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Water desalination

Nanofiltration is a relatively recent membrane filtration process used most often with low total dissolved solids water such as surface water and fresh groundwater, with the purpose of softening and removal of disinfection by-product precursors such as natural organic matter and synthetic organic matter.


Nanofiltration is a membrane filtration-based method that uses nanometer sized through-pores that pass through the membrane. Nanofiltration membranes have pore sizes from 1-10 nanometers, smaller than that used in microfiltration and ultrafiltration, but just larger than that in reverse osmosis. Membranes used are predominantly created from polymer thin films.[1] Materials that are commonly used include polyethylene terephthalate or metals such as aluminum.[2] Pore dimensions are controlled by pH, temperature and time during development with pore densities ranging from 1 to 106 pores per cm2. Membranes made from polyethylene terephthalate and other similar materials, are referred to as "track-etch" membranes, named after the way the pores on the membranes are made.[3] "Tracking" involves bombarding the polymer thin film with high energy particles. This results in making tracks that are chemically developed into the membrane, or "etched" into the membrane, which are the pores. Membranes created from metal such as alumina membranes, are made by electrochemically growing a thin layer of aluminum oxide from aluminum metal in an acidic medium.

Range of applications[edit]

Historically, nanofiltration and other membrane technology used for molecular separation was applied entirely on aqueous systems. The original uses for nanofiltration were water treatment and in particular water softening. Nanofilters can "soften" water by retaining scale-forming, hydrated divalent ions (e.g. Ca2+, Mg2+) while passing smaller hydrated monovalent ions.[4][5]

In recent years, the use of nanofiltration has been extended into other industries such as milk and juice production. Research and development in solvent-stable membranes has allowed the application for nanofiltration membranes to extend into new areas such as pharmaceuticals, fine chemicals, and flavour and fragrance industries.[4]

Industry Uses
Fine chemistry and Pharmaceuticals Non-thermal solvent recovery and management

Room temperature solvent exchange

Oil and Petroleum chemistry Removal of tar components in feed

Purification of gas condensates

Bulk Chemistry Product Polishing

Continuous recovery of homogeneous catalysts

Natural Essential Oils and similar products Fractionation of crude extracts

Enrichment of natural compounds Gentle Separations

Medicine Able to extract amino acids and lipids from blood and other cell culture.

Advantages and disadvantages[edit]

One of the main advantages of nanofiltration as a method of softening water is that during the process of retaining calcium and magnesium ions while passing smaller hydrated monovalent ions, filtration is performed without adding extra sodium ions, as used in ion exchangers.[6] Many separation processes do not operate at room temperature (e.g. distillation), which greatly increases the cost of the process when continuous heating or cooling is applied. Performing gentle molecular separation is linked with nanofiltration that is often not included with other forms of separation processes (centrifugation). These are two of the main benefits that are associated with nanofiltration. Nanofiltration has a very favorable benefit of being able to process large volumes and continuously produce streams of products. Still, Nanofiltration is the least used method of membrane filtration in industry as the membrane pores sizes are limited to only a few nanometers. Anything smaller, reverse osmosis is used and anything larger is used for ultrafiltration. Ultrafiltration can also be used in cases where nanofiltration can be used, due to it being more conventional. A main disadvantage associated with nanotechnology, as with all membrane filter technology, is the cost and maintenance of the membranes used.[7] Nanofiltration membranes are an expensive part of the process. Repairs and replacement of membranes is dependent on total dissolved solids, flow rate and components of the feed. With nanofiltration being used across various industries, only an estimation of replacement frequency can be used. This causes nanofilters to be replaced a short time before or after their prime usage is complete.

Design and operation[edit]

Industrial applications of membranes require hundreds to thousands of square meters of membranes and therefore an efficient way to reduce the footprint by packing them is required. Membranes first became commercially viable when low cost methods of housing in 'modules' were achieved.[8] Membranes are not self-supporting. They need to be stayed by a porous support that can withstand the pressures required to operate the NF membrane without hindering the performance of the membrane. To do this effectively, the module needs to provide a channel to remove the membrane permeation and provide appropriate flow condition that reduces the phenomena of concentration polarisation. A good design minimises pressure losses on both the feed side and permeate side and thus energy requirements. Leakage of the feed into the permeate stream must also be prevented. This can be done through either the use of permanent seals such as glue or replaceable seals such as O-rings.[9]

Concentration polarisation[edit]

Concentration polarisation describes the accumulation of the species being retained close to the surface of the membrane which reduces separation capabilities. It occurs because the particles are convected towards the membrane with the solvent and its magnitude is the balance between this convection caused by solvent flux and the particle transport away from the membrane due to the concentration gradient (predominantly caused by diffusion.) Although concentration polarisation is easily reversible, it can lead to fouling of the membrane.[9][10]

Spiral wound module[edit]

Spiral wound modules are the most commonly used style of module and are 'standardized' design, available in a range of standard diameters (2.5", 4" and 8") to fit standard pressure vessel that can hold several modules in series connected by O-rings. The module uses flat sheets wrapped around a central tube. The membranes are glued along three edges over a permeate spacer to form 'leaves'. The permeate spacer supports the membrane and conducts the permeate to the central permeate tube. Between each leaf, a mesh like feed spacer is inserted.[10][11] The reason for the mesh like dimension of the spacer is to provide a hydrodynamic environment near the surface of the membrane that discourages concentration polarisation. Once the leaves have been wound around the central tube, the module is wrapped in a casing layer and caps placed on the end of the cylinder to prevent 'telescoping' that can occur in high flow rate and pressure conditions.

Tubular module[edit]

Tubular modules look similar to shell and tube heat exchangers with bundles of tubes with the active surface of the membrane on the inside. Flow through the tubes is normally turbulent, ensuring low concentration polarisation but also increasing energy costs. The tubes can either be self-supporting or supported by insertion into perforated metal tubes. This module design is limited for nanofiltration by the pressure they can withstand before bursting, limiting the maximum flux possible.[8][9] Due to both the high energy operating costs of turbulent flow and the limiting burst pressure, tubular modules are more suited to 'dirty' applications where feeds have particulates such as filtering raw water to gain potable water in the Fyne process. The membranes can be easily cleaned through a 'pigging' technique with foam balls are squeezed through the tubes, scouring the caked deposits.[12]

Flux enhancing strategies[edit]

These strategies work to reduce the magnitude of concentration polarisation and fouling. There is a range of techniques available however the most common is feed channel spacers as described in spiral wound modules. All of the strategies work by increasing eddies and generating a high shear in the flow near the membrane surface. Some of these strategies include vibrating the membrane, rotating the membrane, having a rotor disk above the membrane, pulsing the feed flow rate and introducing gas bubbling close to the surface of the membrane.[9][10][11]


Many different factors must be taken into account in the design of NF membranes, since they vary so much in material, separation mechanisms, morphology and thus application. Two important parameters should be investigated during preliminary calculations, performance and morphology parameters.

Performance parameters[edit]

Retention of both charged and uncharged solutes and permeation measurements can be categorised into performance parameters since the performance under natural conditions of a membrane is based on the ratio of solute retained/ permeated through the membrane.

For charged solutes, the ionic distribution of salts near the membrane-solution interface plays an important role in determining the retention characteristic of a membrane. If the charge of the membrane and the composition and concentration of the solution to be filtered is known, the distribution of various salts can be found. This in turn can be combined with the known charge of the membrane and the Gibbs–Donnan effect to predict the retention characteristics for that membrane.[9]

Uncharged solutes cannot be characterised simply by Molecular Weight Cut Off (MWCO,) although in general an increase in molecular weight or solute size leads to an increase in retention. The valence charge, chemical structure, functional end-groups as well as pH of the solute, all play an important role in determining the retention characteristics and as such detailed information about the solute molecule characteristics must be known before implementing a NF design.[1]

Morphology parameters[edit]

The morphology of a membrane must also be known in order to implement a successful design of a NF system, and this is usually done by microscopy. Atomic force microscopy (AFM) is one method used to characterise the surface roughness of a membrane by passing a small sharp tip (<100 Ă) across the surface of a membrane and measuring the resulting Van der Waals force between the atoms in the end of the tip and the surface.[9] This is useful as a direct correlation between surface roughness and colloidal fouling has been developed. Correlations also exist between fouling and other morphology parameters, such as hydrophobe, showing that the more hydrophobic a membrane is, the less prone to fouling it is. See membrane fouling for more information.

Methods to determine the porosity of porous membranes have also been found via permporometry, making use of differing vapour pressures to characterise the pore size and pore size distribution within the membrane. Initially all pores in the membrane are completely filled with a liquid and as such no permeation of a gas occurs, but after reducing the relative vapour pressure some gaps will start to form within the pores as dictated by the Kelvin equation. Polymeric (non-porous) membranes cannot be subjected to this methodology as the condensable vapour should have a negligible interaction within the membrane.[9]

Solute transport and rejection[edit]

Mechanisms through which solutes in nanofiltration transport through the membrane.[1]

Unlike membranes with larger and smaller pore sizes, passage of solutes through nanofiltration is significantly more complex.

Because of the pore sizes, there are three modes of transport of solutes through the membrane. These include 1) diffusion (molecule travel due to concentration potential gradients, as seen through reverse osmosis membranes), 2) convection (travel with flow, like in larger pore size filtration such as microfiltration), and 3) electromigration (attraction or repulsion from charges within and near the membrane).

Additionally, the exclusion mechanisms in nanofiltration are more complex than in other forms of filtration. Most filtration systems operate solely by size (steric) exclusion, but at small length scales seen in nanofiltration, one must also consider the impacts of surface charge on the small charged solutes, and also the impacts of hydration, where molecules in solution have a solvation shell of surrounding water molecules. The exclusion due to hydration is referred to as dielectric exclusion, a reference to the different dielectric constants (energy) associated with a particles precense in solution versus within a membrane substrate. Solution pH strongly impacts surface charge,[13] providing a method to understand and better control rejection.

Primary rejection mechanisms that prevent solutes from entering the pores in nanofiltration.[1]

The transport and exclusion mechanisms are heavily influenced by membrane pore size, solvent viscosity, membrane thickness, solute diffusivity, solution temperature, solution pH, and membrane dielectric constant. The pore size distribution is also important. Modeling rejection accurately for NF is very challenging. It can be done with applications of the Nernst–Planck equation, although a heavy reliance on fitting parameters to experimental data is usually requried.[1]

In general, charged solutes are much more effectively rejected in NF than uncharged solutes, and multivalent solutes like SO2−
(valence of 2) experience very high rejection.

Typical figures for industrial applications[edit]

Keeping in mind that NF is usually part of a composite system for purification, a single unit is chosen based on the design specifications for the NF unit. For drinking water purification many commercial membranes exist, coming from different chemical families, having different structures, chemical tolerances and salt rejections and so the characterisation must be chosen based on the chemical composition and concentration of the feed stream.

NF units in drinking water purification range from extremely low salt rejection (<5% in 1001A membranes) to almost complete rejection (99% in 8040-TS80-TSA membranes.) Flow rates range from 25–60 m3/day for each unit, so commercial filtration requires multiple NF units in parallel to process large quantities of feed water. The pressures required in these units are generally between 4.5-7.5 bar.[9]

For seawater desalination using a NF-RO system a typical process is shown below.

Process diagram nanofiltration-desalination

Because of the fact that NF permeate is rarely clean enough to be used as the final product for drinking water and other water purification, is it commonly used as a pre treatment step for reverse osmosis (RO)[7] as is shown above.


As with other membrane based separations such as ultrafiltration, microfiltration and reverse osmosis, post-treatment of eitherpermeate or retentate flow streams (depending on the application) – is a necessary stage in industrial NF separation prior to commercial distribution of the product. The choice and order of unit operations employed in post-treatment is dependent on water quality regulations and the design of the NF system. Typical NF water purification post-treatment stages include aeration and disinfection & stabilisation.


A Polyvinyl chloride (PVC) or fibre-reinforced plastic (FRP) degasifier is used to remove dissolved gases such as carbon dioxide and hydrogen sulfide from the permeate stream.[14] This is achieved by blowing air in a countercurrent direction to the water falling through packing material in the degasifier. The air effectively strips the unwanted gases from the water.

Disinfection and stabilisation[edit]

The permeate water from a NF separation is demineralised and may be disposed to large changes in pH, thus providing a substantial risk of corrosion in piping and other equipment components. To increase the stability of the water, chemical addition of alkaline solutions such as lime and caustic soda is employed. Furthermore, disinfectants such as chlorine or chloroamine are added to the permeate, as well as phosphate or fluoride corrosion inhibitors in some cases.[14]

New developments[edit]

Contemporary research in the area of Nanofiltration (NF) technology is primarily concerned with improving the performance of NF membranes, minimising membrane fouling and reducing energy requirements of already existing processes. One way in which researchers are attempting to improve NF performance – more specifically increase permeate flux and lower membrane resistance – is through experimentation with different membrane materials and configurations. thin film composite membranes (TFC), which consist of a number of extremely thin selective layers interfacially polymerized over a microporous substrate, have had the most commercial success in industrial membrane applications due to the capability of optimizing the selectivity and permeability of each individual layer.[15] Recent research has shown that the addition of nanotechnology materials such as electrospunnanofibrous membrane layers (ENMs) to conventional TFC membranes results in an enhanced permeate flux. This has been attributed to inherent properties of ENMs that favour flux, namely their interconnected pore structure, high porosity and low transmembrane pressure.[16] A recently developed membrane configuration which offers a more energy efficient alternative to the commonly used spiral wound arrangement is the hollow fibre membrane. This format has the advantage of requiring significantly less pre-treatment than spiral wound membranes, as solids introduced in the feed are displaced effectively during backwash or flushing.[17] As a result, membrane fouling and pre-treatment energy costs are reduced. Extensive research has also been conducted on the potential use of Titanium Dioxide (TiO2, titania) nanoparticles for membrane fouling reduction. This method involves applying a nonporous coating of titania onto the membrane surface. Internal fouling/pore blockage of the membrane is resisted due to the nonporosity of the coating, whilst the superhydrophilic nature of titania provides resistance to surface fouling by reducing adhesion of emulsified oil on the membrane surface.[18]

See also[edit]


  1. ^ a b c d e Roy, Yagnaseni; Warsinger, David M.; Lienhard, John H. (2017). "Effect of temperature on ion transport in nanofiltration membranes: Diffusion, convection and electromigration". Desalination. 420: 241–257. doi:10.1016/j.desal.2017.07.020. hdl:1721.1/110933. ISSN 0011-9164.
  2. ^ Baker, L.A.; Martin (2007). "Nanotechnology in Biology and Medicine: Methods, Devices and Applications". Nanomedicine: Nanotechnology, Biology and Medicine. 9: 1–24.
  3. ^ Apel, P.Yu; et al. (2006). "Structure of Polycarbonate Track-Etch: Origin of the "Paradoxical" Pore Shape". Journal of Membrane Science. 282 (1): 393–400. doi:10.1016/j.memsci.2006.05.045.
  4. ^ a b Rahimpour, A; et al. (2010). "Preparation and Characterisation of Asymmetric Polyethersulfone and Thin-Film Composite Polyamide Nanofiltration Membranes for Water Softening". Applied Surface Science. 256 (6): 1657–1663. Bibcode:2010ApSS..256.1657R. doi:10.1016/j.apsusc.2009.09.089.
  5. ^ Labban, O.; Liu, C.; Chong, T.H.; Lienhard V, J.H. (2017). "Fundamentals of low-pressure nanofiltration: Membrane characterization, modeling, and understanding the multi-ionic interactions in water softening" (PDF). Journal of Membrane Science. 521: 18–32. doi:10.1016/j.memsci.2016.08.062. hdl:1721.1/105440.
  6. ^ Baker, L.A.; Martin, Choi (2006). "Current Nanoscience". Nanomedicine: Nanotechnology, Biology and Medicine. 2 (3): 243–255.
  7. ^ a b Mohammed, A.W.; et al. (2007). "Modelling the Effects of Nanofiltration Membrane Properties on System Cost Assessment for Desalination Applications". Desalination. 206 (1): 215–225. doi:10.1016/j.desal.2006.02.068.
  8. ^ a b Baker, Richard (2004). Membrane Technology and Applications. West Sussex: John Wiley & Sons. ISBN 0470854456.
  9. ^ a b c d e f g h Schafer, A.I (2005). Nanofiltration Principles and Applications. Oxford: Elsevier. ISBN 1856174050.
  10. ^ a b c Wiley, D.E.; Schwinge, Fane (2004). "Novel Spacer Design Improves Observed Flux". Journal of Membrane Science. 229 (1–2): 53–61. doi:10.1016/j.memsci.2003.09.015. ISSN 0376-7388.
  11. ^ a b Schwinge, J.; Neal, P.R.; Wiley,D.E.; Fletcher, D.F.; Fane, A.G. (2004). "Spiral Wound Modules and Spacers: Review and Analysis". Journal of Membrane Science. 242 (1–2): 129–153. doi:10.1016/j.memsci.2003.09.031. ISSN 0376-7388.
  12. ^ Grose, A.B.F; Smith, A.J.; Donn, A.; O'Donnell, J.; Welch, D. (1998). "Supplying High Quality Drinking Water to Remote Communities in Scotland". Desalination. 117 (1–3): 107–117. doi:10.1016/s0011-9164(98)00075-7. ISSN 0011-9164.
  13. ^ Epsztein, Razi; Shaulsky, Evyatar; Dizge, Nadir; Warsinger, David M.; Elimelech, Menachem (2018-03-06). "Role of Ionic Charge Density in Donnan Exclusion of Monovalent Anions by Nanofiltration". Environmental Science & Technology. American Chemical Society (ACS). 52 (7): 4108–4116. Bibcode:2018EnST...52.4108E. doi:10.1021/acs.est.7b06400. ISSN 0013-936X. PMID 29510032.
  14. ^ a b American Water Works Association (2007). Manual of Water Supply Practices in Reverse Osmosis and Nanofiltration. Denver: American Water Works Association. pp. 101–102. ISBN 978-1583214916.
  15. ^ Misdan, N.; Lau, W.J.; Ismail, A.F.; Matsuura, T. (2013). "Formation of Thin Film Composite Nanofiltration Membrane: Effect of Polysulfone Substrate Characteristics" (PDF). Desalination. 329: 9–18. doi:10.1016/j.desal.2013.08.021.
  16. ^ Subramanian, S; Seeran (2012). "New Direction is Nanofiltration Applications- Are Nanofibres the Right Materials as Membranes in Desalination". Desalination. 308: 198. doi:10.1016/j.desal.2012.08.014.
  17. ^ Pearce, G (2013). Nifty Nanofiltration, New Developments Show Promise (26 ed.). Water World Magazine.
  18. ^ Dražević, E.; Košutić, K.; Dananić, V.; Pavlović, D.M. (2013). "Coating Layer Effect on Performance of Thin Film Nanofiltration Membrane in Removal of Organic Solutes". Separation and Purification Technology. 118: 530–539. doi:10.1016/j.seppur.2013.07.031.

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