Review of New Approaches for Fouling Mitigation in Membrane Separation Processes in Water Treatment Applications

: This review investigates antifouling agents used in the process of membrane separation (MS), in reverse osmosis (RO), ultraﬁltration (UF), nanoﬁltration (NF), microﬁltration (MF), membrane distillation (MD), and membrane bioreactors (MBR), and clariﬁes the fouling mechanism. Membrane fouling is an incomplete substance formed on the membrane surface, which will quickly reduce the permeation ﬂux and damage the membrane. Foulant is colloidal matter: organic matter (humic acid, protein, carbohydrate, nano/microplastics), inorganic matter (clay such as potassium montmorillonite, silica salt, metal oxide, etc.), and biological matter (viruses, bacteria and microorganisms adhering to the surface of the membrane in the case of nutrients) The stability and performance of the tested nanometric membranes, as well as the mitigation of pollution assisted by electricity and the cleaning and repair of membranes, are reported. Physical, chemical, physico-chemical, and biological methods for cleaning membranes. Biologically induced bioﬁlm dispersion effectively controls fouling. Dynamic changes in membrane foulants during long-term operation are critical to the development and implementation of fouling control methods. Membrane fouling control strategies show that improving membrane performance is not only the end goal, but new ideas and new technologies for membrane cleaning and repair need to be explored and developed in order to develop future applications.


Introduction
According to United Nations International Children's Emergency Fund (UNICEF) reports, over 740 million people worldwide do not have adequate safe water supply, while over 2.5 billion people have access to combined water supply [1]. Traditional water treatment technologies were developed primarily to reduce the risks of waterborne diseases by removing or chemically inactivating viruses, bacteria, and protozoa [2]. Technologies for desalinating seawater and removing contaminants from polluted water bodies are among the advanced water treatment processes [3]. Membrane-based processes, advanced oxidation, and adsorption on activated carbon and other substrates are examples of advanced water treatment processes.
Since 1960, membrane-based technologies have been used in water purification and desalination [4]. Membrane water treatment is a method of removing undesirable constituents from water. A membrane is an imperfect barrier that allows some substances to pass through while blocking others. Water treatment facilities clean surface water, groundwater, and wastewater using various membranes and processes to produce clean water for industry and drinking [5]. The pressure gradient, chemical potential, temperature, or current flux used to pass liquids, gases, particulates, molecules, and ions is the driving force behind membrane technologies. The concentration gradient of chemical potential as the driving force in dialysis and forward osmosis. Membrane desalination is a ature-driven membrane process. Water desalination is currently best accom through reverse osmosis or electrochemical treatment methods.
Membrane fouling is the deposition and accumulation of organic, inorganic ological substances on the membrane surface, which results in the formation of a layer with resistance to hydraulic flow or a loss of membrane performance [6,7]. occurs when the convective transport of foulants from the feed solution to the me surface outweighs the back-diffusion of foulants from the membrane surface bac bulk solution [8]. Fouling not only increases hydraulic resistance, but it also ca formation of a cake layer with significant cake-enhanced concentration pola (CECP) effects, the formation of a cake layer that blocks membrane pores, or a c tion of these effects. In the literature, several potential membrane foulants have be tified and reported. Silica colloids, latex colloids, sodium alginate, colloidal alumi ide, humic acid, bovine serum albumin (BSA), fatty acids, surfactants, natural org ters (NOM), and cellulose are among them [9,10]. These macromolecules enter solution due to unregulated disposal. Several factors contribute to foulant deposi attachment on the membrane surface, which promotes foulant deposition and atta The discussion of membrane fouling entails investigating the factors that influen brane fouling.
The following factors contribute significantly to membrane fouling [11]: chemistry and composition, i.e., pH, ionic strength, and foulant concentration; centration polarization (CP) is broadly defined as the deposition of rejected solute membrane's surface, resulting in the polarized layer, a region near the membra spatially varying concentrations. This increased resistance raises the osmotic across the membrane, lowering the driving force of the process (TMP), permeate f observed solute rejection, all of which increase the possibility of membrane failur (iii) Membrane material type, porosity, hydrophobicity, surface charges, membra phology, and membrane molecular weight cut-off (MWCO) are all examples of me properties; (iv) Temperature, pressure, aeration, permeate flux, and several othe dynamic conditions are examples of process operating conditions. Pressure is used as a common driving force for membrane separation [14]. D ing on the pore size and operating mechanisms, pressure-driven membranes can sified as MF, UF, NF, and RO ( Figure 1) [15].  The schematic presentation of pressure-driven membrane for wastewater treatment [16].
Complete pore blocking, partial pore blocking, internal pore blocking, and cake formation are the four types of fouling mechanisms identified by Hermia [17] that can occur in membrane processes. Because more than one type of fouling can occur simultaneously in a process, the chemical nature of the foulants (e.g., organic, inorganic, or biological) in a process, the chemical nature of the foulants (e.g., organic, inorganic, o must be known in order to inhibit or at least control such mechanisms [18] classification, the pollutant's nature can provide an overview of the type of its impact on membrane properties. Adsorption, accumulation, or precipitati ple, can occur on the surface or within the pores of the membrane. This c membrane's separation performance, such as permeate flux and membrane s well as membrane lifetime [19,20].
The buildup, deposition, and/or adsorption of foulants on the surface of a pressure-driven membrane results in membrane deterioration, permea lute removal efficiency, and TMP drop [12]. The fouling mechanism of lowand UF membranes differs from that of high-pressure NF and RO membra tion in the pore and obstruction are more prevalent in MF and UF membra surface foulants are more common in NF and RO membranes due to the mo non-porous features of RO membranes. Surface fouling is less "hazardous" RO membrane fouling. It is more reversible and may be readily regulated b feedwater fluid dynamics or chemical cleaning. Surface and interior foulin may be permanent depending on the composition of the entering water and tion with the membrane [12].   [12].
Scale is the precipitated inorganic crystals of Ca 2+ , Mg 2+ , CO3 2-, SO4 2-, an Scale formation involves complex crystallization mechanisms and transport the pressure-driven desalination process, when the ion solubility limit is e concentration of the dissolved salt increases 4 to 10 times, resulting in c [21,22]. The ions from the supersaturated solution crystallize at the surface o surface crystallization and bulk crystallization [23]. The former is simply d scale growth (the mechanism of crystal growth due to heterogeneous nucleat plicated process and depends on the interfacial energy at the interfaces in th the surface morphology, in detail in reference [24]), which is more common operating pressure and low cross flow velocity. The latter is the uniform gro cles in the mass phase at high pressure and moderate cross flow velocity. Fi a schematic diagram of the key steps in the formation of scale on the surfa membrane. Colloidal fouling [12].
In the pressure-driven desalination process, when the ion solubility limit is exceeded, the concentration of the dissolved salt increases 4 to 10 times, resulting in crystallization [21,22]. The ions from the supersaturated solution crystallize at the surface of the film by surface crystallization and bulk crystallization [23]. The former is simply due to lateral scale growth (the mechanism of crystal growth due to heterogeneous nucleation is a complicated process and depends on the interfacial energy at the interfaces in the system and the surface morphology, in detail in reference [24]), which is more common under high operating pressure and low cross flow velocity. The latter is the uniform growth of particles in the mass phase at high pressure and moderate cross flow velocity. Figure 3 shows a schematic diagram of the key steps in the formation of scale on the surface of the RO membrane.  [25].
Biological fouling (biofouling) is caused by the adhesion of live microorganisms t the membrane surface from the feed water. These microorganisms rapidly grow to form a biofilm at the expense of nutrients in the feed. Unlike silica fouling and colloidal fouling which mainly occur on specific elements in RO facilities, biological fouling occurs at an stage of the desalination process, mainly resulting in the fouling of the RO membran [26,27]. Organic fouling combines the deposition, reaction, and interaction of high-molec ular-weight organic molecules, such as natural organic matter (NOM) and/or transparen exopolymer particles (TEP), with the membrane surface. Due to the degradation and de composition of living organisms, NOMs, for example, fulvic acid and humic acid, exist i seawater. TEPs are mainly composed of long-chain polymers of amino sugars or muco polysaccharides, which are derived from organic substrates released by aquatic organ isms. Dissolved organic matter (DOM) TEP can occur through biological and non-biolog ical pathways [28]. In the biological pathway, TEPs are produced by microorganism through the shedding of the mucosal/cellular lining, while in the non-biological pathway TEPs are formed from precursors in a specific aquatic environment. In surface seawater the number of TEP with a particle size of approximately 0.4 to 200 µm can reach 400 TEP/mL [29].
To ensure the long-term operating sustainability of membrane filtering systems, reg ular physical and chemical cleanings, as well as various methods of membrane foulin management, are used during operation [30]. Those fouling control measures, on the othe hand, will lead to increased process complexity and, as a result, operational costs. Mem brane fouling can be characterized as reversible or irreversible depending on the foulan cleanability. Reversible fouling may be addressed with basic physical cleanings (e.g., wa ter flushing, air sparging, and backwashing), but irreversible fouling needs chemica cleaning [31,32].
Because membrane fouling is unavoidable, effective tactics and approaches are re quired to mitigate its negative effects. As a result, many researchers are focusing thei efforts on creating effective membrane fouling management strategies. Modifying mem brane surface characteristics [33,34], improving operating parameters [35,36], and provid ing feed pre-treatment [37] are the most frequent ways for membrane fouling manage ment.
In this review article, we have discussed the fouling problems in the membrane tech nology for use in water and wastewater treatment. This review contains an overview o various factors affecting membrane fouling and several approaches to overcome thi problem.  [25].
Biological fouling (biofouling) is caused by the adhesion of live microorganisms to the membrane surface from the feed water. These microorganisms rapidly grow to form a biofilm at the expense of nutrients in the feed. Unlike silica fouling and colloidal fouling, which mainly occur on specific elements in RO facilities, biological fouling occurs at any stage of the desalination process, mainly resulting in the fouling of the RO membrane [26,27]. Organic fouling combines the deposition, reaction, and interaction of high-molecular-weight organic molecules, such as natural organic matter (NOM) and/or transparent exopolymer particles (TEP), with the membrane surface. Due to the degradation and decomposition of living organisms, NOMs, for example, fulvic acid and humic acid, exist in seawater. TEPs are mainly composed of long-chain polymers of amino sugars or mucopolysaccharides, which are derived from organic substrates released by aquatic organisms. Dissolved organic matter (DOM) TEP can occur through biological and non-biological pathways [28]. In the biological pathway, TEPs are produced by microorganisms through the shedding of the mucosal/cellular lining, while in the non-biological pathway, TEPs are formed from precursors in a specific aquatic environment. In surface seawater, the number of TEP with a particle size of approximately 0.4 to 200 µm can reach 4000 TEP/mL [29].
To ensure the long-term operating sustainability of membrane filtering systems, regular physical and chemical cleanings, as well as various methods of membrane fouling management, are used during operation [30]. Those fouling control measures, on the other hand, will lead to increased process complexity and, as a result, operational costs. Membrane fouling can be characterized as reversible or irreversible depending on the foulant cleanability. Reversible fouling may be addressed with basic physical cleanings (e.g., water flushing, air sparging, and backwashing), but irreversible fouling needs chemical cleaning [31,32].
Because membrane fouling is unavoidable, effective tactics and approaches are required to mitigate its negative effects. As a result, many researchers are focusing their efforts on creating effective membrane fouling management strategies. Modifying membrane surface characteristics [33,34], improving operating parameters [35,36], and providing feed pre-treatment [37] are the most frequent ways for membrane fouling management.
In this review article, we have discussed the fouling problems in the membrane technology for use in water and wastewater treatment. This review contains an overview of various factors affecting membrane fouling and several approaches to overcome this problem.

Pressure Driven Membrane Processes
Depending on the water supply, fouling in RO systems include (i) particulate/colloidal fouling, (ii) scaling, (iii) organic fouling, and (iv) biofouling. Autopsies revealed that the fouling kinds and processes differed between seawater RO (SWRO) and wastewater RO (WWRO). SWRO and WWRO (lead and terminal modules) autopsies were done after five and three months of operation, respectively. The fouling layers were subjected to ultrastructural, chemical, and microbiological examinations. The WWRO train exhibited mostly bio/organic fouling at the lead position element and mostly inorganic fouling at the terminal position element, whereas the SWRO train contained bio/organic fouling at both end position elements. In the case of WWRO membranes, Betaproteobacteria were the most abundant colonizing species, with Ca, S, and P being the most abundant inorganic elements. Alpha and Gammaproteobacteria dominated the microbial community of SWRO membranes. Ca, Fe, and S were the most common inorganic components found in the fouling layer of SWRO membranes [38,39]. Small-size colloidal solids cause colloidal fouling. Larger colloids are not greatly shown by dynamic fluid elevation effects for crossflow speed profiles near the membrane surface. Colloidal dirt, clay, iron oxide, silica particles, proteins, polysaccharides, organic polymers, bacteria, nano/microplastics [40,41], and viruses (biocolloids) [42,43] have a range of size from 1 to 1000 nm. However, there are no well-defined limits [44], Colloidal fouling in RO is studied widely as it is summarized by two review articles [44,45].
Inorganic scale is a mineral precipitate on the surface of the membrane. In the case of a salt-rejecting membrane system, as used for NF and RO, the concentration of dissolved mineral salt increased 4-10 times according to the conditions of operation and efficiency of the membrane [46] both cause CP of on the surface of the membrane. When the salinity concentration exceeds its solubility limit, they can be crystallized on a scale of formation of the membrane surface. The most common component of the scale in the RO application is CaCO 3 , CaSO 4 , Ca 3 (PO 4 ) 2 , BaSO 4 , and silicates [21]. A deca-forming mechanism, its pattern and morphology have been reported [47][48][49][50]. Control strategies include chemical products [50,51] or physical disposal methods [52]. The type of scale and the suppression of scale formation have been reported [53,54].
Organic fouling is the most difficult to remove during the pre-treatment stage. Together with the desalination plant in the Mediterranean Sea, a pilot study of a seawater pretreatment system for desalination by RO has been carried out [55]. Although better seawater quality is achieved by advanced membrane treatment, neither membrane nor conventional pretreatment can guarantee the complete removal of NOM in feed. Organic matter is always present in the RO feed [56]: (i) NOM's natural; (ii) algae organic matter (AOM) composed of extracellular and intracellular macromolecules [57]; (iii) wastewater effluent organic matter (EfOM), determined by the background composition of NOM and soluble microbial products (SMPs) of biological wastewater treatment. NOM is one of the most important organic matters that causes RO fouling. Most of the NOM that exists on the surface, groundwater, and seawater is composed of humic substances [58,59]. The complex macromolecular products of chemical and biological degradation of animal and plant residues affect water quality and act as inorganic ion complexing agents [58].
Biological fouling: Unlike the other three forms of fouling, which can be managed by lowering the foulant concentration in the feedwater, biofouling is difficult to regulate simply by lowering the quantity of microorganisms in the feedwater [60]. Bacteria are everywhere and may easily attach, collect, and proliferate in a membrane system, even if their numbers are initially low. When bacteria cling and develop on RO systems, they produce a biofilm, which is a gel-like coating with a dense bacterial concentration and extracellular polymeric molecules [61]. Biofouling is one of the most problematic types of fouling in RO systems, accounting for more than 50% of the deposits removed from the membrane surface during autopsy studies [38,62]. Determining the biofouling tendency of the feed water prior to the RO system is essential in reducing the nutrient content. Chen et al. [63] examined the feasibility of using the retentate RO of the municipal water recovery plant from two aspects: (a) the fouling tendency of the RO retentate membrane and (b) the effectiveness of the anti-fouling strategy. The membrane used is an internal selective thin film composite polyethersulfone hollow fiber membrane (TFC/PES) membrane with high water permeability and good mechanical strength. Phosphate fouling is possible inorganic scale on the innermost layer of PES membrane, while silica fouling is the main scale on the outermost surface of the membrane. Two anti-fouling pretreatments, namely pH adjustment and anti-fouling pretreatment of the feed stream, are both simple and effective. Using RO retentate with pH 7.2 as the feed and 1 M NaCl as the draw solution, the average power density at 20 bar was 7.3 W/m 2 . By using HCl to modify the initial pH value of the RO retentate to 5.5, the average power density was increased to 12.6 W/m 2 , and by adding 1.1 mM ethylenediaminetetraacetic acid (EDTA), to 13.4 W/m 2 . Without specified pretreatment, the flow recovery rate of the fouled membrane washed with deionized water (DI) reached 84.9%, and it was air-bubbled for 30 min at a high crossflow velocity of 23.3 cm/s (Re = 2497) to reach 95.0% After minutes of pretreatment with pH adjustment, the flux recovery rate was increased to 94.6% after washing with DI, and the flux recovery rate was increased to 100.0% after bubbling. After the pretreatment by adding 1.1 mM EDTA to the RO retentate, the flux was almost completely restored by physical cleaning with DI and bubbling air. It is important to develop effective pretreatments by pH adjustment or by adding EDTA before RO and physical cleaning methods for membranes that generate osmotic energy by cleaning with DI and air jets. Figure 4 shows SEM-EDX and XPS images of the outer surface of the layer of fouled membrane at different retentate pH and pretreated with 1 mM EDTA. Zhang et al. [64] found that, in water reuse plants, pretreatment prior to RO systems prevents fast fouling. Secondary effluent may have a high suspended-solids load, as well as a high proportion of colloidal particles, organic compounds, and bacteria at times. If such components are not effectively removed during pretreatment, they might cause the permanent fouling of downstream RO systems. A pretreatment combination of advanced oxidation (ozonation), ceramic MF, and biological activated carbon (BAC) was evaluated to reduce RO membrane organic fouling. In comparison to MF and BAC, or ozone + MF, the fouling generated by the feed wastewater processed by the combination of ozonation + ceramic MF and BAC is readily eliminated by DI flushing. Figure 5 shows the surface morphology of the RO membrane after filtration using different Selfs Point pretreatment feed water. All membranes are cleaned with DI and filtered for about 1 h. Figure 5a shows that deionized water cleaning does not affect membranes exposed to untreated secondary effluent. Although the flux reduction rate of RO Using state-of-the-art TFC/PES hollow fiber membranes for osmotic power production, the power density and fouling tendency of RO retentate from a municipal water recycling facility were investigated. The fouling of RO retentate by phosphate salts and silica resulted in considerable decreases in water flow and power density. In PRO testing, the average power density of the first two batches was only 7.3 W/m 2 when utilizing the original RO retentate at pH 7.2 as the feed and 1 M NaCl as the draw solution at 20 bar. The scaling caused by phosphate salts was reduced by lowering the pH level as a consequence of employing the modified RO retentate with a starting pH of 5.5; the average power density was raised to 12.6 W/m 2 . At 1000 min, the ultimate pH level was 6.8, which was appropriate for disposal. The addition of 1.1 mM anti-scaling EDTA to RO retentate can prevent phosphate salt scaling and delay silica fouling. As a result, the mean power density was increased to 13.4 W/m 2 . Without chemical cleaning, the fouled membrane utilizing the original RO retentate as the feed solution had a cleaning efficiency of 84.9% by DI water flushing and 95.0% by air bubbling for 30 min after the PRO test at a high crossflow velocity of 23.3 cm/s (Re = 2497). Cleaning efficiencies were increased by 94.6% by DI water flushing and 100% by air bubbling when the initial pH value of RO retentate was lowered to 5.5. If the RO retentate was pre-treated with 1.1 mM EDTA, any cleaning technique could achieve 100% flux recovery. EDTA dose optimization and research into additional anti-scalants to minimize the fouling proclivity of RO retentate and phosphorus reduction should also be addressed. Figure 4 presents the SEM-EDX and XPS images of the outer surface of the layer of fouled membrane with the treatment conditions [63].
Zhang et al. [64] found that, in water reuse plants, pretreatment prior to RO systems prevents fast fouling. Secondary effluent may have a high suspended-solids load, as well as a high proportion of colloidal particles, organic compounds, and bacteria at times. If such components are not effectively removed during pretreatment, they might cause the permanent fouling of downstream RO systems. A pretreatment combination of advanced oxidation (ozonation), ceramic MF, and biological activated carbon (BAC) was evaluated to reduce RO membrane organic fouling. In comparison to MF and BAC, or ozone + MF, the fouling generated by the feed wastewater processed by the combination of ozonation + ceramic MF and BAC is readily eliminated by DI flushing. Figure 5 shows the surface morphology of the RO membrane after filtration using different Selfs Point pretreatment feed water. All membranes are cleaned with DI and filtered for about 1 h. Figure 5a shows that deionized water cleaning does not affect membranes exposed to untreated secondary effluent. Although the flux reduction rate of RO membranes with different pretreatment feeds is similar, the membrane surface after DI cleaning is quite different. In Figure 5b, the surface of the RO membrane used as a raw material for BAC pretreatment is still almost completely covered by scale. The membranes that use ozone and ozone + MF to pretreat wastewater (Figure 5c,d) are partially cleaned. However, combined ozone + MF pretreatment shows better performance than ozone pretreatment alone. In the latter case, the dirt is still trapped in the gaps of the two membranes. After a simple DI cleaning, the membrane contaminated by the ozone + MF ceramic +BAC pretreatment feed was almost completely recovered. Using ozone + ceramic MF + BAC to pretreat the feed, frequent RO permeation cleaning can reduce the CIP frequency of the RO membrane. Different RO feed pretreatments were tested to find a viable technology that would minimize the contamination of RO membranes used in remote areas, thus reducing the consumption of cleaning chemicals.
An ozone + ceramic + BAC membrane provides the best protection for the RO membrane. Any foulant in the water after this pretreatment combination can be easily removed from the RO membrane surface with DI. If DI is used frequently for cleaning, chemical cleaning may be reduced. Ozone combines with an MF ceramic membrane to effectively oxidize organic matter. With the ozone remaining in the test, the organic contaminants on the MF ceramic membrane appeared to be partially dissolved. Although BAC can effectively remove DOC from treated water, the retention rate of DOC from the RO membrane has also decreased. The BAC effluent must be pre-filtered to reduce bioorganic matter entering the RO system [64]. Membrane fouling will affect membrane performance and can occur with any type of water supply and membrane type. Scale can even be found in the secondary RO device that handles the RO permeate. The initial impact of the contamination is moderate, and the acceleration is relatively fast. If it is not resolved in time, the performance decrease will not be obvious.
The following steps are involved in the correction of fouling conditions: early detection of the fouling process, identification of fouling conditions and their mitigation, and correction of membrane performance. The cleaning operation sequence involves flushing the RO train with permeate water, connecting the train or train segment to the cleaning unit, An ozone + ceramic + BAC membrane provides the best protection for the RO membrane. Any foulant in the water after this pretreatment combination can be easily removed from the RO membrane surface with DI. If DI is used frequently for cleaning, chemical cleaning may be reduced. Ozone combines with an MF ceramic membrane to effectively e. f Direct osmosis is a common phenomenon in RO systems that treat high-salinity feed water. When a RO unit is turned off, permeate flows back through the membrane to the feed side. It is used in a novel cleaning technique known as direct osmosis-high salinity (DO-HS) membrane performance restoration. While the RO unit is running, the DO-HS technique is to inject a high-salinity solution into the suction of a high-pressure pump. The injection lasts for a few seconds. From the feed to the concentration, the high pulse passes via the membrane components. The flow across the membrane is reversed during the flow of a high-salinity wave via the feed channels of RO components. The foulants are lifted from the membrane surface by the reverse permeate flow. The continuous feed of concentrate flow sweeps removes foulant particles from the membrane components and transports them away from the membrane unit ( Figure 6). This approach of restoring membrane function is particularly successful in controlling membrane biofouling and removing colloidal deposits [65]. feed side. It is used in a novel cleaning technique known as direc (DO-HS) membrane performance restoration. While the RO unit technique is to inject a high-salinity solution into the suction of The injection lasts for a few seconds. From the feed to the conce passes via the membrane components. The flow across the memb the flow of a high-salinity wave via the feed channels of RO comp lifted from the membrane surface by the reverse permeate flow. concentrate flow sweeps removes foulant particles from the mem transports them away from the membrane unit ( Figure 6). Thi membrane function is particularly successful in controlling memb moving colloidal deposits [65]. In chemistry, it is oxidized and halogenated with chlorine chlorine are added to the RO feed stream as water disinfectants an the biological fouling of the direct media filtration system [67]. Ev In chemistry, it is oxidized and halogenated with chlorine (Cl 2 ). Oxidants such as chlorine are added to the RO feed stream as water disinfectants and bactericides to control the biological fouling of the direct media filtration system [67]. Even if the influent water is dechlorinated before the membrane system, there will still be exposure to very low concentrations of residual Cl 2 [68]. Chlorine in the form of hypochlorous acid (HOCl) and hypochlorite ions (OCl − ) attacks the dense layer on top of the poly amide (PA), replaces the hydrogen atoms in the amide nitrogen, and then undergoes cyclic chlorination through Orton's intermolecular rearrangement, resulting in the appearance of chlorination [69], as shown in Figure 7.
In addition to vulnerable amide nitrogen, the terminal NH 2 group in the PA chain is chlorine-sensitive and -reactive and oxidizes and decomposes into secondary and tertiary amine bonds in contact with Cl 2 [70]. Therefore, the degradation of the PA layer leads to the loss of membrane integrity and ultimately increases membrane flux and salt passage. Delamination between the PA layer and the support layer is the main reason for performance degradation and ultimately shortens the life of the RO membrane. Various parameters of the water supply, such as pH value, temperature, chlorine concentration, and contact time, will affect the rate of chlorine erosion [71]. Fouling and treatment methods on different membranes will be clarified. is dechlorinated before the membrane system, there will still be exposure to very low concentrations of residual Cl2 [68]. Chlorine in the form of hypochlorous acid (HOCl) and hypochlorite ions (OCl − ) attacks the dense layer on top of the poly amide (PA), replaces the hydrogen atoms in the amide nitrogen, and then undergoes cyclic chlorination through Orton's intermolecular rearrangement, resulting in the appearance of chlorination [69], as shown in Figure 7.

Figure 7.
Schematic diagram of the chlorine erosion of PA film and the performance degradation caused by attack [68].
In addition to vulnerable amide nitrogen, the terminal NH2 group in the PA chain is chlorine-sensitive and -reactive and oxidizes and decomposes into secondary and tertiary amine bonds in contact with Cl2 [70]. Therefore, the degradation of the PA layer leads to the loss of membrane integrity and ultimately increases membrane flux and salt passage. Delamination between the PA layer and the support layer is the main reason for performance degradation and ultimately shortens the life of the RO membrane. Various parameters of the water supply, such as pH value, temperature, chlorine concentration, and contact time, will affect the rate of chlorine erosion [71]. Fouling and treatment methods on different membranes will be clarified.
In NF, the pretreatment with coupled aluminum (Al) EC-MF reduces the colloid and organic fouling in the NF process of inland natural brackish surface water. The removal of NOM from EC is improved due to the following reasons: compared with the minimum solubility of Al (pH 5.5 vs. 6.2), the extensive protonation of NOM at a weakly acidic constant pH during electrolysis; the use of a medium current density (10 mA/cm 2 ) adequate contact time during electrolysis and flocculation; the combined charge neutralization and scanning solidification through increases in the Al dosage. FTIR spectroscopy provides direct evidence that, compared with MF alone, EC-MF removes the hydrophobic part and part of the hydrophilic residues of NOM. The flow curve of NF using EC-MF to pretreat natural brine is almost the same as the flow curve of a model solution with similar ionic composition, but no NOM added, indicating that the effect of organic fouling is negligible. XPS showed that there was a trace of CaCO3 precipitation after EC-MF pretreatment, which was confirmed by electron microscopy, which caused only a slight decrease in flux. Finally, NF achieves excellent strontium removal, as well as other divalent ions and NOM. EC improves the elimination of NOM by lowering the pH of the condensate, increasing the contact time between the coagulant and NOM and (pH 5.5, 10 mA/cm 2 current density, and 25 mg Al/L dose). Due to the chloride-assisted pitting corrosion, the high salt content of the influent leads to the dissolution of ultra-Faraday aluminum, and the high sulfate concentration and high applied current density further aggravate this pitting corrosion.
Compared to the MF-only pretreatment, the EC-MF pretreatment has better control of NF fouling due to the additional removal of parts of hydrophilic NOM (i.e., polysaccharides and amides), hydrophobic NOM, and nanocolloids, and a high Donnan effect rejects SO4 2− , Ca 2+ , Mg 2+ and Sr +2 ions, while the monovalent Na + and Cl − ions are poorly In NF, the pretreatment with coupled aluminum (Al) EC-MF reduces the colloid and organic fouling in the NF process of inland natural brackish surface water. The removal of NOM from EC is improved due to the following reasons: compared with the minimum solubility of Al (pH 5.5 vs. 6.2), the extensive protonation of NOM at a weakly acidic constant pH during electrolysis; the use of a medium current density (10 mA/cm 2 ) adequate contact time during electrolysis and flocculation; the combined charge neutralization and scanning solidification through increases in the Al dosage. FTIR spectroscopy provides direct evidence that, compared with MF alone, EC-MF removes the hydrophobic part and part of the hydrophilic residues of NOM. The flow curve of NF using EC-MF to pretreat natural brine is almost the same as the flow curve of a model solution with similar ionic composition, but no NOM added, indicating that the effect of organic fouling is negligible. XPS showed that there was a trace of CaCO 3 precipitation after EC-MF pretreatment, which was confirmed by electron microscopy, which caused only a slight decrease in flux. Finally, NF achieves excellent strontium removal, as well as other divalent ions and NOM. EC improves the elimination of NOM by lowering the pH of the condensate, increasing the contact time between the coagulant and NOM and (pH 5.5, 10 mA/cm 2 current density, and 25 mg Al/L dose). Due to the chloride-assisted pitting corrosion, the high salt content of the influent leads to the dissolution of ultra-Faraday aluminum, and the high sulfate concentration and high applied current density further aggravate this pitting corrosion.
Compared to the MF-only pretreatment, the EC-MF pretreatment has better control of NF fouling due to the additional removal of parts of hydrophilic NOM (i.e., polysaccharides and amides), hydrophobic NOM, and nanocolloids, and a high Donnan effect rejects SO 4 2− , Ca 2+ , Mg 2+ and Sr +2 ions, while the monovalent Na + and Cl − ions are poorly blocked by the NF membrane. These points and some implications of membrane and EC process operation/optimization have been clarified. DOC removal is enhanced by EC at a pH value slightly below the minimum solubility of aluminum (i.e., 5.5 vs. 6.2), which removed a portion of the hydrophilic fraction in addition to the typical hydrophobic and highermolecular-weight NOM fractions similar to enhanced conventional chemical coagulation. Therefore, in addition to the better control of NF contamination, this also reduces the formation of disinfection by-products, because the hydrophilic NOM component is also used as a precursor of trihalomethane and haloacetic acid. By using a high current density for brackish water, an increasingly shorter residence time can be designed in the EC unit, which will correspondingly reduce the frequency of NOM hydrogen bubble collision and NOM removal, which results in a suboptimal implementation. For aluminum, similar to iron, a current density of 10 mA/cm 2 is recommended to maximize NOM control and minimize electrolysis time. Electron micrographs of the above mentioned membranes are shown in Figure 8 [72].  Ohno et al. [73] studied the influence of coagulant residues on NF membrane fouling, laboratory-scale MF-NF and MF-NF pilot plant configuration. In lab-scale experiments, NF feedwater is pretreated with polyaluminum chloride (PACl) or alum before using MF. When the aluminum content of the feed water is greater than or equal to 18 µg/L, the permeability of the NF membrane decreases, but it does not decrease when the aluminum content is less than 9 µg/L. After pretreatment with FeCl 3 , the permeability of the NF membrane did not decrease significantly; residual iron did not affect permeability. When SiO 2 was added to water prior to pretreatment with PACl, the permeability of the membrane decreased at approximately twice the rate. Thermodynamic calculations and elemental analysis of fouling recovered from the membrane show that most inorganic fouling compounds are composed of aluminum, silicate, and possibly potassium. In the pilot plant, the NF feed is pretreated with PACl. The transmembrane pressure of NF doubled in 4.5 months of operation. Although the concentration of Al in the NF feed is not high (30 µg/L), analysis of the membrane contaminants shows that the excessive accumulation of Al and silicate indicates that Al residues cause the aluminosilicate or Al(OH) 3 fouling of the membrane. In the pilot-scale MF-NF factory experiment and laboratory-scale MF-NF experiment, when aluminum coagulant is used in the pretreatment process, the residual aluminum in the NF feed water is greatly increased, measured by the permeability of the membrane. In laboratory-scale experiments using FeCl 3 as a coagulant, the permeability of the NF membrane did not decrease significantly. In the laboratory-scale Al coagulant experiment, when the influent contains 18 µg/L or more of residual Al, the permeability of the NF membrane decreases, but not when the Al concentration is less than about 9 µg/L. The control of residual aluminum during NF pretreatment is essential to reduce severe fouling. The silicate concentration in the NF feed water greatly increases fouling, and other cations, especially potassium, can be incorporated into the foulants in the form of zeolite [73].
Xiong et al. [74] planned the layer-by-layer (LbL) self-assembly of positively-charged PEI and GA and NO-CMC alternately on the PES membrane surfaces, resulting in a new surface-modified NF membrane. The modification was intended to improve membrane separation performance. The AgNPs were coated on the modified membrane in two distinct ways as shown in (Figure 9) to improve the antibiological fouling performance of the NF membrane. To evaluate the produced membrane surface chemical composition and shape, FTIR, XRD, SEM, AFM, zeta potential, and water contact angle measurements were used.
The modified membrane rejected different single nonheavy metal salts in the following order: MgCl 2 > MgSO 4 > CaCl 2 > Na 2 CO 3 > NaCl > Na 2 SO 4 . Furthermore, the rejection rates of single heavy metal salts Cr 3+ , Cu 2+ , Cd 2+ , and Ni 2+ were 88.95%, 84.04%, 82.69%, and 83.47%, respectively. The results indicated that the (PEI@GA/NO-CMC)1.5/PES membrane performed well in terms of separation from nonheavy metal salts and heavy metal salts due to Donnan exclusion and steric hindrance. The resulting (PEI@GA-Ag/NO-CMC)1.5/PES membrane and (PEI@GA/NOCMC)1.5-Ag/PES membrane had a high antibiological fouling ability when AgNPs were loaded on the modified membrane in two distinct ways. At the same time, the antibacterial property of the (PEI@GA/NO-CMC)1.5-Ag/PES membrane was superior to that of the (PEI@GA/NO-CMC)1.5/PES membrane, indicating that (PEI@GA/NO-CMC)1.5/PES membrane had a higher capability for ameliorating antibiological fouling. To summarize, the produced NF membranes show a high potential for use in sewage treatment applications.
Xiong et al. [74] planned the layer-by-layer (LbL) self-assembly of positively-charged PEI and GA and NO-CMC alternately on the PES membrane surfaces, resulting in a new surface-modified NF membrane. The modification was intended to improve membrane separation performance. The AgNPs were coated on the modified membrane in two distinct ways as shown in (Figure 9) to improve the antibiological fouling performance of the NF membrane. To evaluate the produced membrane surface chemical composition and shape, FTIR, XRD, SEM, AFM, zeta potential, and water contact angle measurements were used. The modified membrane rejected different single nonheavy metal salts in the following order: MgCl2 > MgSO4 > CaCl2 > Na2CO3 > NaCl > Na2SO4. Furthermore, the rejection rates of single heavy metal salts Cr 3+ , Cu 2+ , Cd 2+ , and Ni 2+ were 88.95%, 84.04%, 82.69%, and 83.47%, respectively. The results indicated that the (PEI@GA/NO-CMC)1.5/PES membrane performed well in terms of separation from nonheavy metal salts and heavy metal salts due to Donnan exclusion and steric hindrance. The resulting (PEI@GA-Ag/NO-CMC)1.5/PES membrane and (PEI@GA/NOCMC)1.5-Ag/PES membrane had a high antibiological fouling ability when AgNPs were loaded on the modified membrane in two distinct ways. At the same time, the antibacterial property of the (PEI@GA/NO-CMC)1.5-Ag/PES membrane was superior to that of the (PEI@GA/NO-CMC)1.5/PES membrane, indicating that (PEI@GA/NO-CMC)1.5/PES membrane had a higher capability for ameliorating antibiological fouling. To summarize, the produced NF membranes show a high potential for use in sewage treatment applications. Figure 9. Schematic diagram of the preparation process and mechanism for the composite membrane [74]. Figure 9. Schematic diagram of the preparation process and mechanism for the composite membrane [74].
Purushothaman et al. [75] built an NF membrane using n-ZnO integrated PEES membranes. XRD-, AT-FTIR-, AFM-, and SEM-coupled EDX analyses were used to characterize the produced membranes. To study the effect of n-ZnO on membrane characteristics, pure water flow, contact angle, MWCO, mean pore size, and porosity were measured. The characterization revealed an asymmetric membrane structure following n-ZnO insertion. This addition improved the hydrophilicity of the PEES membrane. The model foulant HA was used to evaluate the fouling-resistant capability of the membranes, and an improved anti-fouling irreversible property with a matching flux recovery rate of 92.43% was discovered for the prepared membrane. Because of the hydrophilic nature of ZnO particles, the rejection performance and permeability of HA were 98.03% and 166.73 l m −2 h −1 , respectively at a constant transmembrane pressure (1380 KPa). Furthermore, the modified PEES membrane outperformed the standard PEES membrane in terms of separation performance for monovalent and divalent anions. The PEES/n-ZnO hybrid membrane helped NF in a successful method for improving membrane performance and anti-fouling property, indicating its vast use in water reclamation.
Yadav et al. [76] described a new kind of PSf/GO-vanillin NF membranes that are extremely permeable, selective, and fouling resistant. The membranes are made up of two-dimensional GO layers embedded with vanillin as a pyrogen and PSf as the foundation polymer. There is increasing interest in studying the synergistic effect of GO and vanillin on membrane permeability and antifouling properties. Detailed physicochemical and morphological studies were carried out using a variety of spectroscopic and microscopic methods. For 2000 ppm MgSO 4 and NaCl solutions, the improved PSf16/GO0.15-vanillin 0.8 membrane exhibited 92.5% and 25.4% rejection rates, respectively. The antifouling results indicated that BSA was rejected at a rate of over 99% and that FRR was rejected at a rate of 93.57%. The antifouling properties of the developed membranes for treating landfill leachate wastewater were tested experimentally. The findings indicated 84-90% rejection for Mg +2 and Ca +2 with a FRR of 90.32. The experiment showed that adding GO and vanillin to the polymeric matrix increases fouling resistance and membrane performance considerably. Future studies will concentrate on molecular sieving for industrial separations and other specialized applications utilizing mixed matrix membranes.
A dynamic membrane (DM) is a layer of particles deposited on a conventional membrane by permeate drag, and the deposited particles serve as a secondary membrane [77,78]. The rejected ingredients of the feed are generally produced into a cake, which is also called a DM if it improves permeate quality [79]. DMs can be divided into two types based on whether the DM is composed of feed constituents deposited during filtration or intentionally pre-deposited particles with desired properties on the primary membrane (PM) [77], namely (1) self-formed DMs, in which solid particles from wastewater form the DM and aid in improving permeate quality [80], and (2) DMs generated by the deposition of materials such as metallic compounds (particularly oxides), polymers, activated carbon, soil-based compounds, and nanoparticles on meshes or UF, MF, NF, or RO membranes. Based on their content, DMs have been divided into eight categories: metal oxides (e.g., hydrous Zr(IV) oxide, HAOPs), polymers (e.g., PAA, PVA), soil-based (e.g., kaolin, diatomite), other metallic (e.g., AlCl 3 , FeCl 3 , CaCO 3 ), activated carbon (e.g., PAC, GAC), nanoparticles (e.g., CNTs, CNFs), dual or hybrid (e.g., hydrous Zr(IV) oxide-PAA, HAOPs-PAC), and others e.g., AER, ovalbumin). The presence of DMs, which operate as an adsorbing, protecting layer against foulants, aids in the reduction of PM fouling. Figure 10 depicts a schematic describing how DMs minimize fouling by displaying the deposition of DM, the saturation of DM by foulants, and eventually the removal of the DM.

Low Pressure-Driven Membranes
The quantification and identification of relevant parameters in emerging fields is related to biofouling and preventing UF seawater membrane biofouling in membrane systems for seawater desalination [10]. Yu et al. [82] studied the effects of pH and surface charge on membrane fouling in addition to the effects of pre-ozonation during the processing of representative surface water samples (Hyde Park Recreation Lake). Although biopolymers in surface water can be removed by UF membranes, the removal rate of

Low Pressure-Driven Membranes
The quantification and identification of relevant parameters in emerging fields is related to biofouling and preventing UF seawater membrane biofouling in membrane systems for seawater desalination [10]. Yu et al. [82] studied the effects of pH and surface charge on membrane fouling in addition to the effects of pre-ozonation during the processing of representative surface water samples (Hyde Park Recreation Lake). Although biopolymers in surface water can be removed by UF membranes, the removal rate of lower MW NOM is very low, confirming the importance of membrane pore size. For the NF membrane, the removal of the smaller MW fraction (800 Da−10 kDa) is lower than expected due to its pore size; however, for all MW distributions (over 90%), almost all humic hydrophobic substances can pass through the hydrophilic NF membrane removal. The charge and hydrophilicity of NOM is a controlling factor. Hydrophilic NF membrane can remove hydrophobic organic matter but not hydrophilic matter. An increased loading effect (more negative zeta potential) and solution pH improve organic matter removal and reduce fouling (flux decrease), most likely through greater repulsive force on the membrane surface. The pre-ozonation of surface water increases the hydrophilic part and the anionic charge of NOM and changes its size distribution, resulting in less UF contamination and smaller-pore NF (less flux reduction), but the NF contamination of larger pores increased slightly. The difference in the behavior of the NF is related to the relative size of the ozonated organic components and the pores of the NF; similarly sized ozonated organic parts and NF pores can cause the significant fouling of the membrane [82]. The surface of the hydrophobic membrane can be transformed into a hydrophilic substance by (i) coating in a coating solution and (ii) the grafting (immobilization) of hydrophilic substances on its surface from grafting solutions [82,83]. Light-induced grafting functionalizes the membrane surface, provides low-cost process operations, selectively absorbs ultraviolet rays without affecting the bulk polymer, mild reaction conditions, and permanent membrane surface changes and easy chemical control [84][85][86][87].
Membrane fouling will reduce permeate flux and membrane productivity, significantly reduce membrane life, increase feed pressure, and power requirements, and increase membrane maintenance and replacement costs. Qasim et al. [88] researched different fouling mitigation strategies. Ultrasound is an effective technique that can be used for scale control and membrane cleaning. It is an effective means to increase the flow rate and clean the membrane, because it has the unique ability to produce special chemical and physical effects, which can remove the scale on the membrane surface. However, this application cannot have a significant impact on pore clogging and is limited to external fouling. Although ultrasound is effective in improving flow and cleaning membranes, it has some serious limitations, including large-scale applications, lack of suitable transducers, and lack of economic feasibility data [89]. The influence of ultrasound on membrane degradation is discussed, as well as the efficacy of this application for membranes other than the flat-sheet type and an economic analysis of ultrasound-assisted membrane processes. Figure 11 shows a microscopic image of the PES (100 kDa) membrane surface after being sonicated.
Backpulsing: In the literature, backpulsing is also referred to as backshocking [90,91], high-frequency retro filtration [92,93], and transmembrane pressure pulsing [94,95]. Backpulsing is defined by three main parameters: amplitude, duration, and frequency. The absolute value of the negative TMP during each backpulse is defined as amplitude. Each pulse's duration is measured in milliseconds. The inverse of the sum of backpulsing duration and forward filtering time is frequency [96]. It denotes the time between two successive pulses. Backpulsing volume, which is the amount of clean water utilized for each backpulse, is also of interest. Figure 12 depicts the decrease in membrane permeability in the filtration process with and without backpulsing or backwashing. and lack of economic feasibility data [89]. The influence of ultrasound on membrane degradation is discussed, as well as the efficacy of this application for membranes other than the flat-sheet type and an economic analysis of ultrasound-assisted membrane processes. Figure 11 shows a microscopic image of the PES (100 kDa) membrane surface after being sonicated. Figure 11. Microscopic image of the PES (100 kDa) membrane surface after being sonicated at 47 kHz for 2 h (a) with an 80,000 magnification; (b) a heavily damaged area with a 550 magnification [88].
Backpulsing: In the literature, backpulsing is also referred to as backshocking [90,91], high-frequency retro filtration [92,93], and transmembrane pressure pulsing [94,95]. Backpulsing is defined by three main parameters: amplitude, duration, and frequency. The absolute value of the negative TMP during each backpulse is defined as amplitude. Each pulse's duration is measured in milliseconds. The inverse of the sum of backpulsing duration and forward filtering time is frequency [96]. It denotes the time between two successive pulses. Backpulsing volume, which is the amount of clean water utilized for each backpulse, is also of interest. Figure 12 depicts the decrease in membrane permeability in the filtration process with and without backpulsing or backwashing.   Backpulsing: In the literature, backpulsing is also referred to as backshock high-frequency retro filtration [92,93], and transmembrane pressure pulsing [9 pulsing is defined by three main parameters: amplitude, duration, and freq absolute value of the negative TMP during each backpulse is defined as ampl pulse's duration is measured in milliseconds. The inverse of the sum of backp ration and forward filtering time is frequency [96]. It denotes the time betwe cessive pulses. Backpulsing volume, which is the amount of clean water utiliz backpulse, is also of interest. Figure 12 depicts the decrease in membrane perm the filtration process with and without backpulsing or backwashing. The performance of backpulsing on membrane cleaning is depicted in Figure 13. Backpulsing removes hydraulically reversible fouling and reduces concentration polarization ( Figure 13). External fouling and non-adhesive fouling are examples of hydraulically reversible fouling [98]. The mechanisms of fouling generation are used to classify external and internal fouling [99]. Fouling induced by pore constriction or pore obstruction is usually exterior fouling, whereas fouling caused by cake formation is usually internal fouling. Fouling is classified as non-adhesive or adhesive depending on the types of fouling compounds [11]. Particulate and inorganic fouling are often non-adhesive, but biofouling, colloidal, and organic fouling are typically adhesive. zation ( Figure 13). External fouling and non-adhesive fouling are examples of hydraulically reversible fouling [98]. The mechanisms of fouling generation are used to classify external and internal fouling [99]. Fouling induced by pore constriction or pore obstruction is usually exterior fouling, whereas fouling caused by cake formation is usually internal fouling. Fouling is classified as non-adhesive or adhesive depending on the types of fouling compounds [11]. Particulate and inorganic fouling are often non-adhesive, but biofouling, colloidal, and organic fouling are typically adhesive. Figure 13. Depicts an overview of the membrane prior to and after backpulsing in MF and UF processes, where CB, CS, and CP are the concentrations of solutes in the bulk, near the membrane surface, and permeate, respectively [97].
Despite the fact that experiments show that backpulsing is effective at reducing concentration polarization and preventing membrane fouling, backpulsing cleaning efficiency is determined by several factors, including:


Feeding characteristics. The types of foulants present in the feed solution have a direct impact on the types of membrane fouling. Backpulsing is more effective at removing non-adhesive and external fouling. The higher the concentration of foulants, the more severe the fouling of the membrane and the lower the cleaning efficiency of backpulsing.  Membrane characteristics. Because of the elasticity of polymeric membranes, the cleaning capability of backpulsing may be caused by membrane vibration caused by the rapid reverses of TMP rather than reverse flow. Membrane surface modification can alter the types of fouling formation, making backpulsing more effective. Furthermore, membrane pore sizes are related to membrane fouling types and backpulsing efficiency.  The operational parameters. It is critical to perform backpulsing under optimal conditions, such as amplitude, duration, and frequency. It is also advantageous to investigate the three backpulsing parameters as a backpulsing strategy. In addition, the traditional filtration parameters are TMP/flux and CFV [97].
The hydrophilic and anti-fouling PSf membrane is made by the in-situ cross-linking polymerization of AA and vinyltriethoxy (VETOS) in a polysulfone (PSf) solution and non-solvent induced phase separation. The modified doping solution with increased P (AAVETOS) concentration showed increased viscosity and decreased precipitation rate, resulting in morphological changes, from an elongated finger-like macroporous morphology to a completely sponge-like structure. When compared to a neat PSf membrane, the as-cast modified membranes had higher hydrophilicity and electronegativity, which inhibited protein adsorption and improved antifouling. Because of the cross-linked polymer networks, the modified PSf membranes have good long-term stability in hot water and Figure 13. Depicts an overview of the membrane prior to and after backpulsing in MF and UF processes, where C B , C S , and C P are the concentrations of solutes in the bulk, near the membrane surface, and permeate, respectively [97].
Despite the fact that experiments show that backpulsing is effective at reducing concentration polarization and preventing membrane fouling, backpulsing cleaning efficiency is determined by several factors, including: • Feeding characteristics. The types of foulants present in the feed solution have a direct impact on the types of membrane fouling. Backpulsing is more effective at removing non-adhesive and external fouling. The higher the concentration of foulants, the more severe the fouling of the membrane and the lower the cleaning efficiency of backpulsing. • Membrane characteristics. Because of the elasticity of polymeric membranes, the cleaning capability of backpulsing may be caused by membrane vibration caused by the rapid reverses of TMP rather than reverse flow. Membrane surface modification can alter the types of fouling formation, making backpulsing more effective. Furthermore, membrane pore sizes are related to membrane fouling types and backpulsing efficiency. • The operational parameters. It is critical to perform backpulsing under optimal conditions, such as amplitude, duration, and frequency. It is also advantageous to investigate the three backpulsing parameters as a backpulsing strategy. In addition, the traditional filtration parameters are TMP/flux and CFV [97].
The hydrophilic and anti-fouling PSf membrane is made by the in-situ cross-linking polymerization of AA and vinyltriethoxy (VETOS) in a polysulfone (PSf) solution and non-solvent induced phase separation. The modified doping solution with increased P (AAVETOS) concentration showed increased viscosity and decreased precipitation rate, resulting in morphological changes, from an elongated finger-like macroporous morphology to a completely sponge-like structure. When compared to a neat PSf membrane, the as-cast modified membranes had higher hydrophilicity and electronegativity, which inhibited protein adsorption and improved antifouling. Because of the cross-linked polymer networks, the modified PSf membranes have good long-term stability in hot water and mechanical properties. As a result of in situ cross-linked polymerization, a simple and universal method for modifying PSf membranes with high hydrophilicity and antifouling on a large scale has been developed [100].
Even in the absence of filtration, MF fouling is caused by macro solute or particle adsorption due to specific intermolecular interactions between the particles and the membrane. Because of hydrophobic interactions, hydrogen bonding, Van der Waals attractions, and extracellular macromolecular interactions, it is irreversible, and the foulants are usually adhesive. The UF fouling is a non-adhesive fouling caused by reversible filtration-induced macro solute or particle deposition, in which cells, cell debris, and other rejected particles accumulate on the top membrane surface. It manifests itself as external fouling or cake for-mation. In this respect, reversible fouling is caused by cake formation and is less dependent on membrane surface chemistry than irreversible fouling [101,102].
Ma et al. [103] reported that, while UF membranes can reportedly remove algae effectively, the removal process can cause serious fouling. A moderate pre-oxidation method (KMnO 4 Fe (II) process) is used to avoid the adverse effects of algae cells destroyed by oxidants, in order to achieve a balance between intracellular organic matter release and increased algae removal. The performance of the KMnO 4 Fe (II) pretreatment UF membrane after long-term operation in the presence of algae reservoir water shows that algae is almost completely removed, that the dirt is obviously reduced, and that the overall performance is far better than Fe(III) coagulation. The transmembrane pressure (TMP) in the Fe (III) condensation process increased to 42 kPa; however, the TMP in the KMnO 4 Fe (II) process only increased to 25.1 kPa after 90 days. The slower transmembrane pressure is attributed to the larger floc size, higher surface activity, and algae inactivation. Although it has little effect on the development of microorganisms, due to the release of extracellular polymers, the microbial abundance (20.7%) observed during the KMnO 4 Fe (II) process is lower than during the solidification alone (44.9%). The floc layer is easily washed off, and many original membrane pores can be clearly seen.
The effluent water quality is excellent, especially its turbidity, chromaticity, and Mn and Fe concentration. Based on the excellent performance of UF membranes, the KMnO 4 -Fe(II) process is applied to the water treatment of algae-containing water. Teixeira et al. [104] found that seasonal changes in the NOM content of natural surface waters in Algarve, Portugal, affect UF performance. A 47 k Da MWCO plate-and-frame polysulfone membrane can be used to evaluate the use of natural water (clean water, 35 NTU and turbid water, 33-34.6 NTU) at acidic, neutral, and alkaline pH values for seasonal pollution control on a laboratory scale pH adjustment. PH value adjustment controls seasonal UF pollution: when the water has less NOM (in dry periods, clear water), acidity will improve UF performance, and, during heavy rains (cloudy water with high NOM concentration), an alkaline pH value can minimize pollution. According to the effect of the electric charge on the size of the membrane, this behavior is explained for clear water. For cloudy water, the electrostatic repulsion between the membrane surface and NOM and turbid particles decreases at pH 4.13. The protonation of NOM functional groups reduces the hydrodynamic radius of humus and increases its hydrophobicity and adsorption tendency. At pH 4.13, a dense layer of scale will form, and the flux will be less than at pH 8.33. The observed decrease in raw water feed concentration and decrease in WRR rejection rate confirm that moderately hard water cations enhance extensive membrane adsorption. For pure water and clear water, as the pH value increases, the pores of the polysulfone membrane become more negatively charged because preferential anion adsorption reduces the membrane pore size, which reduces flux, and the rejection rate increases. The use of a PSf membrane to adjust the pH value can help seasonally control UF fouling. For clear water with low NOM content (during the Algarve's dry season), acidity increases the yield to UF, while during and after heavy rains (turbid water with high NOM concentration), alkaline pH will be beneficial.
The effect of the ultrasonic cleaning of PTFE MF membranes contaminated with a premixed humic acid bentonite mixture was studied [105]. Figure 14 depicts the set-up for dead-end MF membranes cleaning by ultrasonication. Chemical coagulation prior to MF increased the turbidity and TSS removal rate by 9.5% and 11.4%, respectively. The experimental data fitted to the constant pressure filtration model determined the order of the following main fouling mechanisms: (i) limited resistance of the membrane, (ii) limited resistance to clogging of the pores, and (iii) limited resistance to cake formation. When continuous ultrasonic cleaning is performed within 25 min of a 2.0 cm probe distance, the relative permeability of the membrane is 53 and the FRR is 45%. Continuous ultrasonic cleaning at 2.0 cm probe distance, 25 min total cleaning time, 15 mg/L coagulant dose, and 15 W ultrasonic power resulted in relative membrane permeability of 53 and flux recovery of 45 percent. Ultrasonic cleaning is effective in cleaning membranes that have been fouled by cake formation rather than those that have been fouled by pore blocking.
The efficacy of this cleaning technique is determined by the intensity and duration of ultrasound irradiation, as well as the location of the cavitation zone in relation to the fouled membrane surface. Furthermore, the pretreatment of NOM-water with iron-based coagulants and clay coagulants improves membrane filterability and facilitates ultrasonic membrane cleaning. In terms of flux recovery, ultrasonic cleaning outperforms hydraulic cleaning. In terms of mitigating NOM-induced fouling, it is a competitive and safer alternative to chemical cleaning.
following main fouling mechanisms: (i) limited resistance of the membrane, (ii) limited resistance to clogging of the pores, and (iii) limited resistance to cake formation. When continuous ultrasonic cleaning is performed within 25 min of a 2.0 cm probe distance, the relative permeability of the membrane is 53 and the FRR is 45%. Continuous ultrasonic cleaning at 2.0 cm probe distance, 25 min total cleaning time, 15 mg/L coagulant dose, and 15 W ultrasonic power resulted in relative membrane permeability of 53 and flux recovery of 45 percent. Ultrasonic cleaning is effective in cleaning membranes that have been fouled by cake formation rather than those that have been fouled by pore blocking. The efficacy of this cleaning technique is determined by the intensity and duration of ultrasound irradiation, as well as the location of the cavitation zone in relation to the fouled membrane surface. Furthermore, the pretreatment of NOM-water with iron-based coagulants and clay coagulants improves membrane filterability and facilitates ultrasonic membrane cleaning. In terms of flux recovery, ultrasonic cleaning outperforms hydraulic cleaning. In terms of mitigating NOM-induced fouling, it is a competitive and safer alternative to chemical cleaning A supported carbon nanotube/γ alumina UF membrane with built-in de-fouling capacity was constructed, described, and evaluated for its water-purification performance. Coating a carbon nanotube (CNT)/γ-alumina composite layer over a porous PbZr0.52Ti0.48O3 (PZT) piezoelectric substrate results in an asymmetric UF membrane with a pore size of 8 nm. The PZT support not only provides mechanical strength to the membrane, but it may also be utilized to create ultrasound by using an alternating voltage (AV). This, in turn, prevents and/or eliminates fouling during filtration. The conducting composite layer functions as a size-selective membrane as well as an electrode. Membrane constructions having a piezoelectric layer can be triggered with an alternating current electrical field to create ultrasound from inside. This in-situ ultrasonic emission has the potential to be highly successful in preventing or eliminating fouling during water filtration. Because γ-alumina particles efficiently filled the gap between CNTs, the inclusion of -alumina in the membrane structure was very helpful for mechanical durability and pore size reduction. Further multi-layer structure optimization, long-term stability, more environmentally acceptable (lead-free) piezoelectric compositions, scale-up, and use on tubular geometries and cost-effectiveness is needed The schematic presentation of the cross flow membrane module used for membrane operation with in-situ ultrasound generation is shown in Figure 15 [106]. A supported carbon nanotube/γ alumina UF membrane with built-in de-fouling capacity was constructed, described, and evaluated for its water-purification performance. Coating a carbon nanotube (CNT)/γ-alumina composite layer over a porous PbZr 0 . 52 Ti 0 . 48 O 3 (PZT) piezoelectric substrate results in an asymmetric UF membrane with a pore size of 8 nm. The PZT support not only provides mechanical strength to the membrane, but it may also be utilized to create ultrasound by using an alternating voltage (AV). This, in turn, prevents and/or eliminates fouling during filtration. The conducting composite layer functions as a size-selective membrane as well as an electrode. Membrane constructions having a piezoelectric layer can be triggered with an alternating current electrical field to create ultrasound from inside. This in-situ ultrasonic emission has the potential to be highly successful in preventing or eliminating fouling during water filtration. Because γ-alumina particles efficiently filled the gap between CNTs, the inclusion of -alumina in the membrane structure was very helpful for mechanical durability and pore size reduction. Further multi-layer structure optimization, long-term stability, more environmentally acceptable (lead-free) piezoelectric compositions, scale-up, and use on tubular geometries and cost-effectiveness is needed The schematic presentation of the cross flow membrane module used for membrane operation with in-situ ultrasound generation is shown in Figure 15 [106].
To assess the performance of the membranes, in-house and commercial membranes with varying characteristics were employed for humic acid separation in a circular crossflow filtering system. Seshasayee et al. [107] created the in-house membranes by including bentonite nanoclay in Mendall PVDF, PPSU, PSF, and PES polymers. Because of its capacity to generate membranes with exceptional characteristics, such as mechanical strength, wide surface areas, adsorption, antifouling, and well-defined pore morphology, bentonite nanoclay is considered a promising material for membrane applications. Three different commercial membranes were also employed to remove humic acid from water. The inhouse and commercial membranes were then evaluated in terms of morphology, surface roughness, porosity, and average pore size. When compared to other commercial and in-house membranes, the XM50 commercial membranes had smooth and uniform surface topography. The polymeric membranes' morphological structure, surface roughness, and pore size were altered by the addition of bentonite to the polymer. In a circular crossflow filtering system, pure water flux, permeate flux, and humic acid rejection were evaluated for in-house polymeric membranes and commercial membranes. The addition of bentonite nanoclay to the in-house polymeric membranes was shown to decrease humic acid fouling. To assess the performance of the membranes, in-house and commercial membranes with varying characteristics were employed for humic acid separation in a circular crossflow filtering system. Seshasayee et al. [107] created the in-house membranes by including bentonite nanoclay in Mendall PVDF, PPSU, PSF, and PES polymers. Because of its capacity to generate membranes with exceptional characteristics, such as mechanical strength, wide surface areas, adsorption, antifouling, and well-defined pore morphology, bentonite nanoclay is considered a promising material for membrane applications. Three different commercial membranes were also employed to remove humic acid from water. The inhouse and commercial membranes were then evaluated in terms of morphology, surface roughness, porosity, and average pore size. When compared to other commercial and inhouse membranes, the XM50 commercial membranes had smooth and uniform surface topography. The polymeric membranes' morphological structure, surface roughness, and pore size were altered by the addition of bentonite to the polymer. In a circular crossflow filtering system, pure water flux, permeate flux, and humic acid rejection were evaluated for in-house polymeric membranes and commercial membranes. The addition of bentonite nanoclay to the in-house polymeric membranes was shown to decrease humic acid fouling.
Shen et al.
[108] created a hybrid system comprised of several coagulation methods and UF. The properties and effects of flocs produced in various coagulation systems on UF membrane fouling control were studied ( Figure 16). Within an appropriate range of NOM content, all three coagulation methods were efficient in increasing membrane flow and lowering membrane resistance as UF pretreatment. The effectiveness of PAC on NOM removal and fouling management was significantly restricted at high starting NOM concentrations. The effect of initial NOM concentration on removing NOM and alleviating membrane fouling was slightly weakened in the PAC-PolyDMDAAC coagulation system,  Figure 16). Within an appropriate range of NOM content, all three coagulation methods were efficient in increasing membrane flow and lowering membrane resistance as UF pretreatment. The effectiveness of PAC on NOM removal and fouling management was significantly restricted at high starting NOM concentrations. The effect of initial NOM concentration on removing NOM and alleviating membrane fouling was slightly weakened in the PAC-PolyDMDAAC coagulation system, indicating that the composite flocculant PAC-PolyDMDAAC produced larger flocs through a combination of charge neutralization and adsorption bridging. Under both low and high starting NOM concentrations, the combined action of the adsorption-bridging effect, sweeping effect, and charge neutralization were the processes in the PAC + PolyDMDAAC dual-coagulation system. Although the flocs generated in the PAC + PolyDMDAAC dual-coagulation system had a lower recovery ability than those formed in the PAC and PAC-PolyDMDAAC coagulation systems, they did have a better recovery ability than those formed in the PAC and PAC-PolyDMDAAC coagulation systems. In the PAC + PolyDMDAAC dualcoagulation system, flocs produced by adsorption-bridging and sweeping had a large size and a better capacity to withstand shear force, resulting in the development of a cake layer with a porous and fluffy structure and reduced membrane pore obstruction. These findings showed that using a dual coagulation system that combines PAC coagulation and PolyDMDAAC flocculation as a pretreatment for the UF process can improve floc properties and cake layer structure, resulting in improved NOM removal and membrane fouling management.
ity than those formed in the PAC and PAC-PolyDMDAAC coagulation systems. In the PAC + PolyDMDAAC dual-coagulation system, flocs produced by adsorption-bridging and sweeping had a large size and a better capacity to withstand shear force, resulting in the development of a cake layer with a porous and fluffy structure and reduced membrane pore obstruction. These findings showed that using a dual coagulation system that combines PAC coagulation and PolyDMDAAC flocculation as a pretreatment for the UF process can improve floc properties and cake layer structure, resulting in improved NOM removal and membrane fouling management. Du et al. [109] examined the effects of Ca 2+ on membrane fouling and TrOCs removal in an electric-field-assisted MF system in the presence of Na+ alone for comparison. In the presence of Na + at 1.5 V, negatively charged bovine serum albumin (BSA) moved towards the anode, far away from the membrane surface, resulting in a 42.9% TMP decrease. In contrast, due to Ca 2+ greater charge shielding, the electrophoretic migration of BSA was restricted, resulting in a negligible influence of the electric field (1.5 V) on membrane fouling. Under 3 V of applied voltage, however, the synergistic effects of electrochemical oxidation and bridging interaction between Ca 2+ and BSA promoted the formation of denser settleable flocs and a thinner porous cake layer, alleviating membrane fouling with a 64.5% decrease in TMP and nearly 100% BSA removal ( Figure 17). The removal of TrOCs increased with voltage, reaching 29.4-80.4% at 3 V. The electric field might increase the contact time between TrOCs and the strong oxidants produced on the anode, therefore increasing TrOC elimination. The Ca +2 higher charge buffering capacity, on the other hand, diminished the electric field force and hence, reduced TrOCs elimination. Du et al. [109] examined the effects of Ca 2+ on membrane fouling and TrOCs removal in an electric-field-assisted MF system in the presence of Na+ alone for comparison. In the presence of Na + at 1.5 V, negatively charged bovine serum albumin (BSA) moved towards the anode, far away from the membrane surface, resulting in a 42.9% TMP decrease. In contrast, due to Ca 2+ greater charge shielding, the electrophoretic migration of BSA was restricted, resulting in a negligible influence of the electric field (1.5 V) on membrane fouling. Under 3 V of applied voltage, however, the synergistic effects of electrochemical oxidation and bridging interaction between Ca 2+ and BSA promoted the formation of denser settleable flocs and a thinner porous cake layer, alleviating membrane fouling with a 64.5% decrease in TMP and nearly 100% BSA removal ( Figure 17). The removal of TrOCs increased with voltage, reaching 29.4-80.4% at 3 V. The electric field might increase the contact time between TrOCs and the strong oxidants produced on the anode, therefore increasing TrOC elimination. The Ca +2 higher charge buffering capacity, on the other hand, diminished the electric field force and hence, reduced TrOCs elimination.
As the most important target of membrane separation, the inadequacy of permeability and anti-fouling frequently limits the application of the membrane in actual oily wastewater [110]. Feng et al. [111] proposed a novel concept of membrane surface construction to mitigate this intractable problem, using SiO 2 as the support layer and GO as the isolation layer ( Figure 18). The separation performance of the modified membranes for the simulated emulsion indicated the optimal co-localization percentage of the support layer (56 mg/L) and isolation layer (3.5 mg/L). The thin GO layer may efficiently prevent pollutants from entering the membrane pores while maintaining the roughness of the membrane. The GO@SiO 2 membrane could successfully perform emulsion purification with a consistent permeability (654.11 LMHB) and excellent separation efficiency due to the synergistic action of the isolation layer and support layer (99.41%). With a permeability recovery rate of 89.75% (low-density oil) and 90.41% (high-density oil) after 10 repeated cycles, the membrane's outstanding anti-fouling performance assures its long-term cycling stability. Indirectly, the storage stability proves its worth in practical applications. More significantly, the GO@SiO 2 membrane has good purification and cycle stability, making it ideal for industrial emulsion treatment (permeability recovery rate of 84.01%). As the most important target of membrane separation, the inadequacy of permeability and anti-fouling frequently limits the application of the membrane in actual oily wastewater [110]. Feng et al. [111] proposed a novel concept of membrane surface construction to mitigate this intractable problem, using SiO2 as the support layer and GO as the isolation layer ( Figure 18). The separation performance of the modified membranes for the simulated emulsion indicated the optimal co-localization percentage of the support layer (56 mg/L) and isolation layer (3.5 mg/L). The thin GO layer may efficiently prevent pollutants from entering the membrane pores while maintaining the roughness of the membrane. The GO@SiO2 membrane could successfully perform emulsion purification with a consistent permeability (654.11 LMHB) and excellent separation efficiency due to the synergistic action of the isolation layer and support layer (99.41%). With a permeability recovery rate of 89.75% (low-density oil) and 90.41% (high-density oil) after 10 repeated cycles, the membrane's outstanding anti-fouling performance assures its longterm cycling stability. Indirectly, the storage stability proves its worth in practical applications. More significantly, the GO@SiO2 membrane has good purification and cycle stability, making it ideal for industrial emulsion treatment (permeability recovery rate of 84.01%). Ceramic MF/UF membranes have made rapid progress in industrial/municipal wastewater treatment and drinking water treatment in recent decades due to their superior properties to conventional polymeric membranes. Ceramic membranes' advantageous properties include fouling resistance, high permeability, good recoverability, chemical stability, and long lifetime, which have found applications with recent advancements Figure 18. Concept of membrane surface construction to mitigate oily wastewater problem, using SiO 2 as the support layer and GO as the isolation layer [111].
Ceramic MF/UF membranes have made rapid progress in industrial/municipal wastewater treatment and drinking water treatment in recent decades due to their superior properties to conventional polymeric membranes. Ceramic membranes' advantageous properties include fouling resistance, high permeability, good recoverability, chemical stability, and long lifetime, which have found applications with recent advancements in both fabrication methods and nanotechnology. As a result, ceramic membranes hold a lot of promise in terms of potential applications in water treatment [11]. Ceramic MF/UF membranes, ceramic nanocomposite membranes, ceramic catalytic membranes, and membrane fouling are the current state of the art in ceramic membranes. Figure 19 summarizes the benefits of ceramic membranes and ceramic nanocomposite membranes in hybrid water treatment systems. Figure 18. Concept of membrane surface construction to mitigate oily wastewater problem, using SiO2 as the support layer and GO as the isolation layer [111].
Ceramic MF/UF membranes have made rapid progress in industrial/municipal wastewater treatment and drinking water treatment in recent decades due to their superior properties to conventional polymeric membranes. Ceramic membranes' advantageous properties include fouling resistance, high permeability, good recoverability, chemical stability, and long lifetime, which have found applications with recent advancements in both fabrication methods and nanotechnology. As a result, ceramic membranes hold a lot of promise in terms of potential applications in water treatment [11]. Ceramic MF/UF membranes, ceramic nanocomposite membranes, ceramic catalytic membranes, and membrane fouling are the current state of the art in ceramic membranes. Figure 19 summarizes the benefits of ceramic membranes and ceramic nanocomposite membranes in hybrid water treatment systems. Figure 19. Shows the applications and advantages of ceramic membranes and ceramic nanocomposite membranes in hybrid water treatment systems over their polymeric counterparts [112].

Engineered spacers:
Methods for controlling membrane fouling have been documented, including the invention of spacers. A spacer is often necessary to provide a flow route for the feed and permeate, to promote local mixing, and, more recently, to control membrane fouling. By increasing spacer design and geometry, these vital tasks of a spacer might be strengthened [7]. Biofouling has been seen on feed spacers, resulting in considerable axial pressure reduction. Efficient biofouling management requires a combined strategy in which spacer design improvements are applied, and enhanced hydrodynamic conditions provide a less compact biofilm that is simpler to remove [113]. Although simulation studies show that thicker and coated feed spacers might improve biofilm removal [114], other research has determined that changes to spacer geometry and hydrodynamic circumstances result in relatively few improvements in biofouling [115]. One explanation Figure 19. Shows the applications and advantages of ceramic membranes and ceramic nanocomposite membranes in hybrid water treatment systems over their polymeric counterparts [112].

Engineered spacers:
Methods for controlling membrane fouling have been documented, including the invention of spacers. A spacer is often necessary to provide a flow route for the feed and permeate, to promote local mixing, and, more recently, to control membrane fouling. By increasing spacer design and geometry, these vital tasks of a spacer might be strengthened [7]. Biofouling has been seen on feed spacers, resulting in considerable axial pressure reduction. Efficient biofouling management requires a combined strategy in which spacer design improvements are applied, and enhanced hydrodynamic conditions provide a less compact biofilm that is simpler to remove [113]. Although simulation studies show that thicker and coated feed spacers might improve biofilm removal [114], other research has determined that changes to spacer geometry and hydrodynamic circumstances result in relatively few improvements in biofouling [115]. One explanation is that, while bactericidal coatings might kill bacteria, the resultant biomass can build a layer that supports bacterial multiplication and, ultimately, biofilm formation. Furthermore, antifouling effects frequently differ in static experiments vs. active filtration, prompting suggestions for revisions in how antibacterial activities are defined [116]. The design of the spacer has been changed to decrease pressure loss, enhance local mixing, induce turbulence, and eliminate dead zones. The use of innovative spacer geometries with decreased stagnation zones, as well as the treatment of the spacer surface with a biocide agent, has been demonstrated to be successful in lowering the tendency towards biofouling. Spacers have been effectively employed in the plate-and-frame module to improve air-bubble distribution in liquid/gas streams, create turbulence, and project air bubbles toward the membrane surface for effective membrane cleaning. This biological approach is still understudied, but it has the potential to be combined with physical (new spacer geometries and turbulence-induced flow, such as two-phase flow processes or black flushing, for example) and chemical (surface modification by polymers or metallic/toxic compounds, for example) approaches. Using computational methods, the approaches may involve a combination of two or more approaches, as well as investigating optimum solutions for certain membrane systems or membrane module shapes. This might result in a comprehensive designed spacer design for fouling management in membrane systems [7].
MBR: The construction and operation of central wastewater treatment plants began in the early twentieth century. With the introduction of rigorous membrane research and development in the mid-twentieth century, an increasing number of wastewater facilities began to include an MBR in their designs. The MBR system, on the other hand, is far from flawless. Membrane systems foul continually, and if fouling occurs for an extended length of time, maintenance and cleaning expenses will grow proportionally. In MATLAB/Simulink, a fouling monitoring and prediction tool was created. The model accepts membrane fouling states and estimates membrane total resistance using deterministic and stochastic models. Using an artificial neural network technique, the tool may forecast future TMP cycles based on previous TMP performance. TMP data were created synthetically using a mathematical model that has been verified. Finally, an artificial neural network controller is used to keep temperature and MLSS within their intended ranges. The controller can reduce disturbances in both modes in a small range around their intended setpoints [117].
To enhance the economic and environmental operations of wastewater treatment facilities, optimal operational techniques have been widely used. Inadequate optimization systems, on the other hand, have been used in membrane bioreactor (MBR) plants, resulting in excessive energy consumption owing to unpredictable influent coupled with complicated biological and physical interactions connected with membrane fouling. They use process simulation to create a dual-objective optimization system based on the harmony search method. Among competing models, a bidirectional gated recurrent unit generated the most accurate forecasts of changing fluctuations in hourly influent, and the projected influent data was utilized to recommend operational methods. Using the combined biological and physical model, the optimization system looked for predicted operating methods such as aeration intensities and permeation-cleaning periods. When the permeation-cleaning time was optimized, the indicated aeration intensities were employed for scouring air on membrane surfaces. When compared to a manually run system, a prototype MBR plant outfitted with the recommended optimization system improved energy efficiency by 4% and reduced fouling by 39%. Dual-objective optimization also proved viability and dependability in a full-scale MBR plant, increasing energy efficiency by 12% and lowering fouling by 26% ( Figure 20) [118].  was prolonged by 66.7% due to the interaction between WR and A 2 O-MBR, as well as microaerobic treatment and worm predation in WR. Membrane rejection of soluble and colloidal foulants (SCF) in the combination system was reduced by 26.0% when compared to conventional A 2 O-MBR, which may be ascribed to SCF's increased biodegradability and higher bacterial activity in the combined system. Although sludge disintegration and worm predation in WR reduced floc size in A 2 O-MBR, alterations in floc surface characteristics might mitigate this detrimental effect on fouling. The interaction energy between sludge flocs and the clean/fouled membrane based on extended Derjaguin-Landau-Verwey-Overbeek (XDLVO) theory was used to investigate the complex effects of sludge flocs on membrane fouling (Figure 21). According to the energy barriers, flocs in A 2 O-MBR-WR were harder to attach to the membrane and were more likely to detach. Furthermore, high-throughput sequencing research indicated that the microbial community of the cake layer in the combined system was more even and had a larger proportion of bacteria involved in foulant breakdown, which was advantageous for fouling mitigation. The combination of A 2 O-MBR and WR has demonstrated substantial benefits in the prevention of membrane fouling. Li et al. [119] investigated a hybrid system of anaerobic-anoxic-oxic membrane bioreactor (A 2 O-MBR) and worm reactor (WR). The membrane filtration cycle in A 2 O-MBR-WR was prolonged by 66.7% due to the interaction between WR and A 2 O-MBR, as well as microaerobic treatment and worm predation in WR. Membrane rejection of soluble and colloidal foulants (SCF) in the combination system was reduced by 26.0% when compared to conventional A 2 O-MBR, which may be ascribed to SCF's increased biodegradability and higher bacterial activity in the combined system. Although sludge disintegration and worm predation in WR reduced floc size in A 2 O-MBR, alterations in floc surface characteristics might mitigate this detrimental effect on fouling. The interaction energy between sludge flocs and the clean/fouled membrane based on extended Derjaguin-Landau-Verwey-Overbeek (XDLVO) theory was used to investigate the complex effects of sludge flocs on membrane fouling ( Figure 21). According to the energy barriers, flocs in A 2 O-MBR-WR were harder to attach to the membrane and were more likely to detach. Furthermore, high-throughput sequencing research indicated that the microbial community of the cake layer in the combined system was more even and had a larger proportion of bacteria involved in foulant breakdown, which was advantageous for fouling mitigation. The combination of A 2 O-MBR and WR has demonstrated substantial benefits in the prevention of membrane fouling.  For decades, in-situ fouling management techniques for MBR have been constantly explored and may be broadly classified as biological and physicochemical approaches. However, the processes and performance of these approaches, as well as the possibilities for their use, have not been extensively addressed and compared in a systematic manner. Liu et al. [120] conducted a review of different in situ biological and physicochemical fouling control techniques in terms of fouling control performance, fouling reduction processes, and practicability. This includes a comparison of popular biological control strategies such as quorum quenching (QQ) and physicochemical approaches such as NaClO backflushing, hybrid electrochemical MBR, and anti-biofouling membrane development, as well as an examination of their potential, existing issues, and feasibility in full-scale applications. Future research should focus on creating more sustainable and broadly applicable MBR fouling reduction methods.
To cure industrial liquor condensate, a new anaerobic baffled biofilm-membrane bioreactor (AnBB-MBR) was created. At the same operational hydraulic retention duration of three days, three alternative reactor designs of R1, no media (anaerobic baffled MBR), R2: FF (fixed film AnBB-MBR), and R3: FF + MVB (fixed film and moving bed AnBB-MBR), were tested to reduce membrane fouling, Figure 22. The ceramic membranes' specific fouling rates were 0.98, 0.84, and 0.5 kPa/L/m 2 for R1: no media, R2: FF, and R3: FF + MVB, respectively. Due to biomass retention in the fixed film and the mechanical scouring of the MVB, the R2: FF and R3: FF + MVB reactors reduced membrane fouling rates by 14.1% and 48.9%, respectively, as compared to R1: no media. According to the microbial community study, the biofilm had greater relative abundances of Methanosaeta, but the suspended sludge had more Methanobacterium. Furthermore, greater humic and fulvic chemical accumulations in the system may impede methanogenic activity [121].
To cure industrial liquor condensate, a new anaerobic baffled biofilm-membrane b oreactor (AnBB-MBR) was created. At the same operational hydraulic retention duratio of three days, three alternative reactor designs of R1, no media (anaerobic baffled MBR R2: FF (fixed film AnBB-MBR), and R3: FF + MVB (fixed film and moving bed AnBB-MBR were tested to reduce membrane fouling, Figure 22. The ceramic membranes' specific fou ing rates were 0.98, 0.84, and 0.5 kPa/L/m 2 for R1: no media, R2: FF, and R3: FF + MVB respectively. Due to biomass retention in the fixed film and the mechanical scouring o the MVB, the R2: FF and R3: FF + MVB reactors reduced membrane fouling rates by 14.1% and 48.9%, respectively, as compared to R1: no media. According to the microbial com munity study, the biofilm had greater relative abundances of Methanosaeta, but the sus pended sludge had more Methanobacterium. Furthermore, greater humic and fulvi chemical accumulations in the system may impede methanogenic activity [121]. Photocatalysis is an efficient and ecologically beneficial method of decomposing or ganic contaminants, especially when sunlight is available as an energy source [122,123 Opportunities to use materials and technologies from photocatalytic pollutant degrada tion on the issue of fouling are emerging. Membrane fouling caused by organic foulant is a common issue for all membrane-based technologies and has a significant negativ influence on membrane performance. The application of photocatalysis techniques t membranes offers novel ways for membrane fouling management, which is being pur sued by an increasing number of researchers. Zhang et al. [124] summarize key develop ments in photocatalytic materials and methods in water treatment and present recent pro gress in the development of processes for the photocatalytic alleviation of membrane fou ing, including photocatalyst design and modification strategies aimed at improving pho tocatalytic efficiency, as well as different photocatalysis membrane system configuration (PMS). Photocatalysis is an efficient and ecologically beneficial method of decomposing organic contaminants, especially when sunlight is available as an energy source [122,123]. Opportunities to use materials and technologies from photocatalytic pollutant degradation on the issue of fouling are emerging. Membrane fouling caused by organic foulants is a common issue for all membrane-based technologies and has a significant negative influence on membrane performance. The application of photocatalysis techniques to membranes offers novel ways for membrane fouling management, which is being pursued by an increasing number of researchers. Zhang et al. [124] summarize key developments in photocatalytic materials and methods in water treatment and present recent progress in the development of processes for the photocatalytic alleviation of membrane fouling, including photocatalyst design and modification strategies aimed at improving photocatalytic efficiency, as well as different photocatalysis membrane system configurations (PMS).
Shen et al. [125] discussed the most recent discoveries in polymeric membranes using ZnO nanoparticles for membrane fouling prevention. The review summarizes the reports on PVDF-ZnO composite membranes, PES-ZnO composite membranes, and other composite membranes containing ZnO nanoparticles. The uses of polymer-ZnO membranes are depicted in Figure 23.

Membrane Fouling Mitigation in Membrane Distillation (MD)
Membrane distillation (MD) is a relatively new technology with enormous promise in water treatment. Despite the fact that there has been a huge lot of study done on MD over the last two decades, the long-term usage of this technique is still limited by membrane fouling [126]. The membrane surface and structure are critical to the MD unit's performance. In comparison to other membrane processes such as UF and MF, membrane requirements such as macro geometry and microstructure play a larger role in overall process performance [127]. For the MD process application, desirable membranes should be hydrophobic (nonwetting) to allow vapor passage and microporous to allow mass transfer [128]. The pores in the membrane are required to create a vapor flux. The hydrophobicity of the membrane prevents liquid entry into the pores and thus the transfer of the liquid present to the membrane permeate side [129]. Furthermore, certain membrane properties are required to prevent wetting: a small pore diameter, low surface energy on the membrane material, high roughness, a large contact angle, high surface tension of the feed solution in contact with the membrane, and thus a high LEP. The desirable properties of membranes must take into account their interdependence. In MD separation, increasing membrane thickness can increase mechanical strength while decreasing mass transfer. High porosity allows for high permeate fluxes but makes the membrane more susceptible to wetting. Shen et al. [125] discussed the most recent discoveries in polymeric membranes usin ZnO nanoparticles for membrane fouling prevention. The review summarizes the report on PVDF-ZnO composite membranes, PES-ZnO composite membranes, and other com posite membranes containing ZnO nanoparticles. The uses of polymer-ZnO membrane are depicted in Figure 23.

Membrane Fouling Mitigation in Membrane Distillation (MD)
Membrane distillation (MD) is a relatively new technology with enormous promis in water treatment. Despite the fact that there has been a huge lot of study done on MD over the last two decades, the long-term usage of this technique is still limited by mem brane fouling [126]. The membrane surface and structure are critical to the MD unit's per formance. In comparison to other membrane processes such as UF and MF, membran requirements such as macro geometry and microstructure play a larger role in overa process performance [127]. For the MD process application, desirable membranes shoul be hydrophobic (nonwetting) to allow vapor passage and microporous to allow mas transfer [128]. The pores in the membrane are required to create a vapor flux. The hydro phobicity of the membrane prevents liquid entry into the pores and thus the transfer o the liquid present to the membrane permeate side [129]. Furthermore, certain membran properties are required to prevent wetting: a small pore diameter, low surface energy o the membrane material, high roughness, a large contact angle, high surface tension of th feed solution in contact with the membrane, and thus a high LEP. The desirable propertie of membranes must take into account their interdependence. In MD separation, increasin membrane thickness can increase mechanical strength while decreasing mass transfe High porosity allows for high permeate fluxes but makes the membrane more susceptibl to wetting.
Furthermore, the increase in LEP may be related to a decrease in membrane pore size which reduces permeate flux. As a result, criteria must be established to ensure effectiv separation. Table 1 shows the typical values of the desirable properties and their effect on MD applications. Furthermore, the increase in LEP may be related to a decrease in membrane pore size, which reduces permeate flux. As a result, criteria must be established to ensure effective separation. Table 1 shows the typical values of the desirable properties and their effects on MD applications. Table 1. Desired values for the properties of the membranes used in the MD process. Adapted from [129][130][131].

Property Affects Typical Values (Commercial Membranes) Recommendation
Contact angle ( Alkhatib et al. [132] discussed and highlighted new findings on different foulants in the MD process. Furthermore, several fouling processes such as inorganic fouling, organic fouling, biological fouling, and colloidal fouling ( Figure 24) were explored to improve the understanding and prevention of membrane fouling. To create a sustainable MD process, different fouling mitigation strategies, such as pre-treatment procedures and cleaning methods ( Figure 25) were thoroughly addressed. The advantages and disadvantages of various techniques have been studied and analyzed in order to offer a comprehensive knowledge of fouling reduction in the membrane distillation process. Fouling mitigation methods for various foulants in MD have been proposed (Figure 26).
Membrane modifications break down barriers in terms of the MD process' operational limitations and explore new possibilities for recovering water from industrial effluents [131]. Water recovery from oily solutions [133], which would cause severe fouling in traditional membranes, becomes possible with modified membranes, such as those containing hydrophilic compounds. Long-term operation is enabled using fluorinated polymers, which also contribute to wetting resistance. The use of inorganic nanoparticles, siloxanes, and perfluoro polymers and GO allows for operation with complex effluents containing surfactant solutions, VOCs, and several inorganic foulants [131].
The exposition time under spinning and the dope solution used in electrospinning of MD membranes allow for the precise control of membrane porosity and thickness. Its design calls for more robust equipment than other techniques like coating [134]. On the other hand, using the dope solution entirely on the membrane surface requires less material to modify. The viscosity of the dope solution determines the drop or spinning formation, which allows the membranes to have a variety of porosities and roughnesses. To initiate chemical reactions between the membrane and the dope solution, the membrane must be pretreated to activate its structure. Electrospun membranes have a high roughness, a high hydrophobicity, a small thickness, and a high porosity. As high as possible Alkhatib et al. [132] discussed and highlighted new findings on different foulants i the MD process. Furthermore, several fouling processes such as inorganic fouling, organi fouling, biological fouling, and colloidal fouling ( Figure 24) were explored to improve th understanding and prevention of membrane fouling. To create a sustainable MD proces different fouling mitigation strategies, such as pre-treatment procedures and cleanin methods ( Figure 25) were thoroughly addressed. The advantages and disadvantages o various techniques have been studied and analyzed in order to offer a comprehensiv knowledge of fouling reduction in the membrane distillation process. Fouling mitigatio methods for various foulants in MD have been proposed ( Figure 26).    Table 1. Desired values for the properties of the membranes used in the MD process. Adapted from [129][130][131]. As high as possible Alkhatib et al. [132] discussed and highlighted new findings on different foulants the MD process. Furthermore, several fouling processes such as inorganic fouling, organ fouling, biological fouling, and colloidal fouling ( Figure 24) were explored to improve t understanding and prevention of membrane fouling. To create a sustainable MD proce different fouling mitigation strategies, such as pre-treatment procedures and cleani methods ( Figure 25) were thoroughly addressed. The advantages and disadvantages various techniques have been studied and analyzed in order to offer a comprehensi knowledge of fouling reduction in the membrane distillation process. Fouling mitigati methods for various foulants in MD have been proposed ( Figure 26).   [132]. Figure 25. Different fouling mitigation methods [132]. Membrane modifications break down barriers in terms of the MD process' operational limitations and explore new possibilities for recovering water from industrial effluents [131]. Water recovery from oily solutions [133], which would cause severe fouling in traditional membranes, becomes possible with modified membranes, such as those con- Coating is the most-researched modification technique for MD membranes, owing to its simple methodology and lack of complex equipment [135,136]. The dip-coating technique, for example, necessitates no additional equipment beyond standard laboratory equipment. It allows for a variety of modifications by varying the solution in which the membrane is immersed. The hydrophobicity of coated membranes was varied by different crosslinks created by grafting. Dip coating with inorganic nanoparticle-containing solutions has the potential to increase membrane porosity. Strongly fluorinated solutions are also used to achieve high LEPs. Vacuum filtration can produce highly homogeneous surfaces, and the sol-gel method can result in significant changes in structure and mechanical strength. However, because of the lack of control over these properties during the experimental procedure, the coating method can have a negative impact on membrane porosity and thickness. Nonetheless, the coating technique appears to be the most feasible for industrial applications because it does not require high temperatures, pressures, or energy to design the process, and it is the simplest fabrication technique among the related techniques.

Property Affects Typical Values (Commercial Membranes) Recommendation
Because of its greater complexity and the greater robustness of the resulting membranes, plasma treatment has received the least attention in the last five years [137]. Plasma does not require any pretreatments on the membrane surface and is strongly influenced by the exposure time. The membrane modification reactions occur over a short period of time. The use of various gases and attachments to generate radicals on the membrane surface results in a variety of modifications, primarily for more robust and refined separations in MD. Because it facilitates bond formation between the membrane and the modified agent, plasma is an effective strategy for enhancing other modification techniques.
A hybrid ultrasound-assisted DCMD process was designed [138] and the effect of ultrasonic irradiation in mitigating HA membrane fouling during the DCMD process was studied. Although the initial HA concentration does not affect the permeation flux characteristics within the experimental range, ultrasonic irradiation can increase the permeation flux by more than 30% without destroying the HA rejection rate, and all HA permeation concentrations are less than 0.40 mg/L. The higher the concentration factor, the greater the ultrasonic improvement of the obtained permeate flow. The effect of ultrasonic irradiation on a PTFE membrane is shown in Figure 27. When CaCl2 is added to the HA solution, it can be found that the permeation flux is severely reduced. The presence of Ca +2 will aggravate the organic pollution of HA through charge neutralization, complexation, and the formation of calcium bridges. In the absence of liquid penetrating the membrane pores, HA aggregates spread on the membrane surface to form a thick and dense HA fouling layer, which increases heat-transfer resistance and reduces the pores available for water vaporization. As a result, both permeation flux and thermal efficiency are reduced. Ultrasound brings important mechanical and thermal effects and generates powerful shock waves and micro currents at high speed. The mechanical effect promotes turbulence, reduces boundary layer, and improves color diffusion. Micro-flows, shock waves, and acoustic vortices continuously stimulate the liquid/membrane interface, thereby cooling the interface and reducing HA aggregate deposition. Under ultrasonic irradiation, although some HA contamination spreads over the membrane surface, most of the membrane pores remain open and clean. When the concentration factor reaches 4.0, the relative permeation flux can be kept at approximately When CaCl 2 is added to the HA solution, it can be found that the permeation flux is severely reduced. The presence of Ca +2 will aggravate the organic pollution of HA through charge neutralization, complexation, and the formation of calcium bridges. In the absence of liquid penetrating the membrane pores, HA aggregates spread on the membrane surface to form a thick and dense HA fouling layer, which increases heat-transfer resistance and reduces the pores available for water vaporization. As a result, both permeation flux and thermal efficiency are reduced. Ultrasound brings important mechanical and thermal effects and generates powerful shock waves and micro currents at high speed. The mechanical effect promotes turbulence, reduces boundary layer, and improves color diffusion. Micro-flows, shock waves, and acoustic vortices continuously stimulate the liquid/membrane interface, thereby cooling the interface and reducing HA aggregate deposition. Under ultrasonic irradiation, although some HA contamination spreads over the membrane surface, most of the membrane pores remain open and clean. When the concentration factor reaches 4.0, the relative permeation flux can be kept at approximately 94%. Figure 28 presents morphology images of PTFE membrane after a HA solution concentration experiment under ultrasonic irradiation with different CaCl 2 dosage [139]. and thermal efficiency are reduced. Ultrasound brings important mechanical and thermal effects and generates powerful shock waves and micro currents at high speed. The mechanical effect promotes turbulence, reduces boundary layer, and improves color diffusion. Micro-flows, shock waves, and acoustic vortices continuously stimulate the liquid/membrane interface, thereby cooling the interface and reducing HA aggregate deposition. Under ultrasonic irradiation, although some HA contamination spreads over the membrane surface, most of the membrane pores remain open and clean. When the concentration factor reaches 4.0, the relative permeation flux can be kept at approximately 94%. Figure 28 presents morphology images of PTFE membrane after a HA solution concentration experiment under ultrasonic irradiation with different CaCl2 dosage [139].
x FOR PEER REVIEW 31 of 45 Hou et al. [140] observed that, due to the formation and deposition of colloidal polysilicic acid on the membrane surface, the permeation flux gradually decreased during the concentration of the silica solution. The hollow fiber PTFE membrane maintains its mechanical properties and initial pore-size distribution under ultrasonic irradiation. Ultrasound provides important mechanical and thermal effects and generates powerful shock waves and high-speed microcurrents. Microflows, shock waves and acoustic vortices continuously stimulate the liquid/membrane interface, effectively keeping the membrane surface clean, and the permeation flux is hardly affected by increasing concentration factors. Even at the beginning of the concentration process, a large amount of silica scale is deposited on the surface of the membrane (Figure 29). Under ultrasonic irradiation, the permeation flux is stable and increased by about 43%; ultrasonic irradiation ( Figures 30  and 31) can effectively control the silica scale in the MD process [140]. Hou et al. [140] observed that, due to the formation and deposition of colloidal polysilicic acid on the membrane surface, the permeation flux gradually decreased during the concentration of the silica solution. The hollow fiber PTFE membrane maintains its mechanical properties and initial pore-size distribution under ultrasonic irradiation. Ultrasound provides important mechanical and thermal effects and generates powerful shock waves and high-speed microcurrents. Microflows, shock waves and acoustic vortices continuously stimulate the liquid/membrane interface, effectively keeping the membrane surface clean, and the permeation flux is hardly affected by increasing concentration factors. Even at the beginning of the concentration process, a large amount of silica scale is deposited on the surface of the membrane (Figure 29). Under ultrasonic irradiation, the permeation flux is stable and increased by about 43%; ultrasonic irradiation ( Figures 30 and 31 can effectively control the silica scale in the MD process [140]. factors. Even at the beginning of the concentration process, a l is deposited on the surface of the membrane (Figure 29). Under permeation flux is stable and increased by about 43%; ultraso and 31) can effectively control the silica scale in the MD proces   ysilicic acid on the membrane surface, the permeation flux gradually decreased during the concentration of the silica solution. The hollow fiber PTFE membrane maintains its mechanical properties and initial pore-size distribution under ultrasonic irradiation. Ultrasound provides important mechanical and thermal effects and generates powerful shock waves and high-speed microcurrents. Microflows, shock waves and acoustic vortices continuously stimulate the liquid/membrane interface, effectively keeping the membrane surface clean, and the permeation flux is hardly affected by increasing concentration factors. Even at the beginning of the concentration process, a large amount of silica scale is deposited on the surface of the membrane (Figure 29). Under ultrasonic irradiation, the permeation flux is stable and increased by about 43%; ultrasonic irradiation (Figures 30 and 31) can effectively control the silica scale in the MD process [140].

Ion Exchange Membrane (IEM)
Environmentally friendly processes are increasingly used in modern industry for demineralization, concentration, product modification, and energy conversion and storage [5,141]. Scale formation due to concentration polarization is a significant impediment in the ED process, particularly on the concentrate side of IEMs [142,143]. However, scale formation in the IEM will significantly reduce the efficiency of the process and increase the cost of the process. The main types of IEM scale, such as colloidal fouling, organic fouling, scale, and biological fouling, are discussed and the main factors affecting scale formation and development are considered. Colloidal fouling: Colloids are undissolved suspended solids that exist in natural water, processed water, and many wastewater streams. They exist in the form of clay minerals, colloidal silica, iron oxide, alumina, manganese oxide, organic colloids, etc. [144,145]. The diameter of the colloidal particles ranges from 10 Å to 1 µm. For example, most of the colloidal particles found in natural water are

Ion Exchange Membrane (IEM)
Environmentally friendly processes are increasingly used in modern industry for demineralization, concentration, product modification, and energy conversion and storage [5,141]. Scale formation due to concentration polarization is a significant impediment in the ED process, particularly on the concentrate side of IEMs [142,143]. However, scale formation in the IEM will significantly reduce the efficiency of the process and increase the cost of the process. The main types of IEM scale, such as colloidal fouling, organic fouling, scale, and biological fouling, are discussed and the main factors affecting scale formation and development are considered. Colloidal fouling: Colloids are undissolved suspended solids that exist in natural water, processed water, and many wastewater streams. They exist in the form of clay minerals, colloidal silica, iron oxide, alumina, manganese oxide, organic colloids, etc. [144,145]. The diameter of the colloidal particles ranges from 10 Å to 1 µm. For example, most of the colloidal particles found in natural water are small aluminum silicate clays. The diameter of these clays ranges from 0.3 to 1.0 microns. The excessive net charge on the surface of the colloid results in the adsorption of ions from the surrounding solution. Figure 32 shows the general model of the colloidal particle electrical double layer [146][147][148]. The solid surface in this model has too much positive charge, which will attract negatively charged molecules from the solution. Since the electrostatic force compensates for most of the excess positive charge, the back layer is closely attached to the solid. The ions in the diffusion layer neutralize the excess charge. The diffusion layer plays a preventive role by preventing colloids from contacting and coagulating [145].

Ion Exchange Membrane (IEM)
Environmentally friendly processes are increasingly used in modern industry for demineralization, concentration, product modification, and energy conversion and storage [5,141]. Scale formation due to concentration polarization is a significant impediment in the ED process, particularly on the concentrate side of IEMs [142,143]. However, scale formation in the IEM will significantly reduce the efficiency of the process and increase the cost of the process. The main types of IEM scale, such as colloidal fouling, organic fouling, scale, and biological fouling, are discussed and the main factors affecting scale formation and development are considered. Colloidal fouling: Colloids are undissolved suspended solids that exist in natural water, processed water, and many wastewater streams. They exist in the form of clay minerals, colloidal silica, iron oxide, alumina, manganese oxide, organic colloids, etc. [144,145]. The diameter of the colloidal particles ranges from 10 Å to 1 µm. For example, most of the colloidal particles found in natural water are small aluminum silicate clays. The diameter of these clays ranges from 0.3 to 1.0 microns. The excessive net charge on the surface of the colloid results in the adsorption of ions from the surrounding solution. Figure 32 shows the general model of the colloidal particle electrical double layer [146][147][148]. The solid surface in this model has too much positive charge, which will attract negatively charged molecules from the solution. Since the electrostatic force compensates for most of the excess positive charge, the back layer is closely attached to the solid. The ions in the diffusion layer neutralize the excess charge. The diffusion layer plays a preventive role by preventing colloids from contacting and coagulating [145]. Figure 32. Model of positively charged colloidal particle [149].
Organic fouling is similar to organic colloidal fouling, except that organic fouling initially dissolves in the ED-treated solution. Compared with ordinary organic molecules that have mainly covalent bonds, the colloidal state of organic molecules is maintained by weak long-range van der Waals attraction and electrostatic repulsion. Organic pollutants are oils, carbohydrates, proteins, aromatics, humic acids, nano/microplastics, and defoamers. These organic substances adhere to the surface of the film and/or remain on Figure 32. Model of positively charged colloidal particle [149].
Organic fouling is similar to organic colloidal fouling, except that organic fouling initially dissolves in the ED-treated solution. Compared with ordinary organic molecules that have mainly covalent bonds, the colloidal state of organic molecules is maintained by weak long-range van der Waals attraction and electrostatic repulsion. Organic pollutants are oils, carbohydrates, proteins, aromatics, humic acids, nano/microplastics, and defoamers. These organic substances adhere to the surface of the film and/or remain on the film. This type of membrane fouling is important due to the large number of processed products of different substrates that contain organic matter. There are many different strategies to prevent and control flaking during erectile dysfunction. However, the nature of the dirt must always be considered because some strategies may be applicable to one type of dirt and not be effective for another type of dirt. After that, in emergency systems containing different types of dirt, complex procedures may be involved, including the application of multiple procedures (Figure 33). the film. This type of membrane fouling is important due to the large number of processed products of different substrates that contain organic matter. There are many different strategies to prevent and control flaking during erectile dysfunction. However, the nature of the dirt must always be considered because some strategies may be applicable to one type of dirt and not be effective for another type of dirt. After that, in emergency systems containing different types of dirt, complex procedures may be involved, including the application of multiple procedures ( Figure 33).

Biofouling:
The main characteristic of these microbial cells is the presence of special bacteria on the surface of the anode. These bacteria can oxidize biodegradable substrates and produce electrons and protons. The electrons move towards the cathode to complete the electrical circuit. The anode and cathode are separated by CEM and AEM. The life

Biofouling:
The main characteristic of these microbial cells is the presence of special bacteria on the surface of the anode. These bacteria can oxidize biodegradable substrates and produce electrons and protons. The electrons move towards the cathode to complete the electrical circuit. The anode and cathode are separated by CEM and AEM. The life cycle of biofilms is shown in Figure 34, with photomicrographs of various stages of biofilm development. The initial interaction of the bacteria with the surface is reversible (1), and the subsequent adhesion is irreversible (2). After attaching to the surface of the membrane, the bacteria begin to produce and excrete extracellular polymers (2), allowing the cells to adhere to the surface. Continuous growth leads to the development of a microcolony (3). As the size of the microcolonies continues to increase (4), the cells in the microcolonies will experience crowding, reduced nutrient availability, increased excretion of waste products, increased concentrations of toxins and metabolites (including intercellular signaling molecules), and changes in their physical and chemical properties environment. Finally, the matrix is digested in the microcolonies, and the cells move freely through active movement or through browning movement (5). Eventually, a crack forms in the matrix at the edge of the microcolony, through which bacteria can escape into the large amount of surrounding fluid [149]. The types of contamination can involve complex procedures that involve the application of multiple procedures. Figure 33. Examples of organic fouling (adapted with permissions). (A) chitosan fouling anthocyanin fouling [151]; (C) protein fouling [152]; (D) polyacrylamide fouling [153].

Biofouling:
The main characteristic of these microbial cells is the presence o bacteria on the surface of the anode. These bacteria can oxidize biodegradable su and produce electrons and protons. The electrons move towards the cathode to c the electrical circuit. The anode and cathode are separated by CEM and AEM. cycle of biofilms is shown in Figure 34, with photomicrographs of various stages o development. The initial interaction of the bacteria with the surface is reversible the subsequent adhesion is irreversible (2). After attaching to the surface of the me the bacteria begin to produce and excrete extracellular polymers (2), allowing the adhere to the surface. Continuous growth leads to the development of a microco As the size of the microcolonies continues to increase (4), the cells in the micro will experience crowding, reduced nutrient availability, increased excretion o products, increased concentrations of toxins and metabolites (including intercell naling molecules), and changes in their physical and chemical properties envir Finally, the matrix is digested in the microcolonies, and the cells move freely thro tive movement or through browning movement (5). Eventually, a crack forms in trix at the edge of the microcolony, through which bacteria can escape into t amount of surrounding fluid [149]. The types of contamination can involve comp cedures that involve the application of multiple procedures.  When the salt present in the water precipitates and settles on the surface of the membrane and/or its channels, scale will form in the IEM. The main scale ions present in EDtreated solutions include magnesium, calcium, barium, bicarbonate, and sulfate [155][156][157][158][159][160][161][162] When the balance of the solution changes, precipitation occurs, making the solubility lower than the concentration of the salt, causing them to precipitate out of the solution. Generally, there are two main factors that affect precipitation in solution, ion concentration and solution temperature [156,163,164].
IEM's fouling prevention and control strategy allows fouling to be prevented and controlled during emergencies. However, the nature of fouling should always be kept in mind because a certain strategy may be suitable for one type of foulant but not for another. Subsequently, in the ED system containing different types of fouling, a complicated procedure may be involved, including the application of the following procedures: Many feed solutions for desalination contain foulants, such as organic matter of various molecular weights, suspended solids, and colloids or insoluble salt until saturated. Therefore, the feed solution needs to be pretreated to remove and reduce the concentration level to reduce the possibility of fouling, so as to achieve effective ED operation. Almost all ED systems apply the filtration of the feed solution to remove particles. However, depending on the nature of the feed solution and the water quality of the product, additional procedures such as flocculation, metal hydroxide precipitation, and ion exchange may be required.
Hydraulic, mechanical, and chemical cleaning methods are effective scale-control methods, depending on the separation process and module configuration. Chemical cleaning is the most effective CIP procedure during ED operation. Fouling can be controlled by changes in polarity during ED. When an electric field is applied to the feed solution, negatively charged particles or large organic anions migrate to the anion exchange membrane and deposit on the surface membrane. If the polarity is reversed, Figure 35 negatively charged species will migrate from the ion exchange membrane and return to the feed stream. Pulsing the electric field at an optimal frequency can reduce the fouling potential of an already dirty membrane system. It can be understood that the electrical pulse enhances the electrophoretic mobility of the charged particles in the fouling layer near the surface of the membrane, thus reducing fouling potential [153].
feed solution needs to be pretreated to remove and reduce the concentration level to reduce the possibility of fouling, so as to achieve effective ED operation. Almost all ED systems apply the filtration of the feed solution to remove particles. However, depending on the nature of the feed solution and the water quality of the product, additional procedures such as flocculation, metal hydroxide precipitation, and ion exchange may be required. Hydraulic, mechanical, and chemical cleaning methods are effective scale-control methods, depending on the separation process and module configuration. Chemical cleaning is the most effective CIP procedure during ED operation. Fouling can be controlled by changes in polarity during ED. When an electric field is applied to the feed solution, negatively charged particles or large organic anions migrate to the anion exchange membrane and deposit on the surface membrane. If the polarity is reversed, Figure 35 negatively charged species will migrate from the ion exchange membrane and return to the feed stream. Pulsing the electric field at an optimal frequency can reduce the fouling potential of an already dirty membrane system. It can be understood that the electrical pulse enhances the electrophoretic mobility of the charged particles in the fouling layer near the surface of the membrane, thus reducing fouling potential [153]. Generally, IEM modification aims to change the surface properties of the membrane, such as surface charge, hydrophobic/hydrophilic balance, and roughness. Considering the nature of the dirt, you can choose a cleaning agent to remove dirt from the surface of the IEM or prevent dirt from forming during erectile dysfunction treatment. However, rinsing by adding chemicals can have a negative impact on the performance of the membrane. For example, cleaning the IEM with an alkaline solution can lead to the degradation of the ion exchange groups. Cleaning with an oxidizing agent can cause the degradation of ion exchange groups and the polymer matrix. Also, the addition of some chemicals can have a continuous negative impact on the quality of erectile dysfunction products, which becomes very important when talking about the food industry. Generally, IEM modification aims to change the surface properties of the membrane, such as surface charge, hydrophobic/hydrophilic balance, and roughness. Considering the nature of the dirt, you can choose a cleaning agent to remove dirt from the surface of the IEM or prevent dirt from forming during erectile dysfunction treatment. However, rinsing by adding chemicals can have a negative impact on the performance of the membrane. For example, cleaning the IEM with an alkaline solution can lead to the degradation of the ion exchange groups. Cleaning with an oxidizing agent can cause the degradation of ion exchange groups and the polymer matrix. Also, the addition of some chemicals can have a continuous negative impact on the quality of erectile dysfunction products, which becomes very important when talking about the food industry.
In the development of graphene oxide nanocomposite (GO)/multi-walled carbon nanotube (MWCNT) conductive film to reduce electrical enhancement fouling, the mixed phase inversion method uses graphene oxide (GO) and multi-walled carbon nanotubes (MWCNT) to manufacture conductive films. The influence of the weight ratio of the membrane polymer: solvent and GO: MWCNTs on membrane conductivity was studied. The M10 batch of membranes exhibited moderately high conductivity due to the incorporation of carbon nanomaterials that form a continuous electron path through the membrane matrix. The electric field exerts a stronger repulsive force to repel dirt, thereby reducing the blockage of the membrane surface. Compared with the case of no electric field, the normalized fluxes of M10 (c) −5, M10 (c) −10, and M10 (c) −20 under a continuous electric field are increased by 108.14%, 90.54%, and 89.69%, respectively. A flux of 300 volts/cm. Overall, M10 (c) −5 showed the best performance due to increased conductivity without affecting other membrane properties such as pore size and surface roughness. It was found that the intermittent application of an electric field can achieve fouling mitigation similar to its continuous application [163].
The fouling of APAM towards AEM during the ED of industrial wastewater has recently received attention. Xiang et al. [164] studied the fouling dynamics using several techniques for monitoring the modification of solution and membrane characteristics. The results revealed that conductivity and pH fluctuation are less sensitive than electrochemical signals through TMEP and EIS, concentrating on micro-scale variation at/near the membrane interface. Initially, APAM deposition resulted in minimal current-transfer restrictions, as seen by the TMEP profile's plateau area. The accumulation of APAM fouling eventually hampered current transmission, resulting in an elevated TMEP due to the development of a gel layer on AEM and/or free volume obstruction. Later, water splitting occurred, as shown by an evident pH difference between the dilute and the concentrate, which may have accelerated fouling by changing the particle size of APAM. The electrochemical properties of the membrane bulk and boundary layer were effectively separated by EIS, suggesting that internal fouling is primarily responsible for the increased membrane resistance (Figure 36). Future research should focus on clarifying the external and internal fouling on IEM and investigating effective fouling mitigation techniques in the ED.
The fouling of APAM towards AEM during the ED of industrial wastewater has recently received attention. Xiang et al. [164] studied the fouling dynamics using several techniques for monitoring the modification of solution and membrane characteristics. The results revealed that conductivity and pH fluctuation are less sensitive than electrochemical signals through TMEP and EIS, concentrating on micro-scale variation at/near the membrane interface. Initially, APAM deposition resulted in minimal current-transfer restrictions, as seen by the TMEP profile's plateau area. The accumulation of APAM fouling eventually hampered current transmission, resulting in an elevated TMEP due to the development of a gel layer on AEM and/or free volume obstruction. Later, water splitting occurred, as shown by an evident pH difference between the dilute and the concentrate, which may have accelerated fouling by changing the particle size of APAM. The electrochemical properties of the membrane bulk and boundary layer were effectively separated by EIS, suggesting that internal fouling is primarily responsible for the increased membrane resistance (Figure 36). Future research should focus on clarifying the external and internal fouling on IEM and investigating effective fouling mitigation techniques in the ED.  Patil et al. [165] reviewed recent work using carbonaceous conductive membranes for fouling mitigation, contaminant degradation, permeability and selectivity enhancement, highlighting the benefits of carbonaceous conductive membranes in each and highlighting areas that we believe are promising future research directions. Future research should focus on disentangling fouling-reduction processes, overcoming mass transfer constraints and testing more relevant model systems for contaminant degradation, and identifying largescale application areas that might benefit from permselective capability. A technoeconomic study was carried out for the installation of an electric setup to an example desalination plant. According to the findings, future efforts toward commercialization should focus on increasing fouling reduction from electrification and lowering electrical energy consumption in order to justify the use of conductive carbonaceous membranes in water filtration and separation operations.
It is an urgent challenge to reduce the membrane fouling that is widely occurring in membrane-based water treatment technologies in an effective and long-lasting way. The new electrically assisted membrane coupling technology shows great potential to solve this problem. In the presence of an electric field, it can successfully repel scale, such as natural organic charges, colloids, and bacteria, from the membrane surface, thereby reducing absorption, accumulation, and clogging. More importantly, electric-field-induced microbial inactivation plays an important role in inhibiting the formation of stubborn biofilms ( Figure 37). Compared with other membrane fouling control methods such as hydrophilic surface modification, chemical cleaning, and pretreatment optimization, it shows a significant and significant effect. It still has some shortcomings. For example, the production of Joule heat can weaken the mechanical properties of the membrane, and the production of chlorine can produce disinfection by-products that are harmful to the environment. Therefore, corresponding solutions must be implemented. Successful results for reducing electrode biofilm contamination in microbial fuel cells indicate that alternating current may be an ideal choice to avoid the above-mentioned drawbacks. More research can be done to reveal the potential of AC coupled membrane systems and promote wider applications [166]. microbial inactivation plays an important role in inhibiting the formation of stubborn biofilms ( Figure 37). Compared with other membrane fouling control methods such as hydrophilic surface modification, chemical cleaning, and pretreatment optimization, it shows a significant and significant effect. It still has some shortcomings. For example, the production of Joule heat can weaken the mechanical properties of the membrane, and the production of chlorine can produce disinfection by-products that are harmful to the environment. Therefore, corresponding solutions must be implemented. Successful results for reducing electrode biofilm contamination in microbial fuel cells indicate that alternating current may be an ideal choice to avoid the above-mentioned drawbacks. More research can be done to reveal the potential of AC coupled membrane systems and promote wider applications [166].
Pretreatment: Pressure-driven membrane process: By applying the driving membrane process pressure as a pretreatment technique before ED, particles that cause a layer of fouling on the ion exchange membrane or that block the ED stack can be rejected. These filtration technologies use pressure gradients as the driving force and allow separation based on particle size or molecular weight. The general classification distinguishes pressure-driven membrane processes based on pore size and applied pressure, including MF, UF, NF, and RO. Mechanical action: The filtration process involves mechanical procedures (such as ultrasonic, vibration, air bubbles, etc.) to prevent and destroy scale. However, in Figure 37. Illustration of electro-assisted membrane coupling technology [166].
Pretreatment: Pressure-driven membrane process: By applying the driving membrane process pressure as a pretreatment technique before ED, particles that cause a layer of fouling on the ion exchange membrane or that block the ED stack can be rejected. These filtration technologies use pressure gradients as the driving force and allow separation based on particle size or molecular weight. The general classification distinguishes pressuredriven membrane processes based on pore size and applied pressure, including MF, UF, NF, and RO. Mechanical action: The filtration process involves mechanical procedures (such as ultrasonic, vibration, air bubbles, etc.) to prevent and destroy scale. However, in the ED process, mechanical cleaning is rarely used due to changes in membrane performance or even membrane degradation. Other pretreatment technologies: activated carbon, filtration, particle reactor, ultraviolet radiation, and phytoremediation.

Conclusions
This study illustrates the many forms of fouling in various membrane types, as well as the methods of both original treatment and the least-advanced technologies in treatment processes, such as introducing nanochemistry into the area of water treatment. Fouling kinds (inorganic, colloidal, organic, and biological) influence membrane productivity and morphology, resulting in lower flux rates; thus, its mitigation and avoidance are important concerns in water treatment and material science. From a chemical engineering standpoint, the main challenge of membrane modification is to combine the desired property with materials that are economically feasible using more straightforward and effective techniques. Backpulsing has been used in a variety of low-pressure membrane configurations, including flat sheet, tubular, hollow fiber, and spiral-wound membranes. Backpulsing research also encompasses a wide range of industrial fields, including water and wastewater treatment, the food industry, biotechnology applications, and others. The surface ozonation of surface water and membrane modification by coating and grafting decrease flux decline and organic fouling on NF and UF membranes. Flux recovery rose to 94.6% by DI water flushing and 100.0% by air bubbling for RO membrane pre-treatment by pH adjustment. After pretreatment with 1.1 mM EDTA in RO retentate, flux was nearly entirely recovered by physically cleaning with DI water flushing and air bubbling, as well as RO pre-treatment with ozonation. The ceramic membrane and BAC offered the optimum protection for the RO membrane, and the foulant generated from the water prepared by this combination was readily removed from the RO membrane surface by DI. Other techniques, such as pH adjustment, chemical cleaning, and backwashing, have also been considered in order to reduce the effects of CP and foulants' adsorption affinity towards the membrane surface [167].
Membranes modified using simpler methods, such as coating, will be used to mitigate MD operational problems in large-volume processes, such as desalination or water recovery from industrial discharges. Antifouling properties, resistance in long-term operations, and self-cleaning capability will be required in these cases, which may be achieved through coating. Separations involving high-value-added products that require robust membranes, on the other hand, will gravitate toward more robust techniques, such as electrospinning and plasma, wherein desirable features can be highly controlled and achieved quickly.
New membrane treatment approaches, such as the use of ultrasonic waves, the coupling of applied electric fields in membrane systems, and the creation of conductive membranes for electrically improved fouling mitigation, show great promise.