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. 2021 Aug 11;11(8):611.
doi: 10.3390/membranes11080611.

Membrane Fouling Behavior of Forward Osmosis for Fruit Juice Concentration

Zihe Li  1   2 , Chongde Wu  1   2 , Jun Huang  1   2 , Rongqing Zhou  1   2   3 , Yao Jin  1   2
Affiliations

Membrane Fouling Behavior of Forward Osmosis for Fruit Juice Concentration

Zihe Li et al. Membranes (Basel). .

Abstract

Forward osmosis (FO) technology has a broad application prospect in the field of liquid food concentration because of the complete retention of flavor components and bioactive substances. Membrane fouling is the main obstacle affecting the FO performance and concentration efficiency. This work systematically investigated the membrane fouling behavior of the FO process for fruit juice concentration elucidated by the models of resistance-in-series, xDLVO theory and FTIR analysis. The results show that the AL-FS mode was more suitable for concentrating orange juice. Increasing the cross-flow rate and pretreatment of feed solutions can effectively improve the water flux and reduce the fouling resistance. The ATR-FTIR analysis revealed that the fouling layer of orange juice was mainly composed of proteins and polysaccharides, and the pretreatment of microfiltration can greatly reduce the content of the major foulant. There was an attractive interaction between the FO membrane and orange juice foulants; by eliminating those foulants, the microfiltration pretreatment then weakened such an attractive interaction and effectively prevented the fouling layer from growing, leading to a lower process resistance and, finally, resulting in a great improvement of concentration efficiency.

Keywords: forward osmosis; fruit juice concentration; membrane fouling; xDLVO.

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Conflict of interest statement

The authors declare no conflict of interest.

Figures

Figure 1
Figure 1
Schematic diagram of forward osmosis concentration experimental device.
Figure 2
Figure 2
Evolution of water flux (a), concentration factor (b) and instantaneous resistance (c) over time during FO process at different membrane orientations (FS = ROJ; cross-flow rate = 6.4 m·s−1; tR = 10 h).
Figure 3
Figure 3
Evolution of water flux (a), concentration factor (b) and instantaneous resistance (c) over time during FO process at different cross-flow rates (FS = ROJ; AL-FS mode; tR = 10 h).
Figure 4
Figure 4
Evolution of water flux (a), concentration factor (b) and instantaneous resistance (c) over time during FO process after different pretreatments (cross-flow rate = 6.4 m·s−1; AL-FS mode; tR = 24 h).
Figure 5
Figure 5
Comparison of process resistance of different (a) membrane orientations, (b) shear rates, (c) pretreatments and (d) running durations.
Figure 6
Figure 6
Evolutions of interaction energies between membrane and feed solutes over interfacial distance includes (a) FOSL–ROJ, (b) FOAL–ROJ, (c) FOAL–CeOJ and (d) FOAL–MFOJ.
Figure 7
Figure 7
Evolutions of interaction energies between feed solutes over interfacial distance includes (a) ROJ–ROJ, (b) CeOJ–CeOJ, (c) MFOJ–MFOJ and (d) TOT.
Figure 8
Figure 8
FTIR spectra of clean and fouled CTA membranes.
See this image and copyright information in PMC

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