Startseite Preparation and performance of homogenous braids-reinforced poly (p-phenylene terephthamide) hollow fiber membranes
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Preparation and performance of homogenous braids-reinforced poly (p-phenylene terephthamide) hollow fiber membranes

  • Chun Wang EMAIL logo , Dinghe Yan , Shubin Song , Jingjing Yan , Haolong Xue und Changfa Xiao EMAIL logo
Veröffentlicht/Copyright: 21. August 2023
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e-Polymers
Aus der Zeitschrift e-Polymers Band 23 Heft 1

Abstract

A novel homogenous braid-reinforced (HBR) poly (p-phenylene terephthamide) (PPTA) hollow fiber membrane was prepared in this study. The effects of PPTA concentration on the morphologies and properties of the membranes were further investigated. The results showed that when the PPTA concentration was 2.0 wt%, the cross-sectional morphology of satisfactory interfacial bonding was achieved and the permeation was still maintained at about 200 (L·m−2·h−1) after ultrasonic vibration. In addition, the tensile force exceeded 600 N, which indicated that the homogeneous effect effectively improved the poor mechanical properties and interfacial bonding. In addition, the HBR PPTA hollow fiber membranes were applied to simulate the membrane bioreactor system to explore the control factors of membrane fouling. The results demonstrated that the average removal of total phosphorus and NH4 +–N was above 49% and 96%, respectively; meanwhile, the operating time was up to 120 days. Furthermore, it was easier to nearly remove the pollutants by chemical cleaning.

Nomenclature

BSA

bovine serum albumin

CHCl3

trichloromethane

HBR

homogenous braid-reinforced

MBR

membrane bioreactor

NF

nanofiltration

NH4 +–N

ammonia nitrogen

NMP

N-methyl-2-pyrrolidone

PEG

polyethylene glycol

PFAs

pore-forming agents

PPTA

poly (p-phenylene terephthamide)

PVP

polyvinylpyrrolidone

THF

tetrahydrofuran

TMP

transmembrane pressure difference

TP

total phosphorus

UF

ultrafiltration

1 Introduction

The membrane bioreactor (MBR) system is a new wastewater treatment technology combining traditional biotechnology and membrane separation technology, with a high solid–liquid separation rate, stable effluent quality, and high treatment efficiency, which has become the widely used technology for wastewater resource utilization and water environment treatment (1,2). However, MBR technology requires high performance of hollow fiber membranes, which not only requires membrane materials with excellent separation performance but also be able to withstand the effects of high-intensity water impact and aeration disturbance during MBR operation, which was difficult to be applied for traditional homogenous hollow fiber membranes (3,4).

The preparation methods of reinforced hollow fiber membranes are divided into two types: polymeric-reinforced membrane and fibrous-reinforced membrane (5,6,7,8). In the former, the hollow fiber membrane prepared by the thermally induced phase separation method or melt spinning-cold stretching method was used as the base membrane, and the separation layer was combined with its surface to prepare a polymeric-reinforced hollow fiber membrane. In the latter, the fiber or the fiber bundle was used as reinforcement, and the separation layer was combined with its surface to prepare a fibrous-reinforced hollow fiber membrane. In the process of fibrous-reinforced hollow fiber membrane preparation, it is important to solve the problem of interfacial bonding between the reinforcement and the surface separation layer for the preparation of high-performance-reinforced hollow fiber membranes (9,10).

According to the relationship of interfacial bonding between the reinforcement and the surface separation layer, the reinforced hollow fiber membrane could be divided into homogeneous BR (HBR) hollow fiber membrane and heterogeneous BR (HTR) hollow fiber membrane. Homogeneous reinforcement indicated that the fibrous reinforcement and the surface separation layer were of the same material and they were no thermodynamic compatibility differences so that an ideal interface structure could be easily formed between the surface separation layer and the reinforcement. Thus, there was an increasing demand for fabricated HBR hollow fiber membranes that combined high separation accuracy (smaller average pore size and narrower distribution) with high strength (fiber reinforcement) and high throughput (high porosity) for widely harsh environment applications (11,12,13).

Currently, the tubular braids-reinforced (BR) hollow fiber ultrafiltration (UF) membrane has been the most widely used in the MBR system instead of traditional homogeneous hollow fiber membrane, and its preparation process is similar to the concentric circle composite method (14); the inner layer is tubular braids and the outer layer is the polymer separation layer and the interfacial layer between them. For this reason, many researchers at home and abroad have developed and applied HTR hollow fiber membranes. Especially, the HTR PVDF hollow fiber membranes are made of PET or PP tubular braids as reinforcement and have become the most used UF membrane for the MBR system because of their high permeance, easy scale production, and engineering applications (15,16,17).

However, most polymeric materials lacked stability, including the PVDF membrane under extreme conditions, such as high temperatures, processes coupled to acid and alkali solutions, or in the presence of organic solvents. Meanwhile, the inorganic membranes were very expensive and hard to manufacture though they were suitable to be used under such requirements (18). Therefore, there was an urgent demand to develop high-performance membrane materials.

Poly (p-phenylene terephthamide) (PPTA) is a kind of rigid linear chain aromatic polyamide, which has superior mechanical strength, is acid and alkali-resistant, and is thermal and solvent resistant (19,20,21). Nevertheless, there were few relevant researchers in this field of PPTA membranes. Zschocke and Strathman (22) have reported a solvent-resistant membrane from PPTA. Wang et al. (23,24,25) have published a series of high-performance PPTA UF/nanofiltration membranes. Therefore, based on previous research studies (26,27,28,29,30), in this study, the HBR PPTA hollow fiber membranes consisting of PPTA hollow tubular braids and a PPTA separation layer were fabricated by the concentric circle extrusion spinning method. The influence of the PPTA concentration on the structure and performance of HBR PPTA hollow fiber membranes was investigated in terms of membrane morphologies, mechanical properties, and permeation/rejection performance. Then, it was applied in the MBR system, which was a simulation of urban domestic sewage to observe and further investigate the results on membrane performances such as transmembrane pressure difference (TMP), total phosphorus (TP) concentration, and ammonia nitrogen (NH4 +–N), aimed to verify the anti-fouling properties of HBR PPTA hollow fiber membranes.

2 Materials and methods

2.1 Materials

PPTA resin (PPTA, fiber grade, η inh = 5.5−6.5 dL·g−1) and filament yarn (PPTA, single fiber denier = 244 dtex, modulus = 590.48 CN‧dtex−1) were purchased from Zhonghua High-performance Fiber Material Co., Ltd. Concentrated sulfuric acid (H2SO4, 98%, AR) was purchased from Shanghai Titan Chemical Reagent Technologies Co. Ltd. Silica (SiO2) particles with an average size of 30 nm were purchased from Beijing Boyu Gaoke Advanced Materials Technical Co. Ltd. Bovine serum albumin (BSA, M w = 68,000) was purchased from Beijing Solarbio Science and Technology Co. Ltd. Polyethylene glycol (PEG) and polyvinylpyrrolidone (PVP) were purchased from Tianjin Kemel Reagent Co. Ltd. N,N-Dimethylacetamide (AR), N,N-dimethylformamide (AR), trichloromethane (CHCl3, AR), tetrahydrofuran (THF, AR), and N-methyl-2-pyrrolidone (AR) were purchased from Tianjin Guangfu Fine Chemical Institute.

2.2 Membrane preparation

First, the PPTA tubular braids were prepared by the two-dimensional braided method. Then, they were coated with the PPTA casting solutions and guided through a coagulation bath, where the HBR PPTA hollow fiber membranes were formed. The casting solution was prepared with the mixtures of different compositions consisting of PPTA resin, pore-forming agents (PFAs, composed of PEG/PVP), SiO2, and H2SO4, and they were blended in a special weight homogeneously under high-speed agitation for 2–3 h at 80–90℃. After the formation of HBR PPTA hollow fiber membranes, they were stored in clean water to remove the residual solvents and PFAs.

The samples of HBR PPTA hollow fiber membranes with different PPTA resin concentrations are shown in Table 1 and the spinning parameters are shown in Table 2.

Table 1

Samples of HBR PPTA hollow fiber membranes

Sample PPTAp (%) H2SO4 (%) PFAs (%) SiO2 (%)
PPTA-1# 1.5 88 10 0.5
PPTA-2# 1.75 87.75 10 0.5
PPTA-3# 2.0 87.5 10 0.5
PPTA-4# 2.5 87 10 0.5
Table 2

Spinning parameters of HBR PPTA hollow fiber membranes

Spinning parameter
Spinning temperature (℃) 80.0 ± 5.0
Coagulation bath Water
Coagulation temperature (℃) 30.0 ± 5.0
Air gap (cm) 5.0 ± 0.5
Take-up speed (m·h−1) 10.0 ± 1.0

2.3 Characterization

2.3.1 Scanning electron microscopy (SEM)

The surface and cross-section morphology of membranes were observed by field emission SEM (Nano-230, FEI, Netherlands). The membrane was freeze-dried before cryogenically fractured in liquid N2, and they were sputtered with gold.

2.3.2 Mechanical performances

Mechanical properties were measured using an electronic stretching machine (AG-250kNE, Japan) at room temperature. The tensile rate was 50 mm·min−1 and the gripping length was 50 mm. The OD/ID values were about 1.8 mm/1.6 mm. The average value of five tests was chosen.

2.3.3 Permeation and interfacial bonding

Membrane permeation was characterized by pure water flux and organic solution flux. The pressure difference across the membrane was 0.1 MPa. The permeance was determined by the following equation (1):

(1) J w 1 = V A × t

where J w1 is the permeation (L·m−2·h−1), V is the total quantity of the filtrate (L), A is the tested membrane area (m2), and t is the testing time (h).

2.3.4 BSA protein separation

All experiments were carried out at room temperature. Before the test, each membrane was initially compacted for 10 min at 0.15 MPa and then the feed solution and filtrate were recorded at 0.1 MPa every 10 min until 60 min. The original BSA protein solution (1 g·L−1) was prepared in 0.03 wt% NaOH solution (pH = 11). The rejection rate was calculated by the following equation (2):

(2) R = 1 C p C f × 100 %

where C p and C f are the filtrate and the feed solution density, respectively. The absorbances of feed solution and filtrate were determined by UV spectroscopy at 280 nm, using a Beijing Purkinje UV-1901 spectrophotometer.

2.3.5 Simulation of the MBR system

The HBR PPTA-3# hollow fiber membrane was tested in the MBR system, which was a simulation of urban domestic sewage. The volume of the biochemical reactor was 50 L, and the flux was controlled at a constant rate of 40 mL·min−1. The level of the reactor was controlled by a liquid level controller. The raw water was controlled by the inlet pump and the outlet water was controlled by the suction pump. The intermittent pumping mode of 9 min pumping and 1 min stop was used. The aeration rate was 3.6 L·min−1 with air compressor, the air/water ratio was about 50:1, and the effective area of the membrane module was 0.1 m2. The experimental period was 120 days. The sludge concentration was about 8,500 mg·L−1, dissolved oxygen was about 6.5–8.5 mg·L−1, the pH was about 6.5–7.5, and the water temperature was about 18–20℃.

The membrane surface was observed by SEM before and after pollution, the TMP before and after pollution was observed by a pressure flow meter, and changes in parameters including TP and NH4 +–N were tested by standard methods (33,34,35).

3 Results and discussion

3.1 Morphology of the membrane

The outer surface and cross-sectional morphologies of the HBR PPTA-3# hollow fiber membranes are shown in Figure 1a–d. As shown in Figure 1a, a dense and smooth coating layer was formed at the outer surface of the tubular braids, which resulted typically from the solution phase separation via the solvent and non-solvent mutual diffusion (36). This was beneficial to obtain good rejection properties. As shown in Figure 1b–d, compared with the HTR PPTA-3# hollow fiber membrane (PPTA-3# was the outer separation layer and PET tubular braids were fibrous reinforced), the cross-section of the HBR PPTA-3# hollow fiber membrane separation layer had a finger-like pore structure, and as both were homogeneous materials, the concentrated sulfuric acid would etch the surface of the PPTA braided tube reinforcement to enable the surface separation layer casting solution to penetrate the fiber spacing, which improved the bonding strength between the hollow braided tube and the surface separation layer (shown in Figures A1 and A2 in Appendix). Moreover, the forming process adopted the concentric circle extrusion spinning method, which could effectively regulate the uniformity of the surface separation layer and reduced the eccentricity of the surface separation layer.

Figure 1 
                  Outer surface and cross-sectional morphologies of the braids-reinforced PPTA hollow fiber membranes. (a) The outer surface of HBR PPTA-3#, (b) the cross-section of HBR PPTA-3#, (c) HBR PPTA-3# membrane, and (d) HTR PPTA-3# membrane (PET braids/PPTA).
Figure 1

Outer surface and cross-sectional morphologies of the braids-reinforced PPTA hollow fiber membranes. (a) The outer surface of HBR PPTA-3#, (b) the cross-section of HBR PPTA-3#, (c) HBR PPTA-3# membrane, and (d) HTR PPTA-3# membrane (PET braids/PPTA).

3.2 Interfacial bonding

Interfacial bonding is important for BR hollow fiber membranes because it would restrict the operation life of the membranes. Ultrasonic vibration analysis is a typical method to evaluate the interfacial bonding state. Thus, the effect of ultrasonic treatment on pure water flux of HBR PPTA hollow fiber membranes is shown in Figure 2. The results showed that HBR PPTA-3# and 4#, with nearly no change in their pure water fluxes, possessed a stable interfacial bonding state. There was relatively strong interfacial bonding between the separation layer and the tubular braids because of the infiltration of the casting solution. Besides, the part of fiber bundles that were in contact with the separation layer was swollen to a certain extent and adhered to each other (shown in Figure A2). It was obvious that the pure water flux of PPTA-1# and 2# had a relatively higher vibration due to the lower PPTA concentration, which indicated that the interfacial bonding was weaker so there was a significant breakage phenomenon between the two interfaces.

Figure 2 
                  The effect of ultrasonic treatment on the interfacial bonding of HBR PPTA hollow fiber membranes.
Figure 2

The effect of ultrasonic treatment on the interfacial bonding of HBR PPTA hollow fiber membranes.

3.3 Permeation properties

Figure 3 shows the pure water flux of the HBR PPTA hollow fiber membranes and the solvent flux of the HBR-3# PPTA hollow fiber membranes for five kinds of common organic solvents. As shown in Figure 3a, it is obvious that the pure water flux of the HBR PPTA hollow fiber membrane exhibits four very linear relationship because PPTA is a rigidly linear chain macromolecule, which could prevent the pore structure from deformation, and then the flux is stable under constant pressure conditions. This indicated that the swelling and adhering of the tubular braids increase the intrinsic resistance of the membranes. Therefore, there was a balanced state between the separation layer porosity and bonding strength, which only resulted in a little change in permeation. Figure 3b shows that the shrinking effect due to solvent interaction was considered to be insignificant. The HBR-3# PPTA hollow fiber membranes were proved to be stable in these organic solvents.

Figure 3 
                  The pure water flux of HBR PPTA hollow fiber membranes (a) and the solvent flux of the HBR PPTA-3# hollow fiber membranes (b).
Figure 3

The pure water flux of HBR PPTA hollow fiber membranes (a) and the solvent flux of the HBR PPTA-3# hollow fiber membranes (b).

3.4 BSA rejection

Figure 4 shows the BSA rejection of the prepared HBR PPTA hollow fiber membranes. According to Figure 4, with the increase of the PPTA concentration in casting solutions, it was obvious that all the rejection ratios could reach above 80% depending on the test time; especially, with the increase of PPTA concentration, the higher rejection was more quickly achieved (such as HBR PPTA-4#), which indicated the denser separation layer (that was higher transmembrane pressure) and stable membrane pore structure. Besides, the results also showed that the rejection rate was stable. On the one hand, the membrane surface was of dense layer and narrow pore distribution, which could effectively intercept the protein spherical molecules. On the other hand, the strong polar amide groups (–NH–CO–) in the PPTA macromolecular chain caused strong electronegativity in the membranes, which was due to protein absorption and concentration polarization on the membrane surfaces (37,38).

Figure 4 
                  The BSA rejection of HBR PPTA hollow fiber membranes.
Figure 4

The BSA rejection of HBR PPTA hollow fiber membranes.

3.5 Mechanical properties

Figure 5 shows the tensile stress–strain behavior of the HBR PPTA-3# hollow fiber membrane. Different from the homogeneous PPTA hollow fiber membrane, the tensile force of HBR PPTA hollow fiber membranes mainly depended on the tubular braids while it hardly depended on the PPTA concentration. As shown in Figure 5, the curve exhibited a kind of stepwise fracture, and the maximum number of tensile stress was 0.6 kN while the elongation at break was about 20%. The curves exhibited a very linear relationship; the tensile strength quickly dropped to zero when it reached the breaking point and the yield area did not appear. The slope of the linear curve gave Young’s modulus, and the failure point was the ultimate strength of the membrane along their axial direction. It was because the PPTA had a high crystalline macromolecule structure. When elongation at break occurred, the areas of lamellar crystal bedded slip (39).

Figure 5 
                  The mechanical properties of HBR PPTA-3# hollow fiber membranes.
Figure 5

The mechanical properties of HBR PPTA-3# hollow fiber membranes.

3.6 Simulate MBR separation

3.6.1 Surface elements

Figure 6 shows the surface morphology of the homogeneous HBR PPTA-3# hollow fiber membrane in the MBR system after activation of sludge pollution and citric acid backwashing. Table 3 shows the surface elemental analysis. As shown in Table 3, after a period of MBR operation, different contents of N, P, Ca, Mg, Al, K, and Na, and other elements appeared on the membrane surface. This was because the feed solution contains NaCl, MgSO4, MnSO4, (NH4)2SO4, KH2PO4, etc., Mg, Al, Ca, and other elements in the form of cations, which could easily form precipitates with OH, CO3 2−, PO4 3−, and other anions in the water. When operating for some time, a biofilm layer was formed on the membrane surface and these cations were present in the biopolymer, which could easily combine with metal ions to form a dense filter cake layer on the membrane surface. The elemental content of the membrane surface was significantly reduced after hydrodynamic backwashing, and the inorganic elements were removed after a shorter period of citric acid washing with a better cleaning effect, which was consistent with the results of the morphology diagram in Figure 6b, indicating that the resulting HBR PPTA hollow fiber membranes were easy to clean and had better anti-fouling performance.

Figure 6 
                     The outer surface morphologies of HBR PPTA-3# hollow fiber membranes (a) after sludge pollution; (b) citric acid backwashing.
Figure 6

The outer surface morphologies of HBR PPTA-3# hollow fiber membranes (a) after sludge pollution; (b) citric acid backwashing.

Table 3

Surface element content on the HBR PPTA-3# hollow fiber membrane surface

Element Original (%) Fouled 1 (%) Water (%) Fouled 2 (%) Chemical (%)
C 77.36 64.74 77.91 65.16 77.78
O 20.59 24.08 16.57 22.47 10.62
N 0 1.00 1.13 2.21 0.02
P 0 0.43 0.21 0.59 0.02
Ca 0.35 3.92 2.44 3.21 0.45
Mg 0 0.09 0.02 0.09 0
Al 0 0.12 0.23 0.33 0
Cl 0.90 4.17 1.08 4.59 0
K 0 0.45 0.01 0.68 0
Na 0 1.00 0.40 0.67 0

3.6.2 TMP

In this study, the HBR PPTA-3# hollow fiber membrane module was operated at a constant flux of 40 mL·min−1 for 120 days while monitoring the change of TMP. Figure 7 shows the TMP variation with the operation time of the HBR PPTA-3# hollow fiber membrane module. As shown in Figure 7, due to the strong hydrophilic separation layer of the HBR PPTA-3# hollow fiber membrane, the membrane was running for a longer period without cleaning. During the initial 56-day operation, the TMP showed a stable growing trend and the TMP difference gradually increased from 0.04 to 0.08 MPa with time. Meanwhile, the membrane surface pollution worsened. Subsequently, it was hydrodynamically backwashed, the TMP basically recovered to 0.04 MPa, and the membrane performance recovered well. This was because the woven pitch gap of tubular braids was larger and the internal pressure of backwash water through the pitch gap was lower, which could directly affect the surface separation layer and thus the cleaning effect was significant.

Figure 7 
                     Variation in the TMP with time.
Figure 7

Variation in the TMP with time.

After 30 days of stable operation, the TMP increased to 0.08 MPa. Then, the TMP only recovered to 0.07 MPa when the membrane was backwashed again and the TMP quickly reached 0.08 MPa after a week of operation, which greatly shortened the operation period. This was because most of the organic pollutants deposited on the membrane surface had been removed, while metal inorganic pollutants were still attached to the membrane surface and were difficult to be removed by hydraulic cleaning. Through citric acid cleaning, TMP could be restored to 0.046 MPa. After1 month, the TMP again increased to 0.08 MPa. The membrane module was cleaned by citric acid cleaning again and the TMP decreased to 0.07 MPa.

In 10 consecutive days, TMP was more stable. It could be inferred that the HBR PPTA-3# hollow fiber membranes exhibited the surface compression resistance and structural stability of membrane pores because of the excellent mechanical properties of PPTA molecules. The membrane surface is not easily compacted, and organic contaminants such as proteins only caused membrane pore blockage resistance, while inorganic contaminants caused filter cake layer resistance forming deposition contamination (24,40,41). Overall, the HBR PPTA hollow fiber membranes had longer operating times and longer cleaning cycles, which exhibited excellent anti-pollution performance.

3.6.3 TP

Figure 8 shows the removal rate of phosphorus concentration (TP) from the supernatant and the filtrate of the HBR PPTA-3# hollow fiber membrane module. As shown in Figure 8, during the initial operation period, the number of phosphorus-polymerizing bacteria was low and the TP removal rate was only about 10%. With the increase of the operation time, the TP removal rate gradually increased and the TP removal rate reached a maximum value at 40 days of operation. After active sludge removal and washing, the TP removal rate started to increase again and when the system was running stable, the TP removal rate fluctuated in a wide range. The TP removal rate of the supernatant ranged from 12% to 83%; meanwhile, the TP removal rate of the HBR PPTA-3# hollow fiber membrane module ranged from 13% to 85%. After the active sludge removal at 96 days, the TP removal rate gradually increased again. This was mainly due to the long sludge retention time, which led to an increase in the sludge concentration, a decrease in sludge activity, and a sludge accumulation zone at the bottom of the reactor, where the dissolved oxygen was insufficient and turned anaerobic. In the anaerobic zone, polyphosphate bacteria fully released polyphosphates in their bodies, leading to an increase in the TP content in the system. After increasing the aeration to eliminate the anaerobic zone, the TP removal rate increased. After hydrodynamic backwashing and chemical cleaning, the TP removal rate of the membrane module was slightly higher than that of the supernatant, and the cleaning effect of the HBR PPTA-3# hollow fiber membrane module could be obtained.

Figure 8 
                     The TP removal rate in the supernatant and HBR PPTA-3# hollow fiber membranes.
Figure 8

The TP removal rate in the supernatant and HBR PPTA-3# hollow fiber membranes.

3.6.4 NH4 +–N

Figure 9 shows the removal ratio of ammonia nitrogen (NH4 +–N) in the supernatant and filtrate of the HBR PPTA-3# hollow fiber membrane module. As shown in Figure 9, they were more stable and the removal effect was better. When the simulated MBR system was running stable, the average NH4 +–N removal rate of the supernatant was about 94%, and the average NH4 +–N removal rate of the HBR PPTA-3# hollow fiber membrane module was about 96%. When the system was running until 96 days, the NH4 +–N removal rate dropped to the minimum. Afterwards, the NH4 +–N removal rates increased rapidly after the active sludge elimination. This was attributed mainly to the decrease in bacterial activity under long operation times.

Figure 9 
                     The NH4
                        +–N removal rate in the supernatant and HBR PPTA-3# hollow fiber membranes.
Figure 9

The NH4 +–N removal rate in the supernatant and HBR PPTA-3# hollow fiber membranes.

Compared with the NH4 +–N removal rate after two hydraulic backwashes, the results showed that there was no significant decrease in the removal rate after the second cleaning. After chemical cleaning, the NH4 +–N removal rate decreased, which indicated that a better cleaning effect for the HBR PPTA-3# hollow fiber membrane was achieved at this time.

4 Conclusion

The HBR PPTA hollow fiber membranes were fabricated by the concentric circle extrusion spinning method, which consisted of a PPTA separation layer and PPTA hollow tubular braids. With the increase of the PPTA concentration in the casting solution, the separation layer of the HBR PPTA hollow fiber membranes became dense and the pure water flux decreased from about 300 to 100 L·m−2·h−1. Then, the tensile force of HBR PPTA hollow fiber membranes reached above 600 N, which mainly depended on the tubular braids. Moreover, there was an effective interfacial bonding state between the separation layer and the tubular braids when the PPTA concentration was higher than 2 wt%. The HBR PPTA-3# hollow fiber membrane had a high BSA rejection rate, which could be achieved above 90%. Meanwhile, in different organic solvents, the solvents’ permeation of HBR PPTA-3# hollow fiber membranes was about 150–200 L·m−2·h−1. Especially, the THF permeation was above 270 L·m−2·h−1, which was nearly similar to the PWF of HBR PPTA-1# hollow fiber membranes. Moreover, the HBR PPTA-3# hollow fiber membranes applied in the MBR system showed stable removal rates of NH4 +–N and TP; the average removal rates were 96.71% and 49.81%, respectively, and the filtrate quality was stable. Based on the changes in the elemental mass fraction on the membrane surface after hydraulic backwashing and chemical cleaning, the inorganic elements were removed after a short period of citric acid cleaning, and the HBR PPTA-3# hollow fiber membrane was more resistant to pollution.

  1. Funding information: This research was financially supported by the National Natural Science Foundation of China (Grant No. 21808165, 52173038) and Jiangsu Provincial Science and Technology R&D Projects of China – Key Core Technology Tackling (BE2022140).

  2. Author contributions: Chun Wang: conceptualization, methodology, writing – original draft; Jingjing Yan: methodology, supervision, project administration, writing – review and editing; Dinghe Yan: investigation, visualization; Haolong Xue: investigation; and Shubin Song, Changfa Xiao: supervision, funding acquisition.

  3. Conflict of interest: The authors state no conflict of interest.

  4. Data availability statement: Data will be made available and shared on request.

Appendix
Figure A1 
                  The outer surface morphologies of HBR PPTA hollow fiber membranes after ultrasonic treatment: (a) HBR PPTA-1#, (b) HBR PPTA-2#, and (c) HBR PPTA-3#.
Figure A1

The outer surface morphologies of HBR PPTA hollow fiber membranes after ultrasonic treatment: (a) HBR PPTA-1#, (b) HBR PPTA-2#, and (c) HBR PPTA-3#.

Figure A2 
                  The cross-sectional morphologies of HBR PPTA hollow fiber membranes: (a) partial cross-section of HBR PPTA-1#, (b) partial cross-section of HBR PPTA-2#, (c) partial cross-section of HBR PPTA-3#, and (d) partial cross-section of HBR PPTA-4#.
Figure A2

The cross-sectional morphologies of HBR PPTA hollow fiber membranes: (a) partial cross-section of HBR PPTA-1#, (b) partial cross-section of HBR PPTA-2#, (c) partial cross-section of HBR PPTA-3#, and (d) partial cross-section of HBR PPTA-4#.

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Received: 2023-06-01
Revised: 2023-07-05
Accepted: 2023-07-06
Published Online: 2023-08-21

© 2023 the author(s), published by De Gruyter

This work is licensed under the Creative Commons Attribution 4.0 International License.

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