A Comprehensive Review on Membrane Fouling: Mathematical Modelling, Prediction, Diagnosis, and Mitigation
Abstract
:1. Introduction
- Feed chemistry and composition, i.e., pH, ionic strength, and foulant concentration.
- Concentration polarization (CP): CP can be broadly described as the deposition of rejected solutes on the membrane’s surface, creating a region near the membrane with spatially varying concentrations known as the polarized layer. This added resistance causes an increase in the osmotic pressure across the membrane, which decreases the driving force of the process (transmembrane pressure (TMP)), the permeate flux and the observed solute rejection, all of which increase the possibility of membrane fouling [5,7].
- Membrane properties include membrane material type, porosity, hydrophobicity, surface charges, membrane morphology, and molecular weight cut-off (MWCO).
- Process operating conditions such as temperature, pressure, aeration, permeate flux, and several other hydrodynamic conditions.
2. Membrane Foulants
2.1. Particulate Fouling
2.2. Organic Fouling
2.3. Inorganic Fouling
2.4. Biofouling
- Flux decline: as with the case of particulate fouling discussed earlier, the biofilm formation increases the resistance and reduces the permeate flux.
- Membrane biodeterioration: damage to the membrane’s structure due to acidic byproducts resulting from the microorganism’s biological activity.
- Deteriorated salt retention: inhibition of conventional transport mechanisms and increased CP effects across the membrane, due to the accumulation of dissolved salts and ions on the surface.
- Increased differential pressure: this is due to the increased resistance caused by biofilm formation.
- Higher energy requirements: the high-pressure requirements and the decline in permeate flux result in increased energy consumption.
- Frequent chemical cleaning: the cleaning process disrupts the membrane plant operation and shortens membrane life.
3. Fouling Prediction
- Pilot plant evaluation of the system’s performance;
- The use of fouling indices; and
- The use of predictive models.
3.1. Pilot Plant Evaluation of System Performance
3.2. Membrane Fouling Indices
3.2.1. Silt Density Index (SDI)
3.2.2. Modified Fouling Index (MFI)
3.2.3. Langelier Saturation Index (LSI) and Stiff and Davis Saturation Index (S&DSI)
3.2.4. Total and Dissolved Organic Carbon (TOC and DOC)
3.3. Predictive Models
4. Membrane Integrity and Fouling Diagnosis
- A thorough assessment of the malfunctioning membrane’s conductivity profiles followed by an evaluation of the extent of deviation from expected performance;
- Examination of the malfunctioning membrane’s peripheral matrix and identifying any defective components (i.e., interconnectors, end-seals, spacers, O-rings).
- External inspection: the different components that constitute the RO membrane are visually examined to diagnose the damaged zones. The core tubes, fiberglass castings, and anti-telescoping devices (ATDs) are carefully checked for potential impairments, including any obvious accumulation of foulants, crystals, scales, and biofilms [62,65,66];
- Mechanical integrity tests: several direct and indirect techniques have been developed to evaluate membrane integrity. Direct methods mainly utilize pressure-driven approaches to specify any grooves or channels in the sheets of the membrane, whereas indirect methods assess the overall integrity of the membrane’s structure [67];
- Dye test: dye testing is used to test damage to the surface of some membrane materials. Commonly used dyes include Congo Red, Methyl blue, and Rhodamine B. A fairly intense color is seen on damaged surfaces, particularly where the damage permits the access of a rather large dye molecule to the exposed surface on the porous supporting layer. If the membrane is intact, a uniformly colored stain would be observed [62,65];
- Cell test: a cell test is carried out to evaluate the performance of the malfunctioning membrane by comparing it against a new one, namely through a comparison of the differences in salt rejection and flux rates. The test is conducted by extracting an autopsied element from the defective membrane, followed by soaking it in deionized (DI) water to clean it from fouling residue and buildup, then inspecting its performance and comparing it against the standard performance of new membrane elements [62,66,68];
- Thorough analysis of the foulants: characterization techniques like scanning electron microscopy (SEM), energy dispersive X-ray (EDaX), Fujiwara oxidation testing, thermogravimetric analysis, and biological reactivity testing are commonly used to depict the membrane’s surface conditions and topography, and distinguish the different types of accumulated foulants [62,65].
5. Fouling Mitigation
5.1. Feedwater Pretreatment
5.2. Operational Conditions Optimization
5.3. Membrane Monitoring and Cleaning
- Sponge ball cleaning: this method is only applicable for tubular modules, and involves scrubbing foulants from the membrane’s surface using a sponge ball made out of polyurethane or another material [105]. The sponge ball cleaning regiment is usually utilized when the membrane is used to treat heavily polluted feedwaters like wastewater and industrial process water [105,106,107].
- Alternative flushing: this method is mostly applicable for the removal of colloidal particles from the membrane’s surface. It entails applying alternative rounds of high-pressure cross-flow water from the permeate side to the feed side and vice versa, which creates turbulence and causes the adsorbed foulants to release from the membrane [107]. It is important to optimize the forward and backward flush times to avoid compromising the membrane’s recovery efficiency, yet ensure complete cleaning cycles of the membrane modules [107,108].
- Backwashing: this method is commonly used in industries as it can retain the membrane’s flux before fouling to a very good extent. It cleans the membrane’s clogged pores by creating a negative pressure gradient across the membrane such that the applied hydraulic pressure on the permeate side exceeds the operating pressure of the module [106]. The flush creates turbulence across the membrane’s surface, loosening the foulants from the surface and out of the pores. Nonetheless, backwashing is not suitable for cleaning irreversible fouling which is characterized by clogging due to the treatment of highly concentrated colloidal solutions [106,109].
- Air flushing: this method, commonly referred to as air sparging, is more suitable for cleaning tubular and flat sheet membranes than fiber and spiral wound modules [107]. It follows the normal flushing procedure except that air is supplied to create bubbles which further augment the produced turbulence, thus enhancing the dislodgement of deposits from the membrane. It can be applied during the filtration process or scheduled periodically, as it is a rapid cleaning method that does not require chemicals and can be easily integrated into an existing membrane system. However, the effectiveness of this cleaning method is limited and the pumping requirements can be costly [110].
- Chemical cleaning: this method involves the use of chemical reagents that react with the foulants and reduce their affinity to the membrane surface, making it easier to remove these deposits. The choice of chemical agents is very important because they should not damage the membrane structure or compromise its integrity in any way. The most commonly used chemicals include acids, bases, surfactants, and chelating agents [5,69]. Low pH cleaners are mostly used to remove colloidal particulates and inorganic scales, while organic foulants and microorganisms are best removed using high pH agents [111]. Hacıfazlıoğlu et al. [112] investigated the effect of chemical cleaning on fouling control in a mini pilot-scale NF and RO system installed at a wastewater treatment plant in the ITOB Industrial Organized Zone located in Izmir/Turkey. The dual-step chemical cleaning (acid cleaning followed by alkaline cleaning) process proposed by the researchers was applied to NF and RO membranes employed for the desalination of MBR effluent discharged from a wastewater treatment plant. The study results showed that the cleaning efficiency increased with increasing cleaning contact time with chemicals.
5.4. Surface Modification and Novel Membrane Materials
5.4.1. Physical Surface Modification
5.4.2. Chemical Surface Modification
- Hydrophilization treatment: in this method, an antifouling lining is hydrophilized onto the membrane’s surface through chemical reactions with protic acids (i.e., hydrofluoric, hydrochloric, sulfuric, and nitric acids), ethanol, or 2-propanol [10,132,133]. Miyamoto et al. [134] investigated the blending of polyvinylpyrrolidone (PVP) into a polysulfone (PSf) membrane. PSf membranes are hydrophobic and are susceptible to fouling by NOM. Therefore, a hydrophilization treatment is conducted using non-solvent-induced phase separation, in which PVP is added to the PSf membrane.
- Radical grafting: in this method, free radicals are produced and then reacted with the membrane’s monomers to graft its surface. Wei et al. [135] conducted a radical grafting study in which they used 3-allyl-5,5-dimethylhydantoin (ADMH) as the grafting monomer. The modified membrane was tested for biofouling resistance in a microbial-cell suspension, where it showed augmented microbial adsorption rejection and enhanced flux rates compared to the unmodified membrane. Another study carried out by Isawi et al. [136] investigated grafting RO membranes with ZnO nanoparticles (NPs). The ZnO-NPs-grafted membrane achieved improved salt, dissolved bivalent ions (i.e., Ca2+ and SO42−), and monovalent ions (Cl− and Na+) rejection percentages of 97%, 99%, and 98%, respectively.
- Chemical coupling: this method entails reacting the active free carboxylic acid and primary amine groups on the surface of the PA-RO with chemical reagents to induce antifouling behaviors [132,137]. Hu et al. [138] covalently attached PVA to the surface of PA-TFC RO membranes. The covalent attachment of PVA resulted in improved surface hydrophilicity, enhanced salt rejection ability, and a slightly increased surface roughness. Additionally, the modification improved the membrane antifouling characteristics to a variety of foulants, including BSA and dodecyltrimethyl ammonium bromide.
- Plasma treatment: this method is further classified into plasma polymerization and plasma-induced polymerization. In the former, plasma is used to induce the accumulation of a layer of polymers onto the surface of TFC and PA-RO membranes. While, in the latter, plasma initiates the activation of oxides and/or hydroxides on the membrane’s surface, which are then involved in other polymerization methods [132,139]. A study by Safarpour et al. [140] used interfacial polymerization to synthesize TFC-RO membranes and modified them by adding dimethyl sulfoxide and glycerol. The modified membranes were characterized using SEM, FTIR, and contact angle measurements. It was reported that using dimethyl sulfoxide and glycerol as additives increased the permeate flux, surface roughness, and hydrophilicity of the membranes while maintaining the same salt rejection performance. Jahangiri et al. [141] applied the dielectric barrier discharge (DBD) plasma method to enhance the antifouling characteristics of a PA-TFC-RO membrane. The novel membrane was characterized using SEM, attenuated total reflectance FITR (ATR-FITR), and contact angle measurements, which revealed changes to the membrane’s surface morphology. ATR-FITR images showed hydrogen bonding on the surface of the modified membrane, and the contact angle measurement showed that the hydrophilicity increased, leading to a boost in surface roughness. The modified membranes had improved performance in terms of salt rejection, permeate flux, and BSA filtration. Another study by Hirsch et al. [142] modified the surface of TFC-RO membranes by combining three methods, namely, plasma activation, plasma bromination, and surface-initiated atom transfer radical polymerization (si-ATRP). Although the synthesized membranes suffered from unstable coating adhesion, the highest biofilm reduction reached was 85.4%, which is a significant enhancement.
5.4.3. Novel Membrane Materials
6. Conclusions
Author Contributions
Funding
Institutional Review Board Statement
Informed Consent Statement
Data Availability Statement
Acknowledgments
Conflicts of Interest
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Microorganism | Examples |
---|---|
Bacteria | Mycobacterium, Flavobacterium, Pseudomonas, Corynebacterium, Bacillus, Arthrobacte, Acinetobacter, Cytophaga, Moraxella, Micrococcus, Serratia, Lactobacillus, Aeromonas |
Fungi | Penicillium, Trichoderma, Mucor, Fusarium, Aspergillus |
LSI Value | Interpretation |
---|---|
<0 | Undersaturation of CaCO3 ions in the feedwater; scaling will not form. |
0 | Neutral feedwater, the index is inconclusive. |
>0 | Supersaturation of CaCO3 ions in the feedwater; scaling is highly probable. |
LSI Value | Interpretation |
---|---|
2 | Non-corrosive scaling |
0.5 | Slight corrosive scaling |
0 | Neutral, probable pitting corrosion occurrence |
−0.5 | Primitive corrosion with no scaling |
−2 | Serious corrosion |
Index | Membrane | Foulant | Filtration and Operating Mode | Test | Equation | Advantages | Limitations | Refs. |
---|---|---|---|---|---|---|---|---|
SDI | MF flat sheet 0.45 µm | Particulate matter | Dead end and constant pressure | t vs. V |
|
| [16,32,57] | |
SDI+ | MF flat sheet 0.45 µm | Particulate matter | Dead end and constant pressure | t vs. V | - | 1. Considers variation in temperature, pressure, and membrane resistance. |
| [16,32,35,57] |
SDIv | MF flat sheet 0.45 µm | Particulate matter | Dead end and constant pressure | t vs. V |
| Inaccurate results if the foulants size is smaller than 45 µm. | [16,32,35,57] | |
MFI | MF flat sheet 0.45 µm | Particulate matter | Dead end and constant pressure | t/V vs. V |
| Inaccurate results if the foulants size is smaller than 45 µm. | [16,32,57] | |
MFI-UFconst. flux | UF, flat sheet, 10-200 kDa | Colloids | Dead end and constant flux | Δp vs. t or Δt/ΔV vs. V | 1. Most industrial-scale RO filtration processes are constant flow processes. |
| [16,32,57] | |
NF-MFI | NF | Organic matter | Dead end and constant pressure | t/(V/A) vs. V/A | 1. Able to filter out the organic matter. |
| [16,32,57] | |
CFS-MFI | MF, UF, and NF | Particulate matter | Crossflow, dead-end, and constant pressure | t/V vs. V |
| Operating under constant pressure. | [16,32,57,58] | |
CFI | MF and NF | All types of foulants | Constant pressure | t/V vs. V |
|
| [16,32,57] | |
LSI | All membranes | CaCO3 | - | - |
| Does not quantify how much scale or calcium carbonate would precipitate at equilibrium conditions. | [16,32,57,59] | |
S&DSI | All membranes | CaCO3 | - | - |
| Inconsiderate of the precipitation reaction kinetics thus fails to consider the induction time required for precipitate formation. | [16,32,57,59] | |
SI | All membranes | CaCO3, CaSO4, BaSO4 and SiO2 | - | - |
| Ksp value is very sensitive to changes in operative parameters or to the presence of contaminants/impurities. | [16] | |
MMAS | MF, UF, and NF | Particulate, colloids and organic matter | Dead end and constant pressure | t/V vs. V | - |
|
| [32,60] |
DFI | MF flat sheet 0.45 µm | Particulate matter | Dead end and constant pressure | t/V vs. V |
| more accuracy and reliability tests are needed to validate the test | [32,61] |
Model | Characteristics | Equation |
---|---|---|
1 | Standard blocking, intermediate pore blockage, and cake formation | |
2 | Standard blocking, complete pore blockage, and cake formation (using the Hagen–Poiseuille law) | |
3 | Standard blocking, intermediate pore blockage, and cake formation (using the Hagen–Poiseuille law) | |
4 | Zero-order standard blocking, complete pore blockage, cake formation | |
5 | Zero-order standard blocking, intermediate pore blockage, and cake formation |
Monitoring Technique | Membrane | Mode | Description | Advantages | Limitations | Refs. |
---|---|---|---|---|---|---|
Pressure decay test | MF, UF, and NF | Offline | The pressure test uses a low-pressure air supply that is applied to the permeate side of the membrane. If the membrane’s integrity is compromised or suffers from leak spots; air would pass through. The air transfer would occur only if the applied pressure exceeds the defected site’s bubble point pressure. | 1. Suitable for a wide array of membranes; from RO to MF, and a vast range of configurations; including hollow fibers, tubular and flat sheets. |
| [90,92,93] |
Vacuum decay test | NF and RO | Offline | The membrane element is placed into a clean water bath for several hours, then drained. The permeate tube is plugged then a vacuum is applied to measure vacuum decay rates. If the decay rate exceeds 10kPa/min, then the membrane’s integrity is compromised. | 1. Suitable for a wide array of membranes; from RO to MF, and a vast range of configurations; including hollow fibers, tubular and flat sheets. | 1. Applicable to separate elements in a system, not to the full system. | [67,90,92] |
Particles tracking | MF and UF | Online | The concentration of a specific particle is tracked in both the feed and the permeate. | 1. Simple and rapid solution for membrane fouling analysis. |
| [92,94] |
Turbidity monitoring | MF and UF | Online | Turbidity levels are measured in both the feed and the permeate. | 1. Simple and rapid solution for membrane fouling analysis. |
| [95,96] |
TOC monitoring | NF and RO | Online | TOC concentrations are measured in both the feed and the permeate. | 1. Suitable for a wide array of membranes; from RO to NF, and a vast range of configurations; including hollow fibers, tubular and flat sheets. Applicable to full-scale setups. | Expensive equipment. | [92,93,97] |
Sulfate tracking | NF and RO | Offline | Sulfate concentrations are measured in both the feed and the permeate. | 1. Suitable for a wide array of membranes; from RO to NF, and a vast range of configurations; including hollow fibers, tubular and flat sheets. Applicable to full-scale setups. | Expensive equipment. | [67] |
Conductivity monitoring | NF and RO | Online | The conductivity is monitored in both the feed and the permeate. | Can assess the performance of critical control points. | Time-consuming. | [97,98] |
Marker-based test (challenge test or seeding method) | MF, UF, NF, and RO | Offline | The feed is supplemented by microorganisms which are then tracked to the permeate. | 1. Assesses viruses’ removal efficiency New markers, like fluorescence-tagged nanoparticles, can provide high-resolution results. | 1. Requires seeding. Expensive. | [67,91] |
Pulse integrity test | NF and RO | Online | The pulse of a highly rejected particle, i.e., magnesium sulfate is measured and monitored. |
| 1. Unsuitable for NF membranes as the elements themselves have substantial conductivity which can alter the accuracy of the test’s results. | [67,91] |
Fluorescence excitation-emission matrix spectroscopy | NF and RO | Online | The concentration of microspheres in both the feed and the permeate is measured by fluorescence spectroscopy. | Up to 4 log10 removal reported.Results can be cross-checked with conductivity-based tests. | 1. Expensive due to the cost of particles. | [91,98] |
Flow cytometry | NF and Ro | Offline | An optical analysis approach to quantify and characterize cells in a liquid matrix. | 1. Highly sensitive, thus accurate and can detect a wide range of membrane integrity problems. |
| [91,99] |
Conventional Pretreatment Method | Advantages | Disadvantages |
---|---|---|
Coagulation/flocculation |
|
|
Chlorination |
|
|
Media filtration |
|
|
Acidification |
|
|
Ozonation | 1. Does not affect the integrity of the feed in terms of odor or taste. |
|
DAF | 1. Cost-effective. | 1. Scraper-related issues. |
Scale inhibitors | 1. Inhibits crystallization-induced scale formation. | 1. Overdosing of scale inhibitors can cause detrimental damage to RO membranes. |
UV |
| 1. Can lead to biofilm formation. |
Aspect of Comparison | Conventional Pretreatment Methods | Membrane Pretreatment Methods |
---|---|---|
Capital cost | lower than non-conventional membrane-based methods | Higher than conventional methods but new developments are causing costs to decline. |
Carbon footprint | High | Low |
Energy requirements | Low | High |
Chemical costs | High | Low |
Quality of permeate | SDI < 4 for 90% of the time inconsistent quality indicators. Turbidity: <1.0 NTU. | SDI < 2.5 for 100% of the time. Constant quality indicators. Turbidity < 0.1 NTU. |
Method | Modifier | Test Conditions | Permeate Flux (Lm−2 h−1) | Salt Rejection (%) | Ref. |
---|---|---|---|---|---|
Surface coating | PDDA and PSS | 2000 ppm NaCl solution at 4.1 MPa | 15.5 | 99 | [122] |
LbL surface coating | Pluronic F127 amphiphilic triblock copolymer | 2 g/L NaCl solution at 4 MPa | 30 | 94 | [123] |
LbL surface coating | PEI and GO | 200 g/L NaCl at 65 °C | 8.4 kg m−2 h−1 | 99.9 | [124] |
Surface coating | SPVA | 2000 ppm NaCl solution at 1.55 MPa | 42.6 | 99.18 | [125] |
Surface coating | Pluronic F127 and Gum arabic | 2000 mg/L NaCl solution at 55.2 bar | - | 98 | [126] |
Slip casting | Nano zeolite-Y | 25,000 mg/L NaCl solution at 25 bar | 5.1 | 99.52 | [127] |
Spin coating | GO | 1 mg/mL NaCl solution at 1.5 MPa and 25 °C | - | 95.3 | [128] |
Surface coating | GO | - | 1356 | 37 | [129] |
Surface coating | PEGDA | 2000 ppm NaCl solution at 20 bar and 25 °C | - | 99 | [130] |
Cation complexation | PEG | 2000 ppm NaCl solution at 1.55 MPa | 40.8 | 99.04 | [131] |
Hydrophilization treatment | PVP | - | - | - | [134] |
Hydrophilization treatment | Chromic acid | 60 °C | 61 | - | [148] |
Free radical grafting | ADMH | 2000 ppm NaCl solution at 1.5 MPa and 25 °C | 184.5 | 95.8 | [135] |
Free radical grafting | ZnO NPs | 2000 mg/l NaCl solution at 15 bar and 25 °C | 35 | 97 | [136] |
Radical grafting | ADMH | 35mM NaCl solution at 27.6 bar and 22 °C | - | 99.1 | [149] |
Chemical coupling | PVA | 500 mg/L NaCl solution at 5 bar and 25 °C | 27 | 98.46 | [138] |
Chemical coupling | Aldehydes | 2000 ppm NaCl solution at 1.6MPa and 25 °C | 37.5 | 98.6 | [150] |
Glow discharge plasma treatment | Clinoptilolite | 16,000 ppm NaCl solution at 1.5 MPa and 25 °C | - | 97.12 | [140] |
Dielectric barrier discharge plasma treatment | - | - | - | - | [141] |
Plasma polymerization and si-ATRP | HEMA, MPC, and SBMA | - | 6042 | 99 | [142] |
Modifier | Test Conditions | Permeate flux (Lm−2 h−1) | Salt rejection (%) | Ref. |
---|---|---|---|---|
Carboxylated CNT | 2000 mg/L NaCl and 500 mg/L BSA solutions at 15 bar and 25 °C | - | 94 | [151] |
CNT | 2000 mg/L NaCl solution at 15 bar and 25 °C | 25.9 | 96 | [145] |
CNT | 2000 mg/L NaCl solution at 15.5 bar | 128.6 | 98.3 | [152] |
Magnetic multi-walled CNT | 2 g/L NaCl, 2 g/L Na2SO4, 2 g/L MgSO4 solutions at 1 MPa and 25 °C | 11.39 (NaCl), 10.84 (Na2SO4) and 11.10 (MgSO4) | 97.04 (NaCl), 96 (Na2SO4) and 95.31 (MgSO4) | [153] |
CNT | 25,000 ppm NaCl solution at 24 bar | 1.78 | 99.91 | [154] |
Zwitterionic diamine monomer N-aminoethyl piperazine | 2000 ppm NaCl solution at 1.5 MPa and 25 °C | 54.5 | 98.3 | [155] |
Zwitterionic colloid nanoparticles | 2000 ppm NaCl solution at 1.5 MPa and 25 °C | 37.3 | 96.5 | [156] |
Zwitterionic polymer | 0.85 wt% NaCl solution at 1.5 MPa and 30 °C | 50.48 | 96.9 | [157] |
Zwitterionic monomer | 2000 ppm NaCl solution at 15 bar and 25 °C | 24.75 | 98.5 | [158] |
Zwitterionic GO | 1000 ppm NaCl solution at 12 bar | 17.52 | 94.8 | [159] |
TiO2 NPs | 2000 ppm NaCl solution at 1.52 MPa and 65 °C | 24.3 | 97 | [160] |
GO-ZnO | 2000 mg/L NaCl solution at 20 bar and 25 °C | 31.42 | 96.3 | [146] |
N-GOQD | 2000 ppm NaCl solution at 15 bar | 24.9 | 93 | [147] |
ZIF-8 | 2 g/L NaCl solution at 15.5 bar and 25 °C | 51.925 | 98.5 | [161] |
Fe NPs and Cu NPs | 1000mg/L NaCl solution at 300 psi and 25 °C | 8.4 (Fe NPs) and 3 (Cu NPs) | 92.96 (Fe NPs) and 74.36 (Cu NPs) | [162] |
palygorskite-chitin (PAL-CH) hybrid nanomaterial | 2000 ppm NaCl solution at 15 bar | 2.4 | 93, 95, 98.5, and 96.6 for PA/PSF-PAL-CH1, PA/PSF-PAL-CH2, PA/PSF-PAL-CH3 and PA/PSF-PAL-CH4 | [163] |
GO | 800 mg/L CaCl2 and Na2SO4 at 25℃ and 20 bar | - | 98 | [164] |
zirconium metal–organic cages | 2000 ppm NaCl at 25 °C and 15.5 bar | 22.79 | 94.7 | [165] |
dZIF-8 | 2000 ppm NaCl solution at 20 bar (brackish water) and 32,000 ppm NaCl at 50 bar (seawater) | 52.2 (brackish water), 38 (seawater) | 98.6 (brackish water), 98.8 (seawater) | [166] |
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AlSawaftah, N.; Abuwatfa, W.; Darwish, N.; Husseini, G. A Comprehensive Review on Membrane Fouling: Mathematical Modelling, Prediction, Diagnosis, and Mitigation. Water 2021, 13, 1327. https://doi.org/10.3390/w13091327
AlSawaftah N, Abuwatfa W, Darwish N, Husseini G. A Comprehensive Review on Membrane Fouling: Mathematical Modelling, Prediction, Diagnosis, and Mitigation. Water. 2021; 13(9):1327. https://doi.org/10.3390/w13091327
Chicago/Turabian StyleAlSawaftah, Nour, Waad Abuwatfa, Naif Darwish, and Ghaleb Husseini. 2021. "A Comprehensive Review on Membrane Fouling: Mathematical Modelling, Prediction, Diagnosis, and Mitigation" Water 13, no. 9: 1327. https://doi.org/10.3390/w13091327
APA StyleAlSawaftah, N., Abuwatfa, W., Darwish, N., & Husseini, G. (2021). A Comprehensive Review on Membrane Fouling: Mathematical Modelling, Prediction, Diagnosis, and Mitigation. Water, 13(9), 1327. https://doi.org/10.3390/w13091327