Introduction

Membrane fouling remains a major barrier limiting the application of ultrafiltration in water and wastewater treatment owing to the resulting increased operating costs and operational constraints (e.g. lower membrane fluxes). Various factors affect membrane fouling, including the membrane characteristics, water conditions, the type of pre-treatment (choice of coagulant and dose) and the operating conditions1, but not the mixed liquor suspended solids concentration or zeta potential of biomass in the case of membrane bioreactors (MBRs)2. Tian et al.3 found that the biopolymer content in water is an important indicator for predicting membrane fouling potential in UF processes and there was no correlation with the presence of humic substances and UF membrane fouling.

Floc-bound extracellular polymeric substances (EPS) have been suggested to play a role in the fouling process of full-scale and the pilot-scale MBR units4. Also, it has been reported that proteins and polysaccharides could be the cause of biofouling5. During the long-term operation of an MBR, bound EPS demonstrated positive correlations with membrane fouling6, produced by different species of bacteria7. Other studies have reported that the concentration of soluble EPS or polysaccharides and the number and size of the bioflocs were responsible for the observed differences in the membrane fouling8,9.

It has been shown that the increased adsorption of EPS onto a membrane resulted in a significant decrease in permeate water flux and EPS production may influence sludge deposition (and attachment rate) and thereby affect the biofouling propensity of the membrane10. The aggregation abilities of sludge samples have been shown to decrease with the extraction of EPS, which confirmed the crucial role of EPS in sludge aggregation, including loosely bound EPS and tightly bound EPS11. It has also been observed that the accumulation of biopolymer clusters in the sludge mixture of a MBR facilitates the formation of a sludge fouling layer on the membrane surface, thus causing serious fouling12. Furthermore, as the thickness of the bio-cake grows, an anoxic and endogenous environment may develop in the lower parts of the bio-cake layer, ultimately leading to cell lysis and release of polysaccharides13,14.

In view of the foregoing observations it is evident that decreasing the EPS concentration and/or inactivating bacteria on the surface of a membrane are potential methods of mitigating fouling. Various approaches have been studied and reported in the literature. A quorum quenching enzyme (acylase) was directly immobilized onto a nanofiltration membrane to mitigate biofouling in a nanofiltration process, which prohibited the formation of a mushroom-shaped mature biofilm15. Fungal inoculation was found to prevent biofouling of MBRs by microbial degradation of primary biofoulants16. Modification of the membrane surface to provide anti-adhesion and anti-bacteria properties has been studied17, as well as grafting copolymers on PVDF surfaces to provide a potent anti-biofouling behavior18. Coating TiO2/polyvinyl alcohol (PVA) on the membrane surface could loosen the cake layer and decrease filtration resistance (membrane fouling) in the treatment of a simulated wastewater19. We believe some of the more extensive research on MBR processes is relevant to the drinking water application.

In addition to changing the surface properties of the membrane, other studies have found that many factors can be controlled to decrease the membrane fouling, such as mechanical stresses20, cell residence times2,21, calcium concentration22, adding cationic polymeric material23 and flocculants24 and by applying intermittent direct electrical current25. Membrane fouling through fiber clogging that is caused by sludge accumulation on the membrane can be prevented by mechanical methods, such as adding suspended carriers26 and moving media27. Powdered activated carbon inside the reactor enhanced the biodegradation of polysaccharides and proteins and mitigated membrane fouling28. Membrane fouling could be also effectively prevented by pre-ozonation29,30 and both external and internal fouling could be effectively mitigated31. A sufficient supply of oxygen could achieve low concentrations of soluble microbial products and reduce membrane fouling9,13,32.

Chemical backwashing is also effective for controlling membrane fouling33 but represents an additional aspect of the process design and operation. Chlorine treatment (cleaning) is widely used by membrane filtration plants to recover the loss of membrane permeability encountered in low-pressure membrane (LPM) filtration of natural waters34,35. Although chemical solutions are widely employed to clean membranes, they can also be responsible for undesirable changes in membrane properties where either the functional properties of the membrane gradually change, or the membrane simply breaks up (hollow fibers)36,37,38; this is a consequence of the need for highly concentrated chemical solutions to wash fouled membranes.

Notwithstanding all the approaches described above for controlling membrane biofouling, the direct application of pre-chlorination has received very little attention to-date. Pre-chlorination is widely applied in treating surface waters for meeting various water quality objectives including pre-disinfection. In this paper, we have evaluated the benefits of applying a low dosage of NaClO continuously with alum as the pre-treatment before UF membrane filtration, in controlling membrane fouling, which is also confirmed for the surface water treatment in Beijing in recent days. It has been achieved through laboratory tests involving the quantification of key relevant factors, such as the dead/live ratio of bacteria, extracellular polymeric substances (EPS) and the properties of the cake layer. The experimental study and key findings are described in the following sections.

Methods

Synthetic raw water and coagulant

A synthetic raw water was prepared for the tests to represent a typical surface water source containing organic pollution arising from land runoff and sewage effluent discharge. Thus, a quantity of domestic settled sewage was added to local (Beijing, China) tap water in a volumetric ratio of 1:50, respectively. In addition, 5 mg/L (TOC≈ 2 mg/L) of humic acid (HA, sodium salt, Aldrich, Cat: H1, 675-2) was added to the raw water. The humic acid and domestic settled sewage represented respectively types of organic matter that are relatively easy or difficult to remove during typical drinking water treatment; the former characterized by high MW (molecular weight) hydrophobic molecules and the latter low MW hydrophilic substances. Prior to mixing with domestic sewage and humic acid solution, the tap water was left for one night to ensure the complete decay of residual chlorine. The characteristics of the synthetic raw water are listed in Table 1.

Table 1 Water quality of raw water and UF influents*/filtrates
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Aluminum sulfate hydrate (Al2(SO4)3·18H2O; Bodi, China, >99%) ‘alum’ was used as a coagulant in this study. Stock alum solution was prepared at a concentration of 0.1 M in DI water. Stock NaClO was prepared as 1 g/L (calculated as active Cl) and stored in the dark.

Two pretreatments before UF processes

Traditional coagulation and flocculation by alum without or with addition of NaClO (at a concentration of 1 mg/L, calculated as active Cl, since higher concentrations of NaClO may affect or change the membrane properties) before ultrafiltration (referred to as CUF/CUF-Cl) were operated in parallel. A schematic illustration of CUF and CUF-Cl arrangements is shown in Figure S1 in supporting information. Synthetic polluted raw water was fed into a constant-level tank to maintain the water head for the membrane tanks. A certain dose of alum (0.15 mM) with or without 1 mg/L NaClO was continuously added into the rapid mixing tanks. The rapid mix speed was 200 rpm (G = 184 s−1; calculated as our previous work39) in the mixing tank with a hydraulic retention time (HRT) of 1 min, which then reduced to 50 rpm (23 s−1) in the three flocculation tanks, each having a HRT of 5 min. After the flocculation tanks, the flow passed directly into the membrane tanks. Each tank contained a submerged polyvinylidene fluoride (PVDF) hollow-fiber UF membrane module (Tianjin Motimo Membrane Technology Co., Ltd, China) with a nominal pore size of 0.03 μm and a surface area of 0.025 m2. The permeate through the submerged membrane module was continuously withdrawn using a peristaltic pump at a constant flux of 20 L.m−2.h−1, operated in a cycle of 30 min filtration and 1 min backwash (40 L.m−2.h−1). Air was supplied to each reactor at 100 L/h (air: water = 200:1) only at every backwash. The trans-membrane pressure (TMP) was continuously monitored with pressure gauges. The HRT of the membrane tanks was maintained at 0.5 h and accumulated sludge was released every 2 days. The ultrafiltration process lasted for more than 60 days and the cake layer on the surface of membrane was removed by high pressure tap water washing once for the CUF system over the whole operation process. The operation conditions can be found in Table S1 of the supporting information.

Flow-cytometric measurements for bacteria in membrane tanks

The variation of bacteria in the membrane systems was measured by flow cytometry. Before staining and measurement, water samples were filtered by copper mesh (300 meshes) and then EDTA was added to all samples immediately before staining to disrupt the outer membrane of Gram-negative bacteria in water40.

Before analysis, all samples were incubated in the dark at 20°C for 25 min and then stained with a mixture of SYBR® Green I and propidium iodide (PI); staining concentrations were those reported previously41. Live cells have intact membranes and are impermeable to dye PI, which only leaks into cells with compromised membranes. SYBR® Green I stains all bacterial cells irrespective of their physiological state and stained cells can easily be distinguished from instrument background with flow cytometry. Thus a combination of these two dyes provides a rapid and reliable method for discriminating live and dead bacteria. Flow-cytometric measurements were made with a Partec CyFlow Space flow cytometer (BD Biosciences, San Jose, CA) with 488 nm excitation from a blue solid-state laser at 200 mW. In the flow cytometer, optical filters were set up so that PI was measured above 630 nm and SYBR® Green I, at 520 nm41.

Extraction and measurements of EPS from cake layer and sludge

At the end of operation, the fouled membrane modules were taken out from the reactors. The external foulants on the membrane surface were carefully scraped off with a plastic sheet (Deli, China). A heating and extraction method42 was modified to extract the loosely bound EPS (LB-EPS) and tightly bound EPS (TB-EPS) from the cake layers and make sure the EPS was not released from bacterial cells. Sludge suspension from cake layers was first dewatered by centrifugation (Anke TGL-10B, China) in a 20-mL tube at 4000 g for 5 min. The concentrate liquor was recovered for water quality analysis. The sludge pellet in the tube was re-suspended in 10 mL phosphate buffer saline (PBS) solution and the sludge suspension was then ultrasonically treated (KH-250DE, KunShanHeChuangultrasonic Co., Ltd., China) for 2 min. Without any delay, the suspension was then sheared by a vortex mixer (Vortex- Genie® 2, Mo Bio laboratories, Inc., USA) for 15 min, followed by centrifugation at 4000 g for 10 min. The organic matter in the supernatant was readily extractable EPS and was regarded as the LB-EPS of the biomass. For extracting the TB-EPS, the sludge pellet left in the centrifuge tube was re-suspended in PBS solution to its original volume (10 mL), ultrasonically treated for 3 min and heated to 80°C in a water bath for 30 min. The mixture was centrifuged at 20000 g for 15 min. The supernatant collected was regarded as the TB-EPS.

EPS extracted from the cake layer and sludge was measured by three-dimensional excitation-emission matrix (EEM) fluorescence and size exclusion chromatography (SEC). EEM fluorescence measurements were conducted using a spectrofluorometer (FP-6500, Jasco, Japan) equipped with a 150 W xenon lamp at ambient temperature of 25°C. Further details of the method can be found in previous research reported elsewhere31,43. SEC was carried out to determine the apparent molecular weight (MW) distribution of UV-active substances of EPS extracted from the cake layer and sludge. This measurement procedure was adapted from the method described by Allpike et al.44.

Fluorescence staining and confocal laser scanning microscopy (CLSM)

Intact, living and hydrated granules and flocs were stained with fluorescently labeled probes with different excitation and emission spectra in order to visualize the distribution of cells, polysaccharides and proteins in samples. Samples were stained in 1.5-ml Eppendorf tubes, covered with aluminum foil and placed on a shaker table (100 rpm) for 15 min each. After being stained by three dyes separately, whole samples were visualized directly by confocal laser scanning microscopy (CLSM; TCS SP 5, Leica, Germany). The probes were visualized on three channels with corresponding excitation and emission wavelengths as follows: FITC (488 nm/520 nm), ConA (543 nm/560 nm) and DAPI (371 nm/397 nm).

Fluoresceinisothiocyanate (FITC) (0.01%) is an amine reactive dye and stains all proteins and amino-sugars of cells and EPS45. Concanavalin A (ConA) lectin conjugated with Texas Red (100 μg/ml) was used in the present study to bind to α-mannopyranosyl and α-glucopyranosyl sugar residues. DAPI is a cell-permeative nucleic acid stain and was used to visualize all cells. All probes were purchased from Molecular Probes (U.S.A.) and samples were washed with PBS after each staining step.

Scanning electron microscopy (SEM) images

The fouled membrane fibers were cut from the two membrane modules and the foulant layer was retained on the membrane surface. The new and fouled membrane samples were then platinum-coated by a sputter and observed under scanning electron microscopy (SEM; JSM7401F, JEDL, Japan).

Results

TMP development in CUF and CUF-Cl systems

The addition of NaClO together with pre-coagulation by alum before ultrafiltration (CUF-Cl) was compared to only pre-coagulation by alum (CUF). In these experiments, the membrane flux of the CUF and CUF-Cl streams were both set at a constant value of 20 L.m−2.h−1 in a cycle of 30 min filtration/1 min water backwash and membrane fouling was represented by the increase in TMP. The comparative increase in TMP for the CUF and CUF-Cl streams is shown in Figure 1. It can be seen that the TMP in both membrane tanks increased with time from an initial value of 4.5 kPa and that a high pressure water wash was required for the CUF membrane on the 20th day, but none was required for the CUF-Cl membrane throughout the 70 day run.

Figure 1
figure 1

Variation of TMP with time for different pretreatment conditions over an operating period of approximately 70 days (20 L.m−2.h−1).

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Comparing the two types of pretreatment, it was clear that the membrane fouling was dramatically different. The combination of alum and NaClO produced a membrane fouling rate much lower than that of only alum (Figure 1). The slope/gradient of the TMP increase with time (TMP rate) can be used to indicate the fouling rates46,47. The TMP increased quickly to 35 kPa from 4.5 kPa after 20 days' operation in the CUF system (TMP rate approximately 1.5 kPa/day), but it only increased to 12 kPa in the CUF-Cl system (TMP rate approximately 0.38 kPa/day). After 20 days of operation, the membrane module in the CUF was taken out from the tank and cleaned by high pressure tap water. It can be seen that the TMP of CUF membrane after washing was 8 kPa, which was only slightly higher than that of a new membrane. Therefore, we can conclude that the membrane fouling was mainly determined by the cake layer on the membrane surface.

The TMP of the CUF membrane after the high pressure wash increased substantially during the subsequent period of continuous operation and reached a value of nearly 50 kPa after approximately 50 days (TMP rate approximately 1.0 kPa/day). The lower TMP rate after washing, compared to the rate before, was believed to be because of the increase in water temperature and variation of water quantity. In sharp contrast, a much lower TMP rate (around 0.2 kPa/day) was evident in the CUF-Cl system throughout the whole period of operation. It was apparent that the TMP became relative stable from the 18th day to the 50th day and then gradually increased to 27 kPa at the 72th day.

The photograph in Figure 1 shows visually different cake layers on the surface of CUF and CUF-Cl membranes at the 60th day's operation, where the much thinner cake layer on the surface of CUF-Cl membrane (also see section 3.7) corresponded well with the lower rate of TMP increase.

Comparison of EPS by EEM in the two membrane systems

Many researchers have found that membrane filtration performance was determined by the EPS in the cake layer for waste water treatment (e.g. Laabs et al.48). Therefore, in this study, the EPS was extracted from the cake layer and sludge from this synthetic drinking water and then analyzed using EEM spectroscopy at the end of operation with respect to LB-EPS and TB-EPS (Figure 2).

Figure 2
figure 2

EEM fluorescence spectra of EPS in cake layer on the membrane surface: LB-EPS on CUF (a) and CUF-Cl (b), TB-EPS on CUF (c) and CUF-Cl (d).

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Information describing the nature of peaks within EEM fluorescence spectra has been reported by some researchers31,43. The results here showed that LB-EPS was mainly composed of protein-like substances (intensity peak T1 and peak T2), but its concentration in the cake layer from the two membrane systems was significantly different (Figures 2a and 2b). Peak T1 and peak T2 in the CUF tank were higher than in the CUF-Cl tank, which indicated that some bacteria were inactivated by the presence of NaClO and produced less LB-EPS.

The EEM fluorescence spectra of TB-EPS extracted from the cake layers in the CUF and CUF-Cl systems are shown in Figure 2 (c and d). It was demonstrated that TB-EPS were composed of humic-like substances represented by Peak A and peak C, as the primary components in the cake layer of the two systems. The appearance of dominant humic acid-like peaks of TB-EPS extracted from the cake layer in both systems indicated the accumulation of humic acid-like substances on the membrane surface. The intensities of peak A and peak C in the CUF cake layer were much higher than in the CUF-Cl. Although peak A overlapped peaks T1 and T2, both two peaks can be distinguished, which showed that there were still some protein-like materials in TB-EPS. It was evident that the intensities (fluorescence units – FU) of peak T1 (358 FU) and peak T2 (258 FU) in the CUF cake layer were greater than those in the CUF-Cl system (165 and 126 FU, for peak T1 and T2).

Overall, the higher LB-EPS and TB-EPS concentrations observed in the CUF cake layer, than in the CUF-Cl cake layer, may be one of the main reasons for the different degree of membrane fouling in the two systems.

Comparison of EPS by SEC in the two membrane systems

The apparent MW distributions of LB-EPS and TB-EPS extracted from the cake layers in the CUF and CUF-Cl systems were measured by SEC and given in terms of UV absorbance at 254 nm (Figure 3). There were two main peaks with MW between 105 and 106 (EPS) and between 103 and 104 (HA) for both LB-EPS and TB-EPS. The higher MW peak (>105) is most likely attributable to polysaccharide and protein-like substances, which was reported previously by Al-Halbouni et al.49.

Figure 3
figure 3

MW distribution of EPS from cake layer and different ages of sludge: LB-EPS (a) and TB-EPS (b) (same conditions as for Figure 2 and Figure S2).

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Comparing the LB-EPS substances extracted from the two cake layers, there appeared to be no significant differences in the absorbance peak in the range, 103 ~ 104. In contrast, for the MW peak between 105 and 106, the magnitude of the absorbance was significantly greater and the concentration of LB-EPS extracted from the CUF cake layer was much greater than from the CUF-Cl cake layer. The difference in MW distributions of LB-EPS in the cake layers in the CUF and CUF-Cl systems suggested that fewer bacteria in the CUF-Cl system produced less LB-EPS, which may influence the nature of the cake layer.

For TB-EPS, it was found that the dominant organic matter were HA-type substances with MW between 103 and 104, but there were no significant differences in the MW distributions for the cake layers in the CUF and CUF-Cl systems. Comparing Figure 3b with Figure 2, it is evident that peaks A and C in the EEM spectra were not only composed of HA substances, since a secondary peak was present in the MW range of 105 and 106. The concentration of organic matter with MW between 105 and 106 in the CUF cake layer was greater than that in the CUF-Cl cake layer. In the light of these results, it seems that controlling the concentration of LB-EPS may be a good way to decrease the membrane fouling.

Variation of bacteria measured by flow cytometry

As living bacteria in the membrane system produce EPS, which may contribute to membrane fouling, measurements of the ratio of dead/live bacteria in the influent of both membrane systems were made using flow cytometry with staining by a combination of SYBR® Green I and PI. Two clusters, representing dead and live fractions, were observed for both membrane systems, as shown in Figure 4 and the dead/live ratio was 38.4%/61.6% in the CUF influent. For the CUF-Cl influent, a shift of the two clusters increased the red fluorescence intensity in the dead cell part and the dead/live ratio was 72.2%/25.8%. These measurements are consistent with the expected inactivation of bacteria in the UF influent caused by the addition of NaClO. In addition, it was evident from Table 1 that the concentration of NH4+-N in the CUF-Cl influent (tank) was higher than in the CUF influent (tank), which indicated there was less overall nitrification (NH4+-N into NO3−-N) in the CUF-Cl system owing to inactivation of bacteria by NaClO. The presence of bacterial populations with different dead/live ratios in the cake layer on the membrane surface may produce different EPS (protein and polysaccharide) concentrations in the cake layer. Thus, for the CUF-Cl system a lower EPS produced by the higher dead/live ratio of bacteria, may induce a lower connection ability of flocs onto the cake layer and thereby contribute to a lower degree of membrane fouling, as the existence of EPS increases the aggregation abilities of sludge/floc11.

Figure 4
figure 4

Examples of flow-cytometric dot plots from stained water samples: a) CUF influent and b) CUF-Cl influent.

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CLSM

In order to further confirm the higher concentrations of protein, polysaccharides and bacteria in the CUF than in the CUF-Cl systems, CLSM images of samples of the cake layer were taken. It was found that protein and polysaccharides (sugar) were extensively distributed on both membrane surfaces, together with some bacteria (Figure 5). Comparing the two cake layers, it was evident that more proteins and polysaccharides (sugar) were present in the CUF cake layer than in the CUF-Cl cake layer (Figures 5a–5d). Similarly, the DAPI stain images indicated a higher concentration of bacteria in the CUF cake layer (Figures 5e and 5f). More than 10 images for every sample confirmed these results, which were of statistic.

Figure 5
figure 5

CLSM images of cake layer on the surface of membranes: stained with FITC in CUF (a) and CUF-Cl (b), stained with ConA-Red in CUF (c) and CUF-Cl (d) and stained with DAPI in CUF (e) and CUF-Cl (f) (FITC stains all proteins and amino-sugars of cells and EPS; ConA-Texas Red stains α-mannopyranosyl and α-glucopyranosyl sugar residues; DAPI stains all dead and live cells).

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The images showed that the addition of NaClO inactivated bacterial activity in the CUF-Cl system, leading to lower concentrations of bacteria and their associated proteins and polysaccharides, in the cake layer. Since polysaccharides and proteins can enhance the connection ability of flocs within the cake layer, their lower concentrations in the CUF-Cl system contributed to a reduced thickness of the cake layer. The evidence from these CLSM images is consistent with the other tests described above with regard to the relative presence of bacterial populations and the impact on TMP in the two systems.

SEM images

The tests described above have focused on microbial indicators, but did not consider the structure of the membrane cake layer. Figure 6 presents SEM images of fouled and washed UF membranes and cross-section images of the cake layer. The pre-coagulated fouling layer looked like a colloidal deposit with relatively low density, which was formed by small primary particles of around 30 nm size (Figure 6a). According to the SEM images of the cake layer on the surface of membrane, although the size of the nano-scale primary particles changed little by the addition of NaClO, the porosity of the cake layer in the CUF-Cl system appeared to be greater than in the CUF system. Comparing the images of the fouled membranes after washing by sponge, the porosity of both membranes was very similar (Figures 6c and 6d), but had decreased slightly, compared to a new membrane (Figure S2), through particulate adsorption in/on the membrane pores/surface. These results indicate that the addition of NaClO increased the porosity of the cake layer, but did not change the extent of internal membrane fouling.

Figure 6
figure 6

SEM images of membranes with different pretreatments: membrane fouled by CUF flocs (a) and CUF-Cl flocs (b); fouled membrane surface washed by DI water in the CUF (c) and CUF-Cl (d) systems; cross-section of CUF cake layer (e) and CUF-Cl cake layer (f).

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SEM images were also used to provide information about the thickness of the cake layer on the surface of the two membranes (Figures 6e and 6f); this was based on samples cut from the top of the membrane modules. The cake layer formed in the CUF system was considerably thicker than in the CUF-Cl system (more than 6 times). It is believed that the high concentration of proteins and polysaccharides (especially LB-EPS) in the CUF cake layer enabled the coagulant flocs or particles to attach easily to the cake layer on the surface of membrane, increasingly with time, thereby forming a thicker cake layer. The results of subsequent research showed that flocs and related nano-particles are difficult to attach onto the surface of bacteria after the addition of NaClO (Figure S4 in supporting information). Similar results were found with MBR processes in waste water treatment50,51. Therefore, the different pretreatment conditions led to significant differences in the thickness and structure of the cake layers deposited on the membrane surface, thereby causing different degrees of membrane fouling. It is believed that a higher density and larger thickness of the cake layer in the CUF system (external fouling), gave a much higher membrane fouling overall.

Variation of THMs and HAAs in the two membrane tanks

The occurrence and removal of THMs and HAAs in the CUF and CUF-Cl systems were investigated since these compounds were present in the raw water (from the tap water) and formed from the hypochlorite dosing in the CUF-Cl system. The compound concentrations were measured in the raw water and pre- and post- UF and the results are shown in Figure S3. As expected, the concentrations of HAAs were generally lower than THMs in the raw and UF influent waters and influent concentrations were increased slightly by hypochlorite dosing. The combination of coagulation and UF had very little effect on reducing HAA concentrations (Figure S3a) but achieved approximately 50% reduction in total THMs (Figure S3b). The total THMs was higher in the CUF-Cl influent than in the CUF influent (60 ± 10 μg/L and 50 ± 12 μg/L, respectively), but there was no detectable difference after ultrafiltration for the two systems (40 ± 8 μg/L and 41 ± 10 μg/L). In all, a low dosage of NaClO has no adverse effect on the formation of disinfection by-products.

Conclusions

1. The combination of alum and a low dose of NaClO (1 mg/l) as pretreatment before UF membrane separation (CUF-Cl) substantially reduced the rate (near 60%) of membrane fouling compared to alum only as pretreatment (CUF). The result is also found in drinking water plants (Beijing) by the pilot scale experiments in recent days.

2. The addition of the NaClO was found to cause a substantial inactivation of bacteria, which resulted in lower microbial proliferation and less production of proteins and polysaccharides. The lower presence of polysaccharides applied to both loosely-bound (LB-EPS) and tightly-bound (TB-EPS) substances and was evident from a reduction in the concentration of 105 to 106 MW compounds. The concentration of polysaccharides within the cake layer is believed to be a key factor causing membrane fouling.

3. Although the size of nano-scale primary particles in the influent flow appeared to be unchanged by the addition of NaClO, the porosity of the cake layer in CUF-Cl system was greater than that without chlorine (CUF system), possibly because of a lower concentration of LB-EPS in the CUF-Cl cake layer. Furthermore, the thickness of the cake layer formed in the CUF-Cl system was substantially thinner (less than 6 times) than that in the CUF system, which is also believed to be the result of lower concentrations of protein and polysaccharide in the cake layer. Thus, the combination of a more porous and thinner cake layer helps to explain the lower rate of membrane fouling as indicated by the TMP.

4. The addition of a low dose of NaClO (1 mg/l) did not have any significant adverse effect on the formation of disinfection by-products, as indicated by the concentrations of THMs and HAAs after ultrafiltration.