A Fl LTER MEDI A

Fl ELD OF THE I NVENTI ON

The present invention relates to a filter media, more particularly, to a filter media which may be used for filtering contam inants such as heavy metals from fluids such as water.

1 NTRODUCTI ON

Heavy metals are naturally occurring metallic elements which have a relatively high atomic weight and density com pared to water. As a result of their industrial, domestic, agricultural, medical and technological uses, heavy metals have become widely distributed in the environment and as a result pose a health risk to humans. The toxicity of heavy metals is dependent on a num ber of factors, including the level of exposure, the identity of the metal species, and the means of exposure. The metals posing the greatest risk to public health due to their toxicity are lead, arsenic, cadmium , chrom ium , and mercury.

Due to their adverse effects on human health, the presence of heavy metals in drinking water is strictly controlled. For exam ple, the maximum allowable concentration in drinking water for lead is 5 pig/L, for arsenic is 10 pg / L, for cadm ium is 5 pg/ L, and for mercury is

2 pg/L.

Lead is one of the most com mon heavy metal contam inants in drinking water. Sources of lead contam ination include lead water pipes, water tanks, plum bing fixtures, and pipe fittings. Exposure to lead can cause a num ber of negative health effects, im pacting the nervous, reproductive, and renal systems, causing high blood pressure and anaemia, and at very high concentrations, leading to death.

Heavy metal impurities are present in fluids such as water in both soluble and particulate forms. Most current fluid filtration systems are designed to retain particulates only, since they only have mechanical retention mechanisms. Removal of soluble heavy metals, however, requires the filter media to chem ically or electrostatically interact with solubilised metal particles in order to retain them .

Current filtration solutions capable of retaining soluble heavy metals such as lead typically include large blocks of absorbent materials. However, the large quantity of absorbent material required in these systems can make them expensive. They also have reduced flow rates due to the large quantity of filter material through which the fluid has to pass, and generally are incapable of removing soluble heavy metals to the levels recom mended by regulatory bodies, such as the National Sanitation Foundation (NSF) and the Water Quality Association (WQA) . Also, current filtration systems are not capable of retaining both particulate and soluble heavy metals to within regulatory lim its.

There is accordingly a need for new filter media capable of removing particulate and dissolved heavy metal contaminants such as lead from fluids such as water.

SUMMARY OF THE I NVENTI ON

I n accordance with a first aspect of this invention, there is provided a filter media com prising a filtration particle, said filtration particle having an AI ₂ O ₃ content of from 15 wt% to 70 wt% and a SiO ₂ content of less than 70 wt% based on the weight of the particle.

I n accordance with a further aspect of the invention, there is provided a filter media com prising a filtration particle, said filtration particle having an AI ₂ O ₃ content of from 15 wt% to 70 wt% and a SiO ₂ content of less than 70 wt% based on the weight of the particle, wherein the filtration particle com prises at least 5 wt% Na ₂ O.

The filtration particle may have an AI ₂ O ₃ content of from 20 wt% to 45 wt% , preferably from 30 wt% to 40 wt% .

The filtration particle may have a SiO ₂ content of less than 60 wt% , preferably less than 50 wt% .

The filtration particle may com prise at least 5 wt% , preferably at least 10 wt% , most preferably at least 15 wt% Na ₂ O.

The filtration particle may have a mass ratio of silicon to alum inium (Si/AI) of from 0.6 to 4, preferably from 0.7 to 3.5, more preferably from 0.8 to 1 .5.

The filtration particle may have a mass ratio of sodium to silicon (Na/Si) of from 0.1 to 0.9, preferably 0.4 to 0.7, more preferably 0.5 to 0.6.

The filtration particle may have a mass ratio of sodium to alum inium (Na/ Al) of from 0.1 to 2, preferably from 0.3 to 1 .5, more preferably from 0.5 to 1 .2. The filtration particle may be a alkali-treated filtration particle.

The filtration particle may com prise pores having a diameter of from 0.1 to 1 .0 nanometers, preferably from 0.3 to 0.7 nm .

The filtration particle may further com prise one or more additional com ponents selected from titanium-containing com ponents (such as TiO ₂ ) , phosphorus-containing com ponents (such as P ₂ O ₅ ) , sulphur-containing com ponents (such as SO3), potassium-containing com ponents (such as K ₂ O) , calcium-containing com ponents (such as CaO) , iron-containing com ponents (such as FeO, FeO ₂ or Fe ₂ O ₃ ) , strontium-containing com ponents (such as SrO) , yttrium-containing com ponents (such as Y ₂ O ₃ ) , and zirconium-containing com ponents (such as ZrO ₂ ) . The additional com ponents may be within a zeolite framework in this case they are not in oxide form . For example, titanosilicate zeolite is a zeolite which has a titanium-containing com ponent within the zeolite framework.

The filtration particle may constitute 5 to 70 wt% , preferably 10 to 50 wt% , most preferably 20 to 40 wt% based on the total weight of the filter media.

The filter media may further com prise matrix fibres selected from one or more of cellulose fibres, polymeric fibres, glass fibres and fibrillated fibres, preferably cellulose fibres and/or glass fibres.

Fibrillated fibres are generally synthetic or cellulosic fibres that were subjected to mechanical treatment to create fibrils. When present fibrillated cellulosic fibres are accounted for as cellulosic fibres and fibrillated synthetic fibres are accounted for as synthetic fibres.

The cellulose fibres may be selected from one or more of softwood fibres, hardwood fibres, vegetable fibres and regenerated cellulose fibres also known as man-made cellulosic fibres (such as Lyocell and Rayon fibres) . The cellulose fibres may be present in an amount of from 5 to 100 wt% , more preferably 10-70% . For exam ple, from 7 to 20 wt% in some em bodiments or from 50 to 70 wt% in other embodiments based on total weight of matrix fibres. The cellulose fibres may preferably be regenerated cellulose fibres.

The glass fibres may be present in an amount of from 5 to 100 wt% , more preferably from 10 to 70 wt% . For exam ple, from 7 to 20 wt% in some em bodiments or from 50 to 70 wt% in other em bodiments based on the total weight of matrix fibres. The polymeric fibres may be polyester fibres and may be present in an amount of from 1 wt% to 30 wt % , preferably from 5 wt% to 30 wt% based on the total weight of the filter media. The polyester fibres may be biopolyester fibres, which may be biodegradable or even com postable according to the EN 1334 standard.

The filter media may com prise a m ixture of cellulose fibres and synthetic fibres. The synthetic fibres may be oil-based (such as polyolefin) or plant-based synthetic fibres.

The matrix fibres may be at least partially coated with nanoalum ina and the filtration particle may be substantially uncoated with nanoalumina.

The filter media may be a non-woven filter media. The non-woven filter media may be corrugated, cut, folded, pleated and assem bled into the filtration product that will ultimately be used.

The filter media may further com prise one or more additives selected from a resin com ponent, preferably a polyam ide-epichlorohydrin (PAE) resin, a binder, preferably com prising latex, activated carbon and/or silver particles.

The filter media may be configured for domestic fluid filtration.

The filter media may be configured for industrial fluid filtration.

The filter media may be a water filter media. The pH of the water may be from 5 to 9 and preferably from 6.5 to 8.

The filter media may com ply with the NSF/ANSI 53 (2019 version) : Drinking Water Treatment Units - Health Effects standard.

I n some em bodiments, a glass free media may be needed. The filter media, in such em bodiments may com prise less than 1 wt% glass fibers, preferably less than 0.1 wt.% glass fibers.

The filter media may be configured for use as a pre-filter of a second filter media. The second filter media may com prise nanoalum ina-coated fibres.

I n accordance with a second aspect of this invention, there is provided a method of manufacturing a filter media as defined above, the method com prising: (a) contacting a filtration particle which has an AI ₂ O ₃ content of from 15 wt% to 70 wt% and a SiO ₂ content of less than 70 wt% based on the weight of the particle with an alkaline solution ;

(b) form ing a wet laid sheet from a fibrous slurry com prising the filtration particle; and

(c) drying the sheet to obtain the filter media.

I n accordance with a further aspect of this invention, there is provided a method of manufacturing a filter media as defined above, the method com prising

(a) contacting a filtration particle which has an AI ₂ O ₃ content of from 15 wt% to 70 wt% and a SiO ₂ content of less than 70 wt% based on the weight of the particle and which com prises at least 5 wt% Na ₂ O with an alkaline solution ;

(b) form ing a wet laid sheet from a fibrous slurry com prising the filtration particle; and

(c) drying the sheet to obtain the filter media.

The contacting step may reduce the SiO ₂ content of the filtration particle, preferably to less than 70 wt% .

Step (a) and step (b) may be performed concurrently.

Step (a) may be performed before step (b) .

The alkaline solution may have a pH of between 8 and 14, preferably between 9 and 1 1 , most preferably 10.

The fibrous slurry may com prise matrix fibres and/or one or more additives as defined above.

The method may include at least partially coating the filtration particle matrix fibres with nanoalum ina. The method may com prise:

(a1 ) contacting the matrix fibres and/or binder fibres with nanoalumina to at least partially coat the matrix fibres and/or binder fibres; and

(a2) com bining the at least partially coated fibres with the filtration particle and alkaline solution to form the fibrous slurry.

I n accordance with a third aspect of this invention there is provided a method of filtering a fluid, the method com prising passing the fluid through the filter media defined above. The fluid may be water, preferably drinking water.

I n accordance with a fourth aspect of this invention, there is provided a method of removing a heavy metal from a fluid, the method com prising passing the fluid through the filter media defined above.

The heavy metal may be selected from arsenic, antimony, cadmium , cobalt, copper, iron, lead and oxidised lead, mercury, nickel, palladium , selenium , silver, thallium , tin and organotin, and zinc, preferably lead. The heavy metal may be in soluble and/or particulate form .

The present invention will be better understood in light of the following exam ples that are given in an illustrative manner and should not be interpreted in a restrictive manner and of the accom panying figures.

BRI EF DESCRI PTI ON OF THE Fl GURES

I n the accom panying Figures:

Figure 1 is a graph illustrating the effect of pH during filter media formation on lead retention performance;

Figure 2 is a graph illustrating the com parative abilities of a nanoalumina- coated glass fibre filter media (“4603”) and a filter media of the present disclosure (“19P64”) to filter lead from a fluid;

Figure s is a graph illustrating the lead filtration abilities of two filter media prepared according to the present disclosure, with each filtration media incorporating a different aluminosilicate zeolite (“SZT” or “SZP”) as filtration particles; and

Figure 4 is a graph illustrating the lead filtration abilities of two filter media prepared according to the present disclosure, with each filtration media incorporating a different aluminosilicate zeolite (“SZT” or “ Alusil”) as filtration particles. DETAI LED DESCRI PTI ON

As used herein and in the accom panying claims, unless the content requires otherwise, the terms below are intended to have the definitions as follows.

5

"Com prise" or variations such as "comprises" or "com prising" will be understood to im ply the inclusion of a stated integer or group of integers but not the exclusion of any other integer or group of integers.

“Nanoalum ina” refers to a com position of alum inium oxide hydroxide [AIO(OH)] and alum inium hydroxide [AI(OH) ₃ ] , which is obtained by reacting alum inium metal with an aqueous alkaline solution, such as NaOH, KOH or ammonium hydroxide.

"Fibre" is a fibrous or filamentary structure having a high aspect ratio of length to5 diameter.

The “mass ratio” of two com ponents A and B with respect to each other, can be recited in the form : Com ponent A/Com ponent B. This refers to the ratio of (weight of Com ponent A) : (weight of Com ponent B) . Com ponent A and Com ponent B may be elements (such as0 Al, Si, Na, etc.) or chemical species (such as AI ₂ O ₃ , SiO ₂ , Na ₂ O, etc) . The mass ratio can be converted to a molar ratio by dividing the masses of the com ponents by their molecular weights.

Sim ilarly, the “molar ratio” of two com ponents A and B with respect to each other, can be5 recited in the form : Com ponent A/Com ponent B. This refers to the ratio of (moles of Com ponent A) : (moles of Com ponent B) . Com ponent A and Com ponent B may be elements (such as Al, Si, Na, etc.) or chem ical species (such as AI ₂ O ₃ , SiO ₂ , Na ₂ O, etc) . The molar ratio can be converted to a mass ratio by m ultiplying the moles of the com ponents by their molecular weights. 0

The prior art seldom explains whether a reported ratio is a mass ratio of substances (e.g. the mass ratio of alumina and silica) or a molar ratio of specific elements within the substances (e.g. the molar ratio of alum inium and silicon atoms) . The lack of specific explanation represents the ratio in an am biguous and undefined manner, making it difficult5 for the skilled person to know the teaching of the prior art with any certainty. As used throughout the present disclosure, the mass ratio and molar ratio of two com ponents of a filtration particle or filter media, as the case may be, will be understood in terms of the above definitions. "Staple fibre" means a fibre which naturally possesses or has been cut or further processed to definite, relatively short, segments or individual lengths.

"Fibrous" means a material that is composed predominantly of fibre and/or staple fibre.

The terms "non-woven" or "web" refers to a collection of fibres and/or staple fibres in a web or mat which are randomly interlocked, entangled and/or bound to one another so as to form a self-supporting structural element.

"Synthetic fibre" refers to fibres made from fibre-forming substances including polymers synthesised from chemical compounds, modified or transformed natural polymer and silicious (glass) materials. Such fibres may be produced by conventional melt-spinning, solution-spinning, solvent spinning and like filament production techniques.

The present disclosure provides a filter media suitable for use in a variety of industrial and domestic fluid purification applications. The filter media is particularly suitable for removing impurities, such as heavy metals (e.g. arsenic, antimony, cadmium, cobalt, copper, iron, lead and oxidised lead, mercury, nickel, palladium, selenium, silver, thallium, tin and organotin, and zinc), dyes, oils, biological materials (e.g. bacteria, viruses, natural organic matter, cysts, and cell debris), and trace pharmaceuticals from fluids, such as water.

The filter media comprises a filtration particle which has an AI2O3 content of from 15 wt% to 70 wt% and a SiO ₂ content of less than 70 wt% based on the weight of the particle. The filtration particle may have an AI ₂ O ₃ content of from 20 wt% to 65 wt%, 20 wt% to 60 wt%, 20 wt% to 55 wt%, 20 wt% to 50 wt%, 20 wt% to 45 wt%, 20 wt% to 40 wt%, 25 wt% to 65 wt%, 25 wt% to 60 wt%, 25 wt% to 55 wt%, 25 wt% to 50 wt%, 25 wt% to 45 wt%, 25 wt% to 40 wt%, 30 wt% to 65 wt%, 30 wt% to 60 wt%, 30 wt% to 55 wt%, 30 wt% to 50 wt%, 30 wt% to 45 wt%, 30 wt% to 40 wt%, 35 wt% to 65 wt%, 35 wt% to 60 wt%, 35 wt% to 55 wt%, 35 wt% to 50 wt%, 35 wt% to 45 wt%, or 35 wt% to 40 wt%. The filtration particle may have a SiO ₂ content of less than 70 wt%, 65 wt%, 60 wt%, 55 wt%, 50 wt%, 45 wt%, 40 wt%, or 35 wt%, preferably less than 50 wt%. The filtration particle may have a SiO ₂ content of from 10 wt% to 65 wt%, 10 wt% to 60 wt%, 10 wt% to 55 wt%, 10 wt% to 50 wt%, 10 wt% to 45 wt%, 10 wt% to 40 wt%, 10 wt% to 35 wt%, 10 wt% to 30 wt%, 10 wt% to 25 wt%, 10 wt% to 20 wt%, 15 wt% to 65 wt%, 15 wt% to 60 wt%, 15 wt% to 55 wt%, 15 wt% to 50 wt%, 15 wt% to 45 wt%, 15 wt% to 40 wt%, 15 wt% to 35 wt%, 15 wt% to 30 wt%, 15 wt% to 25 wt%, 15 wt% to 20 wt% , 20 wt% to 65 wt% , 20 wt% to 60 wt% , 20 wt% to 55 wt% , 20 wt% to 50 wt% , 20 wt% to 45 wt% , 20 wt% to 40 wt% , 20 wt% to 35 wt% , 25 wt% to 65 wt% , 25 wt% to 60 wt% , 25 wt% to 55 wt% , 25 wt% to 50 wt% , 25 wt% to 45 wt% , 25 wt% to 40 wt% , 25 wt% to 35 wt% , 25 wt% to 30 wt%, 30 wt% to 65 wt% , 30 wt% to 60 wt% , 30 wt% to 55 wt% , 30 wt% to 50 wt% , 30 wt% to 45 wt% , 30 wt% to 40 wt% , 30 wt% to 35 wt% , 35 wt% to 65 wt% , 35 wt% to 60 wt% , 35 wt% to 55 wt% , 35 wt% to 50 wt% , 35 wt% to 45 wt% , 35 wt% to 40 wt% , 40 wt% to 65 wt% , 40 wt% to 60 wt% , 40 wt% to 55 wt% , 40 wt% to 50 wt% , or 40 wt% to 45 wt% . The mass ratio of silicon to alum inium (Si/ Al) in the filtration particle may be from 0.7 to 4.0, 0.7 to 3.5, 0.7 to 3.0,

0.7 to 2.5, 0.7 to 2.0, 0.7 to 1 .5, 0.8 to 4.0, 0.8 to 3.5, 0.8 to 3.0, 0.8 to 2.5, 0.8 to 2.0,

0.8 to 1 .5, 0.9 to 4.0, 0.9 to 3.5, 0.9 to 3.0, 0.9 to 2.5, 0.9 to 2.0, or 0.9 to 1 .5.

The filtration particle is capable of binding soluble heavy metal cations in fluids such as water and trapping particulate metal particles when the filtration particle is incorporated into a filter media. The com bination of AI ₂ O ₃ and SiO ₂ in the above quantities has been found to enhance the performance of the filtration particle by optim ising the degree of electrostatic attraction between the filtration particle and im purities (such as heavy metals) in fluids such as water during filtering. Without wishing to be bound by theory it is believed that the specific mass ratio of Si/ Al in the filtration particle creates a stronger negative charge concentration within the filtration particle than particles with a higher Si content. This is because aluminium sites in the filtration particle are negatively charged while silicon sites remain neutral. By having a higher proportion of negatively charged sites, the negative charge concentration is higher, which results in a greater num ber of exchangeable cations such as Na ⁺ ions, within the particle and an im proved ability to bind positively charged soluble heavy metal cations, such as lead cations.

The filtration particle may com prise at least 5 wt% , 10 wt% , 15 wt% or 20 wt% , preferably at least 15 wt% Na ₂ O. The filtration particle may com prise between 5 and 40 wt% Na ₂ O, preferably between 10 and 30 wt% Na ₂ O, more preferably between 15 and 25 wt% Na ₂ O. The mass ratio of Na/Si in the filtration particle may be from 0.1 to 0.9, from 0.2 to 0.8, from 0.3 to 0.8, from 0.4 to 0.7, or from 0.5 to 0.6. The filtration particle may have a mass ratio of sodium to aluminium (Na/ Al) of from 0.1 to 2.0, from 0.2 to 1 .5, from 0.3 to 1 .5, from 0.4 to 1 .5, from 0.5 to 1 .2, more preferably from 0.6 to 0.9. These ratios provide an indication of the proportion of exchangeable Na ⁺ cations in the filtration particle.

The filtration particle may be a alkali-treated filtration particle. The base may be selected from one or more of NaOH, KOH, Ba(OH) ₂ , Ca(OH) ₂ , LIOH, and NH ₄ OH. The filtration particle may be treated with an alkaline solution at a pH of from 8 to 14, preferably from 9 to 1 1 , or more preferably at about pH 10. The alkaline solution may alter at least an outer surface of the filtration particle, for exam ple, by altering the Si, Al, or Na content of the filtration particle. I n some em bodiments, the alkaline solution may reduce the Si content of an outer surface of the filtration particle.

The filtration particle may further com prise one or more additional com ponents selected from titanium-containing com ponents (such as TiO ₂ ) , phosphorus-containing com ponents (such as P ₂ O ₅ ) , sulphur-containing com ponents (such as SO3), potassium-containing com ponents (such as K ₂ O) , calcium-containing com ponents (such as CaO) , iron-containing com ponents (such as FeO, FeO ₂ or Fe ₂ O ₃ ) , strontium-containing com ponents (such as SrO) , yttrium-containing com ponents (such as Y ₂ O ₃ ) , and zirconium-containing com ponents (such as ZrO ₂ ) . The additional com ponents may be within a zeolite framework in this case they are not in oxide form . For example, titanosilicate zeolite is a zeolite which has a titanium-containing com ponent within the zeolite framework.

The filter media may com prise pores through which fluids can pass during filtering. The pores may have a diameter of from 0.5 to 10 pm, from 0.6 to 5 pm, or from 0.7 to 4 pm. The pores may have an average pore size of from 0.8 to 3 pm, preferably, from 1 .2 to 2.0 pm. The pore size is measured using capillary flow porometry technique according to the American Society of Testing and Materials (ASTM) Standard 316-03 (201 1 ) .

The filter media may have a mean flow pore size of less than 3 pm , preferably less than 2.5 pm , more preferably equal or less than 2 pm .

The filter media may have a gravity flow of less than 200 s/500m l_ and preferably less than 150 s/500m L.

The filter media may have a wet MD tensile strength of at least 3 lb/ in , preferably at least 5 Ib/in and most preferably at least 10 Ib/in.

The filter media may maintain levels of soluble lead no more than 10 ppb in the effluent when challenged with water containing 150 ppb of lead as per NSF/ANSI 53 standard (2019) , for an amount of flow which is at least 2000 L/m ² .

The filter media may maintain levels of soluble lead no more than 5 ppb in the effluent when challenged with water containing 150 ppb of lead as per NSF/ANSI 53 standard (2019) , for an amount of flow which is at least 2000 L/m ² or even 5000 L/m ² . The filtration particle may have pores or channels within which exchangeable cations may be located. I n some em bodiments, the pores or channels may have a diameter of from 0.1 to 1 .0 nanometers, preferably 0.3 to 0.7 nanometers. The pores may act as a molecular sieve to selectively screen molecules or atoms according to size and exchangeable cations. The pores may have a negative internal polarity and a high cation exchange affinity for dissolved heavy metals, such as arsenic, antimony, cadmium , cobalt, copper, iron, lead and oxidised lead, mercury, nickel, palladium , selenium , silver, thallium , tin and organotin, or zinc.

The filtration particle may have a surface area determined by Brunauer-Em mett-Teller (BET) method from 300 to 900 m ² /g, preferably from 400 to 700 m ² /g and most preferably around 600 m ² /g. This may provide sufficient surface for ionic exchange and may im prove the efficiency of the filtration particle for retaining heavy metals.

The filtration particle may have a cation exchange capacity (CEC) of at least 2 meq/g preferably 3 meg/g for heavy metals cations especially lead cations when measured at a pH between 6-8.

The filtration particle may have isotherms at both pH 5 and pH 8.5 ( + /-0.5) that match so as to have a Point of Zero Charge (PZC or Iso-electric point) that is outside the pH range of 5 to 8.5.

I n some em bodiments, the filtration particle may be a powdered aluminosilicate (such as a zeolite) . I n some em bodiments, the filtration particle may be in the form of an alum inosilicate fibre (e.g. a ceram ic fibre) . For the sake of clarity, it is noted that in such em bodiments where the filtration particle is in the form of a fibre, matrix fibres, if present, are different from the filtration particle.

Sim ilar to other naming conventions for polyatom ic species in organic chem istry, the constituents of a zeolite’s com position may be represented in their monomeric form as their common oxide. However, it is recognized that this is a convention intended to sim plify and standardize analysis and comm unication. For exam ple, a alum inosilicate framework is a polyatomic skeletal structure containing repeat units [-SiC -] ^4- and [-AIC -] ⁵ ' in large proportions. When describing the constituents of a zeolite, the base species are considered individually, so rather than describing the base unit in the form of a coordination tetrahedra, the base unit of the zeolite framework is represented in the form of a com mon mineral oxide. I n other words, proportions of elemental species may be represented by the com mon form of that base unit's oxide, such as SiO2 or AI2O3.

The filtration particle may have an average diameter of from 0.1 to 50 pm . Where the filtration particle is in the form of a powder particle, the average diameter may be from 1 to 30 pm , and where the filtration particle is in the form of a fibre, the average diameter may be from 1 to 5 pm .

The filter media may further com prise matrix fibres for structural support. The matrix fibres may be present in an amount of from 10 to 90 wt% , preferably from 20 to 80 wt% , preferably from 30 to 80 wt% based on the total weight of the filter media. I n some em bodiments, the matrix fibres may be present in an amount of from 30 to 50 wt% , preferably from 35 to 45 wt% , based on the total weight of the filter media. I n some em bodiments, the matrix fibres may be present in an amount of from 50 to 70 wt% , preferably from 55 to 65 wt% , based on the total weight of the filter media. The matrix fibres may be selected from one or more of cellulose fibres, synthetic fibres, polymeric fibres, glass fibres and fibrillated fibres. The cellulose fibres may be present in an amount of from 5 to 100 wt% , more preferably from 7 to 20 wt% or more preferably from 50 to 70 wt% based on total weight of matrix fibres. The cellulose fibres may be selected from one or more of softwood fibres, hardwood fibres, vegetable fibres and regenerated cellulose fibres (such as lyocell or Rayon fibres) , and may preferably be regenerated cellulose fibers.

The glass fibres may be present in an amount of from 5 to 100 wt% , more preferably from 10 to 70 wt% , more preferably from 7 to 20 wt% , or in some other em bodiments preferably from 50 to 70 wt% based on the total weight of matrix fibres.

The filter media can com prise at least 80 wt% , preferably at least 90 wt% , or more preferably at least 95 wt% synthetic matrix fibres based on total weight of matrix fibres. The synthetic matrix fibres may be oil-based or plant-based synthetic fibres and may be selected from one or more of synthetic polymeric fibres, modified or transformed natural polymeric fibres, or silicious (glass) fibres. Exem plary fibres include polyesters (e.g. polyalkylene terephthalates such as polyethylene terephthalate (PET) , polybutylene terephthalate (PBT) and the like) , polyalkylenes (e.g. polyethylenes, polypropylenes and the like) , polyacrylonitriles (PAN) , and polyamides (nylons, e.g. nylon-6, nylon 6,6, nylon- 6,1 2, and the like) .

The polymeric fibres may be polyester fibres and may be present in an amount of from 1 wt% to 30 wt % , preferably from 5 wt% to 30 wt% , based on the total weight of matrix fibres. The polyester fibres may be biopolyester fibres, which may be biodegradable or even com postable according to EN 1334 standard.

According to another alternative, the matrix fibres can com prise a mixture of cellulose fibres and synthetic fibres. The synthetic fibres can be present in the filter media in an amount of up to 50 wt% , preferably between 10 wt% and 30 wt% of the total weight of matrix fibres in the filter media.

To enhance bonding between the filtration particles and matrix fibres, the filter media may include binder fibres, such as the Trevira® T256 PET microfibres manufactured by Trevira® . If present, binder fibres are accounted for as matrix fibres when calculating the weight percentages. Binder fibres com prise a thermoplastic portion that can soften or melt during processing of the filter media, for exam ple during a calendering step. Binder fibres can be monocom ponent or bicom ponent. The bicomponent thermoplastic fibres may com prise a polymer core fibre surrounded by a meltable sheath of thermoplastic polymer which has a lower melting point than the core.

The filter media may include a polymeric binder which may be added to enhance general cohesion of the com ponents of the filter media. The filter media may include a polymeric binder, such as styrene acrylic, acrylic, acrylic co-polymer, polyethylene vinyl chloride, styrene butadiene rubber, polystyrene acrylate, polyacrylates, polyvinyl chloride, polynitriles, polyvinyl acetate, polyvinyl alcohol derivates, starch polymers, phenolics and com binations thereof, including both waterborne and solvent versions. I n some cases, the polymeric binder may be in the form of a latex (e.g. Lubrizol® Hycar® 26450) , such as a water-based latex emulsion. The filter media may include less than 15 wt% , preferably less than 10 wt% of a polymeric binder in the form of latex based on the total weight of the filter media.

The filter media may further include one or more additive com ponents. The additive com ponent may be selected from : activated carbon (which may be suitable for chlorine removal and im proving water taste and odour) , a wet strength resin, such as a polyam ideepichlorohydrin (PAE) resin (e.g. Kymene® GHP resin) , which may be added to enhance the wet strength of the filter media; a dyeing agent, which may be required to give the filter media a favourable appearance; fibre retention agents; separation aids (e.g. silicone additives and associated catalysers) ; a hydrophilic or hydrophobic agent; a wetting agent; an antistatic agent; or an antimicrobial agent, such as silver particles. If present, these additives may be included in amounts of greater than 0 wt% , 0.01 wt% , 0.1 wt% , 1 wt% , 5 wt% , 10 wt% and/or less than about 40 wt%, 35 wt% , 30 wt% , 25 wt% , 20 wt% , 15 wt% , 10 wt% , 9 wt% , 8 wt% , 7 wt% , 6 wt% , 5 wt% , 4 wt% , 3 wt% , 2 wt% , 1 wt% , or any com bination thereof, including for exam ple between 0.01 wt% and 1 wt% , based on the total weight of the filter media.

I n some em bodiments, the filter media may be at least partially coated with nanoalum ina. The matrix fibres and/or binder fibres may be at least partially coated, preferably substantially fully coated, with nanoalum ina, and the filtration particle may be substantially uncoated with nanoalumina. I n some em bodiments, the filtration particle may be at least partially coated with nanoalum ina.

The nanoalum ina may be present in the filter media in an amount of from 1 to 70 wt% , preferably from 10 to 50 wt% , from 15 to 40 wt% , or from 25 to 35 wt% based on the total weight of the filter media.

I n use, the nanoalumina coating may become positively charged when submerged in water, such as when water is passed through the filter media. The pH of the water may be from 5 to 9 and preferably from 6.5 to 8. The positive charge may serve to attract and entrap negatively charged im purities in the water electrostatically, thereby permitting the water to be purified by the filter media.

The filtration particle can be blended with the matrix fibres, binder fibres, polymeric binder, and/or additive com ponent to produce a non-woven filter media.

I n some em bodiments, the filter media may com prise less than 1 wt% glass fibers, preferably less than 0.1 wt% glass fibers.

The filter media may be configured for use as a pre-filter meaning it can be used in conjunction with a second filter media. The pre-filter may be connectable to a filtration system containing a second filter media or may be arranged so as to let the effluent pass through the pre-filter before passing through the second filter media. I n some em bodiments, the second filter media may comprise nanoalum ina-coated fibres. I n use, the pre-filter may be positioned upstream of the filtration system and may be arranged to com plement the second filter media by filtering out im purities of a different nature. For example, the pre-filter may be arranged to remove positively charged impurities such as heavy metal cations from a fluid before the fluid enters the filtration system containing the second filter media, and the second filter media may be configured to remove negatively charged contaminants such as particulate matter, organic acids, viruses, bacteria, cysts, cell debris or trace pharmaceuticals. The porosity of the filter media in the pre-filter may be sufficiently large to have a negligible impact of the flow rate through the second filter media. This arrangement can be more cost effective than incorporating a full second layer of the filter media into the filtration system in order to remove heavy metal impurities from fluids to be filtered.

The filter media used as a pre-filter or as standalone filter media may be protected or supported by additional layers which have limited impact on the porosity of the filter media.

The disclosure extends to a method of manufacturing a filter media as defined herein, the method comprising:

(a) contacting a filtration particle which has an AI ₂ O ₃ content of from 15 wt% to 70 wt% and a SiO ₂ content of less than 70 wt% based on the weight of the particle with an alkaline solution;

(b) forming a wet laid sheet from a fibrous slurry comprising the filtration particle; and

(c) drying the sheet to obtain the filter media.

The AI ₂ O ₃ content of the filtration particle in step (a) may be from 20 wt% to 65 wt%, 20 wt% to 60 wt%, 20 wt% to 55 wt%, 20 wt% to 50 wt%, 20 wt% to 45 wt%, 20 wt% to 40 wt%, 25 wt% to 65 wt%, 25 wt% to 60 wt%, 25 wt% to 55 wt%, 25 wt% to 50 wt%, 25 wt% to 45 wt%, 25 wt% to 40 wt%, 30 wt% to 65 wt%, 30 wt% to 60 wt%, 30 wt% to 55 wt%, 30 wt% to 50 wt%, 30 wt% to 45 wt%, 30 wt% to 40 wt%, 35 wt% to 65 wt%, 35 wt% to 60 wt%, 35 wt% to 55 wt%, 35 wt% to 50 wt%, 35 wt% to 45 wt%, or 35 wt% to 40 wt%, and the SiO ₂ content may be less than 65 wt%, 60 wt%, 55 wt%, 50 wt%, 45 wt%, 40 wt%, or 35 wt%, preferably less than 50 wt%, or from 10 wt% to 65 wt%, 10 wt% to 60 wt%, 10 wt% to 55 wt%, 10 wt% to 50 wt%, 10 wt% to 45 wt%, 10 wt% to 40 wt%, 10 wt% to 35 wt%, 10 wt% to 30 wt%, 10 wt% to 25 wt%, 10 wt% to 20 wt%, 15 wt% to 65 wt%, 15 wt% to 60 wt%, 15 wt% to 55 wt%, 15 wt% to 50 wt%, 15 wt% to 45 wt%, 15 wt% to 40 wt%, 15 wt% to 35 wt%, 15 wt% to 30 wt%, 15 wt% to 25 wt%, 15 wt% to 20 wt%, 20 wt% to 65 wt%, 20 wt% to 60 wt%, 20 wt% to 55 wt%, 20 wt% to 50 wt%, 20 wt% to 45 wt%, 20 wt% to 40 wt%, 20 wt% to 35 wt%, 25 wt% to 65 wt%, 25 wt% to 60 wt%, 25 wt% to 55 wt%, 25 wt% to 50 wt%, 25 wt% to 45 wt% , 25 wt% to 40 wt% , 25 wt% to 35 wt%, 25 wt% to 30 wt% , 30 wt% to 65 wt% , 30 wt% to 60 wt% , 30 wt% to 55 wt% , 30 wt% to 50 wt% , 30 wt% to 45 wt% , 30 wt% to 40 wt% , 30 wt% to 35 wt% , 35 wt% to 65 wt% , 35 wt% to 60 wt% , 35 wt% to 55 wt% , 35 wt% to 50 wt% , 35 wt% to 45 wt% , 35 wt% to 40 wt% , 40 wt% to 65 wt% , 40 wt% to 60 wt% , 40 wt% to 55 wt% , 40 wt% to 50 wt% , or 40 wt% to 45 wt% .

Step (a) and step (b) may be performed concurrently. Alternatively, step (a) may be performed before step (b) .

The alkaline solution may have a pH of between 8 and 14, preferably between 9 and 1 1 , or preferably about 10.

The fibrous slurry may com prise matrix fibres, binder fibres, a polymeric binder, and/or an additive com ponent. The method may include a step of blending the filtration particle with the matrix fibres, binder fibres, a polymeric binder, and/or an additive com ponent to form the fibrous slurry. The fibrous slurry may further com prise the alkaline solution. I n some em bodiments, the filtration particle may be separated from the alkaline solution prior to form ing the fibrous slurry.

The filter media produced according to the method may be a non-woven filter media.

By contacting the filtration particle with the alkaline solution, the quantity of neutrally charged SiO ₂ in the filtration particle may be reduced primarily through solubilisation of the SiO ₂ , whereas the quantity of negatively charged AI ₂ O ₃ may remain largely unaffected. This may have the effect of increasing the negative charge density on the filtration particle and consequently increasing the capacity of the filtration particle to retain positively charged heavy metal ions, such as lead ions. The treated filtration particles can be incorporated into a filter media to provide an extended and higher degree of soluble metal ion retention than could be achieved using an equivalent quantity of untreated filtration particle material. Furthermore, a filter media that includes the treated filtration particles may be capable of removing heavy metals from a fluid such as water to within regulatory lim its. However, although in some em bodiments the effect may be further enhanced by alkali treatment, even without alkali treatment the filter media com prising a filtration particle having an AI ₂ O ₃ content of from 15 wt% to 70 wt% , a SiO ₂ content of less than 70 wt% , and a Na ₂ O content of at least 5 wt% based on the weight of the particle may provide an effective heavy metal removal, in particular lead removal. The method may include a step of at least partially coating the matrix fibres and/or binder fibres with nanoalumina. The coating may be applied to the matrix fibres and/or binder fibres before com bining the coated fibres with the filtration particle to form the fibrous slurry. Accordingly, the method may further com prise:

(a1 ) contacting the matrix fibres and/or binder fibres with nanoalumina to at least partially coat the matrix fibres and/or binder fibres; and

(a2) com bining the at least partially coated fibres with the filtration particle and alkaline solution to form the fibrous slurry.

The nanoalumina may be formed in situ by reacting alum inium metal (typically in the form of a powder or flakes) in an alkaline solution (such as an aqueous solution of NaOH, KOH, or am monium hydroxide) at a pH of from 8 to 14, preferably from pH 9 to pH 1 1 , more preferably about pH 10, with heating (from 60 to 80 °C, preferably at about 70 °C) . After com pletion of the reaction, the pH of the solution may optionally be adjusted (e.g. reduced or neutralised) .

Once the dried filter media has been formed, it may be corrugated, cut, folded, pleated and assem bled into the filtration product that will ultimately be used.

The present disclosure extends to a method of filtering a fluid, the method com prising passing the fluid through the filter media defined above. The fluid may be water, preferably drinking water. The fluid may be urged through the filter media by application of an externally applied pressure, or by hydrostatic pressure. During filtration, im purities in the fluid bind to the filter media (e.g. by electrostatic adhesion to the filtration particle and/or nanoalum ina coating) and/or are trapped by physical occlusion, resulting in purified fluid exiting the filter media.

The present disclosure further extends to a method of removing a heavy metal from a fluid, the method com prising passing the fluid through the filter media defined above. The fluid may be water, preferably drinking water. The heavy metal may be selected from arsenic, antimony, cadm ium , cobalt, copper, iron, lead and oxidised lead, mercury, nickel, palladium , selenium , silver, thallium , tin and organotin, and zinc, and is preferably lead or preferably arsenic. The heavy metal may be in a soluble form , a particulate form , or both a soluble and particulate form .

The filter media may be suitable for use in filtering fluids in industrial applications, for exam ple, removing contam inants from municipal drinking or waste water, treating industrial waste water containing chem ical or pharmaceutical contam inants, ameliorating m ine waste water, or treating water contaminated by oil and gas drilling or processing operations.

The filter media may also be suitable for use in filtering fluids in domestic applications, such as purifying water for drinking or cooking purposes.

The filter media may be incorporated into an apparatus for filtering a fluid, such as water. The apparatus may com prise a dispensing unit for dispensing the fluid, and a filtration unit for filtering fluid dispensed by the dispensing unit. The filtration unit may com prise a filter media as defined above.

EXAMPLES

Example 1

The NSF/ANSI -53 industry standard describes a protocol for testing the efficacy of a water filter for filtering lead in two different types of water. The first is a low alkalinity water having a pH of 6.5 and 10-30 mg/L CaCO ₃ . The second is a more mineralized water having a pH of 8.5 and 100 mg/L CaCO ₃ . Both solutions contain 150 pg/L of Pb, of which 3O±io% is particulate lead.

One prior art filter media, as described in US 2019/02181 1 1 A1 , uses a three-layer structure for lead removal. The first and the third layers are cellulosic fibrous material between which iron-coated ceramic granules are arranged. Although this product is capable of retaining soluble lead, it is saturated rapidly and is not suitable for extended use. The results of the NSF/ANSI -53 (2019 version) test performed on this filter media are illustrated below in Table 1 .

Table 1 : Test data indicating lead reduction at pH 6.5

As the above data illustrate, the levels of lead in the output water exceed the NSF level of 5 pg/ L throughout the test.

Exam ple 2 - Effect of pH on lead retention

Preparation of the filter media

The filter m edia was prepared according to the com ponents indicated in Table 2 below.

The am ounts are based on dry basis wt% .

Table 2 : Com ponents and quantities used to prepare the tested filter m edia

Preparation of the filter media and testing

Six filter m edia were prepared by a wet-laying process at pH 5, 7, 8, 9, 10 and 1 1 , respectively. Lead retention performance for each the filter media was tested using a solution containing 150 ppb of soluble lead. The lead-containing solution was passed through the filter media and the am ount of lead ions in the effluent was measured. After this initial screening of the filter m edia it was concluded that the filter media prepared at pH 10 presented the highest perform ance. The results are illustrated in Figure 1 . Example 3

Using the data of Example 2, a filter media was prepared at industrial scale according to the com ponents and their quantities indicated in Table 3 below.

Table 3 : Com ponents and quantities used in tested filter media

The com ponents were added sequentially to a pulper as follows:

50% of the Lauscha B-06-F was added and dispersed for 5 minutes at 850-950 rpm . The rest of Lauscha was added and dispersed for 5 m inutes at 850-950 rpm . Lauscha C-04-F was added and dispersed for 5 m inutes at 850-950 rpm .

Lyocell L-040-6, Trevira T256 and filtration particle (Surfatas SZT powder) were added and dispersed for 5 m inutes at 850-950 rpm .

A sodium hydroxide solution was added until pH 10 was reached.

Kymene 557H was added and dispersed for 1 minute.

Lubrizol (Hycar) 26450 Latex was added and dispersed for 1 minute.

Preparation of the filter media and testing

Using this solution, a filter media was prepared by a wet-laying process. The filter media had the following characteristics:

Table 4 : Physical properties of prepared filter media

Mean Flow Pore Size is the pore diameter at which the flow through a wetted medium is 50% of the flow through the dry medium at the same pressure drop using capillary flow porometry technique.

Pore size was determined by the American Society of Testing and Materials (ASTM) Standard 316-03 (201 1 ) (incorporated fully by reference herein) . I n capillary flow porometry the sam ple is first wetted with a wetting fluid such that all the pores in the sam ple are filled. A nonreacting gas of increasing pressure is applied to one side of the wet sam ple to displace the liquid from the pores. The gas pressure and gas flowrate downstream of the sam ple are measured and plotted for the wet sam ple. After the sam ple is dry, the test is repeated to plot a gas flow vs. the applied pressure curve for the dry sam ple. Using such capillary porometry technique, the “maxim um pore size”, “m inim um pore size” and “mean flow pore size” can be determ ined.

The pore size and mean flow pore size were measured with Porometer 3G zh FULL RANGE CAPI LLARY FLOW POROMETER.

Gravity flow is used to evaluate the filter media’s ability to let liquid pass through the filter media without external pressuring device such as a pum p. The gravity flow is also useful to indirectly evaluate pressure drop during filtration.

To measure the gravity flow of a filter media the following method is used:

The filter media is cut in 13.3 m m disc and securely fixed at the bottom of a 2L water colum n contained in a graduated measuring cylinder. The water column has substantially the same diameter as the filter media disc.

The cylinder is arranged on top of a beaker placed on a balance but the cylinder does not exercise weight on the balance. The amount of water dripping from the water column to the beaker is measured via the balance at different time interval. The gravity flow can be determ ined by measuring the time it takes for the beaker to have 500 m L of water. Wet MD tensile strength is measured following ISO 1924-2 but wherein the test pieces are submerged for 5 seconds in water and are placed between two absorbent papers to absorb excess water. The tensile strength of the test pieces is then measured following ISO 1924- 2.

The filter media was tested for com pliance with NSF/ANSI -53. The results are provided in Table 5 below.

Table 5 : Test data showing lead filtration by filter media at pH 6.5

The results indicate that the filter media of the present disclosure was capable of reducing soluble and particulate lead in the effluent stream to less than 5.0 pig/L, in accordance with the maxim um allowable level stipulated in the NSF/ANSI -53 standard.

Example 4

The filter media from Exam ple 3 (labelled “19P64”) was arranged as a pre-filter upstream of a fibrous nanoalumina-coated media filter (“4603”) and was tested for com pliance with NSF/ANSI -53. The nanoalumina-coated filter media com prised glass fibres coated with nanoalum ina. The results are provided in Table 6 below and show that both particulate and soluble lead levels were maintained below the maxim um allowable level stipulated in the NSF/ANSI -53 standard over the course of the experiment.

Table 6 : Results of lead retention experim ent using prepared filter media

I n order to demonstrate that the lead removal efficacy resulted from the pre-filter and not the fibrous nanoalumina filter media, the lead removal performance of each filter media was tested independently using a solution containing 150 ppb of soluble lead according to the NSF/ANSI -53 protocol. The results are illustrated in Figure 2 which shows that the nanoalumina filter media (“4603”) quickly became saturated whereas the filter media of Example 2 (“19P64”) filtered and retained lead consistently over the whole course of the experiment.

Example 5

A nanoalum ina-coated filter media was prepared according to the com ponents and quantities indicated in Table 7 below.

Table 7 : Com ponents and quantities used in tested filter m edia

After the addition of the fibre com ponents and nanoalumina reagents (aluminium powder and NaOH solution) to a pulper, the mixture was heated at 71 °C for about 15-20 m inutes under stirring. The heating was stopped and the stirring maintained for 20 minutes in order to com plete the nanoalumina formation reaction (hydrolysis of alum inium powder in a solution of NaOH) . The nanoalumina coated fibres were com bined with the filtration particle and additives and a filter media was prepared by a wet-laying process. The filter media was tested for com pliance with NSF/ANSI -53. The results are provided in Table 8 below.

Table 8 : Resu lts of lead retention experim ent using prepared nanoalum ina-coated filter m edia

Example 6

Filter media were prepared using a variety of alum inosilicate zeolites to determine whether treatment with alkaline solution enhanced their ability to retain lead im purities in water. The filter media were prepared according to the protocol described in Exam ple 3. The results are illustrated in Figures 3 and 4.

The results illustrate that both the SZT and SZP alum inosilicate zeolites exhibited high levels of lead retention after treatment with the alkaline solution, whereas Alusil became saturated after about 3600 m L and showed poor retention of lead thereafter. Bauxaline and Zeochem did not demonstrate any appreciable lead removal and pH modification was not attem pted. The chemical com positions of the tested zeolites are provided in Table 9 below.

Table 9 : Chem ical com positions of tested zeolites (values in wt% )

The results further illustrate that the presence of Na ₂ O in the filtration particles enhances the removal of heavy metals from fluids. I n particular, the presence of Na ₂ O im proves lead retention, typically when the filtration particle com prises at least 5 wt% , preferably at least 10 wt% Na ₂ O.

The present invention can be further understood with reference to the following paragraphs:

1 . A filter media comprising a filtration particle, said filtration particle having an AI ₂ O ₃ content of from 15 wt% to 70 wt% and a SiO ₂ content of less than 70 wt% based on the weight of the particle.

2. The filter media of paragraph 1 , wherein the filtration particle has an AI ₂ O ₃ content of from 20 wt% to 45 wt% , preferably from 30 wt% to 40 wt% .

3. The filter media of paragraph 1 or paragraph 2, wherein the filtration particle has a SiO ₂ content of less than 60 wt% , preferably less than 50 wt% .

4. The filter media of any one of paragraph 1 to 3, wherein the filtration particle com prises at least 5 wt% , preferably at least 10 wt% , most preferably at least 15 wt% Na ₂ O.

5. The filter media of any one of paragraph 1 to 4, wherein the filtration particle has a mass ratio of silicon to aluminium (Si/AI)of from 0.6 to 4, preferably from 0.7 to 3.5, more preferably from 0.8 to 1 .5.

6. The filter media of any one of paragraph 1 to 5, wherein the filtration particle has a mass ratio of sodium to silicon (Na/Si) of from 0.1 to 0.9, preferably 0.4 to 0.7, more preferably 0.5 to 0.6. 7. The filter media of any one of paragraph 1 to 6, wherein the filtration particle has a mass ratio of sodium to aluminium (Na/ Al) of from 0.1 to 2.0, preferably from 0.3 to 1 .5, more preferably from 0.5 to 1 .2.

8. The filter media of any preceding paragraph, wherein the filtration particle is a alkali-treated filtration particle.

9. The filter media of any preceding paragraph, further comprising matrix fibres, preferably selected from one or more of cellulose fibres, polymeric fibres, glass fibres and fibrillated fibres.

10. The filter media of paragraph 9, wherein the cellulose fibres is selected from one or more of softwood fibres, hardwood fibres, vegetable fibres and regenerated cellulose fibres.

1 1 . The filter media of any one of paragraph 9 or 10, wherein the cellulose fibres is present in an amount of from 5 to 100 wt% , more preferably 10-70% alternatively from 7 to 20 wt% or from 50 to 70 wt% based on total weight of matrix fibres.

12. The filter media of any one of paragraph 9 to 1 1 , wherein the cellulose fibres is regenerated cellulose fibres.

13. The filter media of any one of paragraph 9 to 12, wherein at least a portion of the cellulose fibres are fibrillated.

14. The filter media of paragraph 9, wherein the glass fibres is present in an amount of from 5 to 100 wt% , more preferably from 10 to 70 wt% alternatively from 7 to 20 wt% or from 50 to 70 wt% based on the total weight of matrix fibres.

15. The filter media of paragraph 9, wherein the polymeric fibres is polyester fibres and is present in an amount of from 1 wt% to 30 wt % , preferably from 5 wt% to 30 wt% based on the total weight of the filter media.

16. The filter media of any preceding paragraph, wherein the filtration particle has an AI ₂ O ₃ content of from 20 wt% to 45 wt% , preferably from 30 wt% to 40 wt% and a SiO ₂ content of less than 60 wt% , preferably less than 50 wt% , based on the weight of the particle, wherein the filtration particle com prises at least 10 wt% , most preferably at least 15 wt% Na ₂ O, wherein the filtration particle has a mass ratio of silicon to aluminium (Si/ Al) of from 0.6 to 4, preferably from 0.7 to 3.5, more preferably from 0.8 to 1 .5.

17. The filter media of paragraph 8, wherein the filtration particle has an AI ₂ O ₃ content of from 20 wt% to 45 wt% , preferably from 30 wt% to 40 wt% and a SIO ₂ content of less than 60 wt% , preferably less than 50 wt% , based on the weight of the particle, wherein the filtration particle com prises at least 10 wt%, most preferably at least 15 wt% Na ₂ O, wherein the filtration particle has a mass ratio of silicon to aluminium (Si/AI) of from 0.6 to 4, preferably from 0.7 to 3.5, more preferably from 0.8 to 1 .5, and wherein the filtration particle is a alkali-t reated filtration particle.

18. The filter media of paragraph 9, wherein the matrix fibres are at least partially coated with nanoalum ina.

19. The filter media of any preceding paragraph, wherein the filter media is configured for use as a pre-filter of a second filter media.

20. The filter media of paragraph 18, wherein the filtration particle has an AI ₂ O ₃ content of from 20 wt% to 45 wt% , preferably from 30 wt% to 40 wt% and a SIO ₂ content of less than 60 wt% , preferably less than 50 wt% , based on the weight of the particle, wherein the filtration particle com prises at least 10 wt%, most preferably at least 15 wt% Na ₂ O, wherein the filtration particle has a mass ratio of silicon to aluminium (Si/AI) of from 0.6 to 4, preferably from 0.7 to 3.5 more preferably from 0.8 to 1 .5, wherein the filtration particle is a alkali-treated filtration particle, wherein the filter media comprises matrix fibres selected from glass fibres and cellulose fibres, and wherein the glass fibres and/or cellulose fibres are at least partially coated with nanoalum ina.

21 . The filter media of paragraph 20, which is configured for use as a pre-filter of a second filter media.

22. The filter media of any preceding paragraph wherein the filtration particle com prises one or more additional com ponents selected from titanium-containing com ponents (such as TIO ₂ ) , phosphorus-containing com ponents (such as P ₂ O ₅ ) , sulphur- containing com ponents (such as SO ₃ ) , potassium-containing com ponents (such as K ₂ O) , calcium-containing com ponents (such as CaO) , iron-containing com ponents (such as FeO, FeO ₂ or Fe ₂ O ₃ ) , strontium-containing com ponents (such as SrO) , yttrium-containing com ponents (such as Y ₂ O ₃ ) , and zirconium-containing com ponents (such as ZrO ₂ ) . 23. The filter media of paragraph 9 to 16 or 18, wherein the filtration particle has an AI ₂ O ₃ content of from 20 wt% to 45 wt% , preferably from 30 wt% to 40 wt% , and a SiO ₂ content of less than 60 wt% , preferably less than 50 wt% , and wherein the matrix fibres are at least partially coated with nanoalum ina.

24. The filter media of any preceding paragraph, wherein the filtration particle may constitute 5 to 70 wt% , preferably 10 to 50 wt%, most preferably 20 to 40 wt% based on the total weight of the filter media.

25. A method of manufacturing a filter media of any one of paragraph 1 to 24, the method comprising

(a) contacting a filtration particle which has an AI ₂ O ₃ content of from 15 wt% to 70 wt% and a SiO ₂ content of less than 70 wt% based on the weight of the particle with an alkaline solution ;

(b) form ing a wet laid sheet from a fibrous slurry com prising the filtration particle; and

(c) drying the sheet to obtain the filter media.

26. The method of paragraph 25, wherein the fibrous slurry com prises matrix fibres, binder fibres, a polymeric binder, and/or an additive com ponent.

27. The method of paragraph 25 or 26, wherein step (a) and step (b) are performed concurrently.

28. The method of paragraph 25 or 26, wherein step (a) is performed before step (b) .

29. The method of any one of paragraphs 26 to 28, further com prising at least partially coating the matrix fibres and/or binder fibres with nanoalumina.

30. The method of paragraph 25 or 28, com prising:

(a) contacting a filtration particle which has an AI ₂ O ₃ content of from 15 wt% to 70 wt% and a SiO ₂ content of less than 70 wt% based on the weight of the particle with an alkaline solution ;

(b) form ing a wet laid sheet from a fibrous slurry com prising the filtration particle; and (c) drying the sheet to obtain the filter media; wherein step (a) is performed before step (b) .

31 . The method of paragraph 26 or 29, further comprising: (a1 ) contacting the matrix fibres and/or binder fibres with nanoalum ina to at least partially coat the matrix fibres and/or binder fibres; and

(a2) com bining the at least partially coated fibres with the filtration particle and alkaline solution to form the fibrous slurry.

32. A method of removing a heavy metal from a fluid, the method com prising passing the fluid through the filter media of any one of paragraphs 1 to 24.

33. The method of paragraph 32, wherein the heavy metal is lead and the fluid is water.