162.

325

[34] Y. Wei, W. Yang, J. Caro, H. Wang, Dense ceramic oxygen permeable membranes and

326

catalytic membrane reactors, Chem. Eng. J. 220 (2013) 185-203.

327

[35] Z. Wang, Y. Kathiraser, T. Soh, S. Kawi, Ultra-high oxygen permeable BaBiCoNb hollow

328

fiber membranes and their stability under pure CH4 atmosphere, J. Membr. Sci. 465 (2014) 151-

329

158.

330

[36] Y. Chu, X. Tan, Z. Shen, P. Liu, N. Han, J. Kang, X. Duan, S. Wang, L. Liu, S. Liu, Efficient

331

removal of organic and bacterial pollutants by Ag-La0.8Ca0.2Fe0.94O3-δ perovskite via catalytic

332

peroxymonosulfate activation, J. Hazard. Mater. 356 (2018) 53-60.

333

[37] L. Liu, J. Gao, P. Liu, X. Duan, N. Han, F. Li, M. Sofianos, S. Wang, X. Tan, S. Liu, Novel

334

applications of perovskite oxide via catalytic peroxymonosulfate advanced oxidation in aqueous

335

systems for trace L-cysteine detection, J. Colloid. Interf. Sci. 545 (2019) 311-316.

336

[38] N. Han, S. Zhang, X. Meng, N. Yang, B. Meng, X. Tan, S. Liu, Effect of enhanced oxygen

337

reduction activity on oxygen permeation of La0.6Sr0.4Co0.2Fe0.8O3−δ membrane decorated by

338

K2NiF4-type oxide, J. Alloy. Compd. 654 (2016) 280-289.

339

[39] Z. Wang, N. Dewangan, S. Das, M. Wai, S. Kawi, High performance oxygen permeable

340

membranes with Nb-doped BaBi0.05Co0.95O3−δ perovskite oxides, J. Membr. Sci. 431 (2013) 180–

341

186.

342

[40] N. Han, C. Zhang, X. Tan, Z. Wang, S. Kawi, S. Liu, Re-evaluation of

343

La0.6Sr0.4Co0.2Fe0.8O3-δ hollow fiber membranes for oxygen separation after long-term storage of

344

five and ten years, J. Membr. Sci. 587 (2019) 117180.

345

[41] N. Han, S. Zhang, B. Meng, X. Tan, The effect of microstructure and surface decoration

346

with K2NiF4-type oxide upon the oxygen permeability of perovskite-type La0.7Sr0.3FeO3-δ hollow

347

fiber membranes, RSC Adv. 5 (2015) 88602–88611.

348

[42] L. Zhuang, J. Li, J. Xue, Z. Jiang, H. Wang, Evaluation of hydrogen separation performance

349

of Ni-BaCe0.85Fe0.15O3-δ cermet membranes, Ceram. Int. 45 (2019) 10120-10125.

350

[43] N. Han, R. Chen, T. Chang, L. Li, H. Wang, L. Zeng, A Novel Lanthanum Strontium Cobalt

351

Iron Composite Membrane Synthesised Through Beneficial Phase Reaction for Oxygen

352

Separation, Ceram. Int. 45 (2019) 18924-18930.

353

[44] N. Han, W. Wang, S. Zhang, J. Sunarso, Z. Zhu, S. Liu, A novel heterogeneous

354

La0.8Sr0.2CoO3−δ/(La0.5Sr0.5)2CoO4+δ dual-phase membrane for oxygen separation, Asia. Pac. J.

355

Chem. Eng. (2018) e2239.

356

[45] M. Zuo, S. Zhuang, X. Tan, B. Meng, N. Yang, S. Liu, Ionic conducting ceramic–carbonate

357

dual phase hollow fibre membranes for high temperature carbon dioxide separation, J. Membr.

358

Sci. 458 (2014) 58–65.

359

[46] Z. Rui, M. Anderson, Y. Li, J. Lin, Ionic conducting ceramic and carbonate dual phase

360

membranes for carbon dioxide separation, J. Membr. Sci. 417-418 (2012) 174-182.

361

[47] M. Anderson, Y. Lin, Carbonate–ceramic dual-phase membrane for carbon dioxide

362

separation, J. Membr. Sci. 357 (2010) 122-129.

363

[48] X. Dong, H. Wang, Z. Rui, Y. Lin, Tubular dual-layer MFI zeolite membrane reactor for

364

hydrogen production via the WGS reaction: Experimental and modeling studies, Chem. Eng. J.

365

268 (2015) 219-229.

366

[49] O. Ovalle-Encinia, H. Pfeiffer, J. Ortiz-Landeros, Ce0.85Sm0.15O2-Sm0.6Sr0.4Al0.3Fe0.7O3

367

composite for the preparation of dense ceramic-carbonate membranes for CO2 separation, J.

368

Membr. Sci. 547 (2018) 11-18.

369

[50] T. Norton, Y. Lin, Ceramic–carbonate dual-phase membrane with improved chemical

370

stability for carbon dioxide separation at high temperature, Solid State Ionics 263 (2014) 172-

371

179.