Application and Challenges of Membrane in Surface Water Treatment
Herein, we reviewed NOM and its components as the major membrane foulants during the separation and purification of water works. In addition, possible fouling mechanisms relating to NOM fouling, current techniques employed to characterize fouling mechanisms and methods to control fouling were briefly discussed. Conventional water treatment which involves a train of operating units such as coagulation, flocculation and sand filtration consumes substantial spaces and high Hydraulic Retention Time (HRT). Besides that it relies most on chemical consumption such as aluminium sulphate, ferric chloride and poly-aluminium chloride which end up as sludge waste contaminated with aluminium or ferric oxides. Furthermore, the chemical reaction between Natural Organic Matter (NOM) and disinfectant agent such as chlorine or chloramines has been extensively reported to form carcinogenic Disinfection By-Product (DBPs) which is potential in causing deleterious cancers diseases. Therefore, a more reliable and greener technology such as membrane technology has been employed as it possesses better capability in producing water of exceptional quality and practicality over the conventional treatment process. However, the widespread of this potential feature is significantly restricted by fouling issue which reduces its productivity, permeate quality and treatment performance.
The need for water and wastewater treatments with regards to human consumption
and industrial requirement are becoming more challenging as mankind continues
to decline the finite water resources with more complex waste of pollutants
contaminants. Looking at the most advanced water treatment process, it is apparent
that the membrane technology is the todays state of the art. Small size
in the plant, easier maintenance and superior water quality produce by membrane
filtration has made this advanced technology possible to replace the conventional
treatment processes (Clever et al., 2000). Though,
membrane technology is fairly new to the water industry but yet its growth in
treatment applications is tremendous (Table 1). This is due
to a steadily decreasing manufacturing cost, a relatively lower chemical consumption
and low maintenance compared to conventional treatment. Membranes remove contaminants
ranging from suspended solids, colloidal, dissolved organic solutes by physical
retention, chemical adsorption and back diffusion. Dissolved organic matter
is ubiquitous in natural surface water and often reclaimed (Youravong
et al., 2010; Mayani et al., 2010;
Buetehorn et al., 2010; She
et al., 2009; Berberidou et al., 2009)
as important factor for both the reversible and irreversible fouling in water
pore size operating, volume treated and application by membrane processes
Pressure driven membrane processes such as microfiltration (MF), ultrafiltration
(UF), nanofiltration (NF) and Reverse Osmosis (RO) allows the production of
high quality drinking waters. The MF unit is widely used for turbidity or fine
particles removal and is an ideal pretreatment for processes using tighter membranes.
The MF can be operated in dead-end or crossflow filtration mode with latter
being advantage of having tangential flow to sweep foulants off. But this high
flow rate requires more energy and usually reserve for high solids water content.
Apart of that, the UF only became popular in water treatment only recently,
primarily due to its ability to remove bacteria or other microorganisms but
it could only be effective either with a PAC or coagulant pretreatment which
makes the operation more complex and generate a waste stream. Earlier studies
using integrated conventional coagulation followed by direct membrane filtration
or an inline coagulation combined with direct membrane filtration (Neubrand
et al., 2010; Beyer et al., 2010;
Mariam and Nghiem, 2010) have demonstrated effective
control of fouling, improved membrane permeability and superior permeate quality
despite having applied on low quality water sources. The NF is often more appropriate
in water treatment as the product is not fully demineralized. The membranes
used exhibited high organic removal but moderate calcium and alkalinity permeability
made the process more economic compared to RO. However, the disadvantage of
NF and RO are high energy cost, proper pretreatment and generation of waste
streams that need further treatment prior to disposal. In spite of providing
many advantages over the conventional treatment, fouling issue is the main challenge
in membrane filtration efficiency as it causes reduction in permeates quality
and filtration productivity. Productivity decline can be defined as a decrement
in flux with time of operation due to the increment of hydraulic resistance.
Productivity decline may also be interpreted as a need for additional energy
supply to the filtration system so as to keep the system performance constant.
Whereas fouling phenomenon is caused by particles smaller than membrane pores
being adsorbed into the membrane pores then followed by particles of similar
size to pore diameter before cake formation by deposited particles (Neubrand
et al., 2010; Ladner et al., 2010).
Therefore, a fundamental knowledge on the possible foulants and how they cause
fouling are essential before any remediation works is carried out.
Microfiltration (MF): Microfiltration is used in a wide variety of industrial
applications where particles of a size greater than 0.1 μm, have to be
retained from a liquid. Applications include the sterilization and clarification
of all kinds of beverages and pharmaceuticals and in particular pre-treatment
for subsequent finer membrane filtrations, especially in water and wastewater
treatment. Physical sieving is the major rejection mechanism for MF with water
convecting through the membrane due to an applied TMP. The deposit or cake on
the membrane can act as a rejecting layer and retain even smaller solutes than
would be expected to be retained. Thus, a fouled MF membrane may have UF rejection
characteristics and flux may decline significantly due to build up of this deposit.
Electrostatic interactions, dispersion forces and hydrophobic bonding may play
some role in rejection.
Ultrafiltration (UF): Ultrafiltration and nanofiltration, in particular, are important processes for the removal of solutes, macromolecules (such as natural organic matter) pathogenic viruses and small colloidal materials in water and wastewater treatment. The production of potable water from seawater or brackish water by reverse osmosis has become increasingly important, especially in remote areas such as island, sea and inaccessible locations. The UF can as well be used for NF and RO pretreatment, which may lengthen the filtration cycle of these processes compared to a MF pretreatment. As MF, physical sieving is an important rejection mechanism in UF and convection dictates solvent passage. The deposit can also act as a self rejecting layer and charge interaction as well as adsorption may also play an important role. Rejection is usually evaluated with macromolecules of different MW such as dextran or proteins, which leads to the determination of MWCO.
Nanofiltration (NF): The NF is a process located between UF and RO. Some researchers refer NF as charged UF, softening membrane and low pressure RO. The NF is generally expected to remove 60 to 80% of hardness, 90% of color and all turbidity. The process has the advantage of low operating pressures compared to a significant to RO and high rejection of organics compared to UF or MF. However, the monovalent salt is not well retained to a significant extent as his is not normally required in water treatment of surface water. Rejection of membranes is usually evaluated by manufacturer with NaCl or MgSO4 solution as opposed to MWCO speciation in the UF. Rejection mechanisms based on charge and size are important in NF. At neutral pH most NF membrane are negatively charges while at low pH they are mostly positive in charge. Physical sieving is the dominant rejection in NF for colloids and large molecules whereas the chemistries of solute and membrane become increasingly important for ions and lower molecular weight organics.
Reverse osmosis (RO): In RO the osmotic pressure of a solution has to be overcome by an applied transmembrane pressure (TMP) to achieve solvent flux and separation. Recovery (ratio of product per feed) has a high impact on flux and rejection and both decrease with increasing recovery. Physical sieving applies to colloids and large molecules. Besides that, RO rejection is mostly a function of the relative chemical affinity of the solute to the membrane material. Ion rejection follows the lyotropic series which means that rejection is increased with increased hydrated radius of ion. The order of the ions however, may change due to ion pairing, complexation or other solute-solute interactions, thus difficult to predict rejection of ion mixtures. The rejection behavior in the presence of organic is still poorly understood and only trends can be noted. In general RO rejection is usually evaluated with NaCl or MgSO4 solutions permeation.
Challenges: Membrane filtration processes involving microfiltration (MF), ultrafiltration (UF), nanofiltration (NF) and Reverse Osmosis (RO) have steadily gained importance in the environmental engineering separations over the past decade. Numerous improvements in the technology have caused widespread applications of this process in environmental, chemical, pharmaceutical and biomedical fields. However, several aspects of this evolving membrane technology has not yet been addressed conclusively and thus, potentially posing obstacles toward its wide adoption such as inevitable fouling problems, costs factor, know-how technology and unsuitable imported technology.
Know how technology: It is vital to identify membrane foulant and fouling mechanisms before membrane fouling can be alleviated or control. Clear fundamental knowledge on understanding and minimization of membrane fouling are important and can be realized though accurate process design and optimal operating conditions. Maintaining proper operating conditions, accurate pretreatment process, suitable cleaning solution or techniques and proper membrane selection for specific membrane application is the key preventative step to minimize membrane fouling and maintaining high membrane productivity. Apparently membrane efficiency in filtration operation depends greatly on tedious management of fouling. Membrane fouling is the prime bottleneck that retards the membrane effectiveness and wide application. The usage of suitable membrane design, construction, configuration and fouling control techniques will result in longer membrane life, lower operational and design costs. Membrane operating management comprises physical and chemical procedures. Physical methods such as intermittent backwashing, application of critical flux, critical TMP, intermittent suction operation, low TMP, high Cross Flow Velocity (CFV) and hydrodynamic shear stress scouring effect produce only temporary recovery of membrane flux and require high energy consumption. On the other hand, the application of effective chemical cleaning agents such as NaOCl, NaOH, HCl and HNO3 has been proven to completely recover the initial membrane permeability. However, these procedures are expensive, can cause severe membrane damage, chemical contamination and may produce toxic by-product wastes. Backwash technique is dependent on the nature of fouling mechanism and only suitable in back flushing weak adhered cake layer. In the case of pore plugging and pore adsorption (irreversible fouling), the consumption of chemical agent is more favourable. Surface water pretreatment prior to membrane filtration can be done either by adjusting the solubility of NOM or reducing the NOM concentration using precoagulation. Aluminium-based or iron-based coagulants had long been used to remove NOM in the conventional method. Subsequently pretreatment of coagulation prior to membrane filtration has also been employed to enhance the permeate quality as MF and UF alone are inadequate. Since, MF/UF has their own limitations due to their larger molecular weight cut off (MWCO) to the relative molecular mass of NOM, pretreatment processes such as coagulation and PAC would definitely help to improve these weaknesses and are capable to meet water quality requirements for NOM removal.
Fouling problems: Fouling is still the single most important problem that retards the widespread use of membrane separation processes as it could cause high operational and maintenance costs, lower productivity and permeate quality and high frequency of membrane regeneration. Membrane fouling can be defined as the decline in permeate flux or an increase in TMP. The flux decline results from a number of complex kinetic processes that lead to gradual deposition of solids on membrane surface or gradual blockage of the membrane pores. Four types of foulants may be distinguished: chemical foulants, which cause scaling, physical foulants, which are related to deposition of particles, biological foulants, which can form bio fouling and organic foulants, which can interact with the membrane. In general membrane with larger pores exhibit a greater flux decline compared to smaller one. This could be reason due to significantly higher intrinsic fluxes and the increased possibility of internal fouling. One important issue in membrane fouling is due to concentration polarization and cake formation of particulate materials. Concentration polarization is a phenomenon wherein there is a concentration of particles in a thin layer adjacent to the membrane which has the effect of reducing flow through the membrane. Cake formation is the accumulation of particulate matter on the membrane surface. Whereas pore blockage is due to deposition of foulant in the membrane pores.
and recovery of several membrane and hybrid filtration system
Cost factor: Membrane process and membrane technology have changed significantly
in recent years. The required membranes characteristics depend greatly on the
application and the desired permeate quality. As emerging technologies, there
are many unknowns regarding the cost-effectiveness of membrane processes such
as ultrafiltration (UF) and nanofiltration (NF) and RO for the potable water
treatment. Uncertainty is related to the process performance and lack of design
history. For example, the permeation rate that reasonably can be anticipated
when treating raw water using a given membrane has great impact on the capital
and operating costs that are estimated for a membrane installation. The RO membrane
process produces water of exceptional quality but is found to be less cost effective
compared to other membranes.
On the other hand, NF represents an interesting trade-off between the high energy requirement RO and the low rejection UF membrane. If water is turbid but not colored or polluted, MF is an attractive alternative due to its low cost operation. The RO process cost reduced by 30 to 40% after the development of MF pretreatment whereas it concluded their cost modeling with comments that cost is largely a function of flux as the flux determines the membrane area to be installed. At small design capacities (<20, 000 m3), MF and UF costs were competitive with conventional treatment. The UF was less costly than MF for larger facilities (>20,000 m3). The importance of particle size in cost evaluation was also pointed out where cost has been found to increase with particle concentration as well. The UF membrane was cost competitive with conventional treatment for low particle (up to 20 mg L-1) if particles are 0.1 μm on average. The total treatment cost describing the capital and operating costs are shown in Table 2.
Efficacy of imported technology: Membrane technology for surface water treatment is considered to be the most promising development in water treatment as it could provide permeate quality far beyond the current regulatory requirement for potable water consumptions. However, lack of field experience, surface water database and knowledge on specific geographical surroundings, the efficacy of imported membrane is therefore, questionable and may not be optimal to be directly applied in our tropical area. Although, this technology is even becoming more attractive with a package of a compact technology (small footprint) and superior permeate quality, problems related to low membrane life, expensive membranes that are prone to fouling and questionable permeate quality are still a major issues in membrane treatment process especially in our country. In particulars there are still many technical challenges which need further optimization so as to ensure membrane technology remain competitive in the market especially for large scale industry. There is a need for further research of advanced membrane materials that are resistant to both chemical and mechanical attacks during surface water treatment (such as Sg Bekok and Yong Peng water intake) as this would help in prolonging the membrane lifespan and induce long term performance. The identification of the best practices in terms of design, treatment configuration and operating parameter that suit to this tropical climate would help to project minimal capital for design, construction and operational costs. The development of clear fundamental knowledge on understanding and minimization of membrane fouling (due to NOM and particulates in surface water) are also vital and can be realized through employing accurate process design and operating conditions. Furthermore, proper selection of pretreatments, improvement of cleaning strategies and membrane system with low energy requirement may help to position this technology to reach market confidence.
SURFACE WATER FOULANTS
Foulant and its fouling mechanisms are extremely vital to be identified before
one can alleviate the membrane fouling. Membrane fouling refers to both reversible
and irreversible alteration in membrane properties. Reversible fouling means
deposition of retained solutes on the membrane surface that generally exists
as a gel cake layer. Irreversible fouling refers to adsorption or pore plugging
of solutes in and within the membrane pore matrix. Concentration polarizations
are the accumulation of retained materials in the boundary layer above the membrane
due to osmotic pressure and hydraulic resistance effect. Increment and variation
of hydraulic resistances may come from variety of organic substances, inorganic
particles, colloids and microorganisms with different fouling behaviors. The
fouling behavior is significantly found to be influenced by various chemical
and physical factors of the foulants. The foulant can be characterized according
to their molecular structure, surface charge, molecular size and functional
groups. One of the most important identified foulant found in surface water
filtration is Natural Organic Matter (NOM). The NOM waters are a complex mix
of particulate and soluble components of both inorganic and organic origin that
vary from one source to others (Howe et al., 2002).
The NOM is a heterogeneous mixture with wide ranges in Molecular Weight (MW)
and functional groups (phenolic, hydroxyl, carbonyl groups and carboxylic acid)
and is formed by allochthonous input such as terrestrial, vegetative debris
and autochthonous such as algae. Natural organic matters that occur in natural
brown water are polyphenolic molecules with MW ranging from 5000 to 50000 Dalton
(Maartens et al., 1999). In particular, NOM can
be fractionated into three segments; the hydrophobic fraction (humic substances),
hydrophilic and transphilic. The hydrophobic fraction represented almost 50%
of dissolved organic carbon (Fig. 1) with larger MW. The hydrophilic
fraction composed 25-40% of Dissolved Organic Carbon (DOC) with lower MW (polysaccharides,
amino acids, protein and etc.) and operationally defined as non-humic fraction.
The transphilic fraction comprised approximately 25% of DOC in natural water
but with MW in between hydrophobic and hydrophilic fractions. A major fraction
of the NOM arises from humic substances and is reported to represent up to 60
to 70% of TOC in soils and 60 to 90% of DOC in most natural water. Fan
et al. (2001) reported the major fraction (over 50% of DOC) of NOM
is composed of humic substances and are responsible for the natural waters
color. A humic substance is the predominant fraction of NOM and generally is
divided into three categories, which are Humic Acid (HA), Fulvic Acids (FA)
and humin. The HA and FA are anionic polyelectrolyte with negatively charged
of carboxylic acid (COOH¯), methoxyl carbonyls (C=O) and phenolic (OH¯)
functional groups. Figure 2 and 3 show both
models of humic acid and fulvic acids structures. Humic acid is soluble at higher
pH normally 10 while fulvic acid is soluble in water under all pH. Humin is
naturally exists in black color and does not soluble in water at any pH (Fig.
4). Humic fraction has been identified as the major foulant in membrane
water filtration, which controls the rate and extent of fouling (Combe
et al., 1999). It causes more fouling than any other NOM components
due to its adsorptive capacity on the membrane surface (Wiesner
and Aptel, 1996). Study done by Mallevialle et al.
(1989) showed organic matrix formed a structure of fouling layer that served
as a glue for inorganic constituents. Similar results were reported by Kaiya
et al. (1996) in analyzing deposited layer formed on a MF hollow
fiber during filtration of Lake Kasumigaura water. The NOM deposition has been
found as the dominant factor causing flux decline along with manganese constituent.
Study by Mo and Huang (2003) on purification of micro-polluted
raw water revealed that fouling on the exterior surface was a combined effect
of microorganisms and inorganic matter while on the inner surface was mainly
due to the biofouling.
of NOM in surface water based on DOC (Thurman, 1985)
of fulvic acid model structure
and chemical characteristics of humic substances (Stevenson,
They found the organic foulants were of low molecular weight and the inorganic
was primarily represented by Ca2+ element. Their investigation on
membrane permeability recovery showed that alkaline cleaning was effective in
removing organic foulants while acidic cleaning was more effective on inorganic
scales. It has also been shown that hydrophobic fraction of NOM causes much
more fouling than hydrophilic fraction (Nilson and di Giano,
They performed NF of a hydrophilic membrane with aquatic NOM using DAX-8 to
fractionate the NOM components. Hydrophobic fraction (absorbable to DAX-8) was
mainly responsible for the permeate flux decline. On the other hand, the hydrophilic
component which passed through DAX-8 showed less fouling effect. Humic macromolecules
with higher hydrophobicity are found to favourably adsorb onto hydrophobic membrane
than hydrophilic fraction (Jones and OMelia, 2000).
Earlier studies done by many researchers showed that humic substances caused
irreversible fouling of membranes. Yuan and Zydney (1999)
studied humic acid fouling on a 0.16 μm hydrophilic MF and found that aggregate
humic acid was responsible for the initial stage of fouling. Furthermore, fouling
mechanism was substantially due to convective deposition with little internal
pore adsorption. This finding is well supported by Schafer
et al. (2001), who observed humic acid to cause 78% decline in flux
compared to fulvic acid (15%). Humic acid was observed to give greater impact
on membrane performance (irreversible fouling) than FA and hydrophilic fraction
(reversible fouling). This scenario might be due to its high aromaticity properties,
adsorptive behavior, hydrophobic and bigger molecular weight that lead to tendency
of fouling. Similar result was also reported by Turcaud
et al. (1990) during ultrafiltration observations with several organic
and inorganic of Seine River. The flux decline observed was primarily due to
humic acid deposition on the membrane surface. The cellulose acetate membrane
(hydrophilic) flux was twice times greater than hydrophobic polyethersulfone
(PES) during UF of river water. The hydrophilic components were thought to impact
water quality less than the humic fraction, however recent studies done by Lin
et al. (1999) and Carroll et al. (1999)
have claimed that the non-humic fraction of NOM (hydrophilic and neutrals) materials
were responsible in determining the rate and extent of flux decline. Carroll
et al. (1999) performed MF of hydrophobic hollow fibre membrane with
a single water source and concluded that the major cause of fouling was due
to the hydrophilic neutral and not the humic substances. Fan
et al. (2001) reported the order of fouling potential of NOM fraction
as hydrophilic neutral >hydrophobic acids >transphilic acids >hydrophilic
charged. They found that hydrophobic membrane had the most fouling effect than
hydrophilic membrane of similar size suggesting that the fouling mechanism was
governed by adsorption. In addition high molecules weight components had been
identified as having the largest impact on membrane fouling compared to smaller
DOM. This finding was well supported by study carried out by Lee
et al. (2002). They found that polysaccharides and protein that have
larger size of MW and lower UV to HPSEC-DOC/UV response, to significantly fouled
their low pressure (MF/UF) membrane. Polysaccharides are aldehydes derivatives
of high polyhydric alcohols, which have neutral characters that can cause adsorption
on a charged hydrophobic UF membrane (Aiken et al.,
1992). They suggested that the neutral NOM fractions with larged sized were
the prime foulants rather than humic substances. Speth et
al. (2000) in their study also found hydrophilic neutrals fouled more
than hydrophobic acids. It can be reasoned that since, polysaccharides (hydrophilic
neutral) has a bulky macromolecular shape and with no electrostatic effect would
definitely be prone to foul and adsorb on membrane surface. Lin
et al. (1999) performed a study on the effect of fractionated NOM
onto a negatively charge UF membrane and observed that both larged-sized molecules
of hydrophobic and hydrophilic of NOM components caused worsen flux decline.
However, the hydrophilic fraction was found to induce the worst fouling. Jarusutthirak
et al. (2002) in their study on the effect of effluent organic matter
for UF membrane also found that the high molecular weight of hydrophilic component
was responsible as the prime contributor of NOM fouling. It can be claimed NOM
fouling was a result of low UV absorbing compounds and high molecular weight
hydrophilic components that occurred through adsorption mechanisms. Inorganic
particles can also affect the fouling behaviors of the organic substances. Presence
of inorganic particles such as clay minerals in the surface water incurred a
significant influence of competition between NOM and inorganic particles to
adsorb onto the membrane surface or in the pores. High surface areas of inorganic
particle enhance adsorption of organic substances on clays minerals and affect
the fouling characteristic. This results in either enhancing particle deposition
on the membrane or would decrease sorption of NOM onto the membrane and hence,
increase the membrane permeability. But opposite finding was experienced by
Hong and Elimelech (1997) when studied the effect silica
(inorganic particle) on fouling of zirconia tubular membrane.
FOULANTS IDENTIFICATION IN SURFACE WATER TREATMENT
A number of techniques including inline Attenuated Total Reflection (ATR) Fourier
transform infrared (FTIR) spectrometry, UV254, SEC-DOC, DOC fractionation,
pyrolysis-GC/MS, UF fractionation, SEM, SEM with Dispersive Spectrometer (EDS)
and AFM to analyze and characterize membrane foulant. The ATR-FTIR spectrometry
can provide insight of foulant nature in the membrane texture that appears to
be a valuable tool for foulants autopsy (Her et al.,
2000). The FTIR can also be used to determine the functional groups of certain
unknown foulants which corresponding to their vibrational energy of atomic bonds.
Different functional group would absorb energy at different specific wavelength
that latter can be translated in intensity response. Frequent absorption bands
seen are shown in Table 3. But this method may also be insignificant
in identifying of certain functional groups when the absorption reading gives
broad overlapping bands. This phenomenon occurred due to heterogeneity of natural
waters. Researchers (Aiken et al., 1992; Kol
and Konieczny, 2003) used UV254 absorbance at 254 nm to measure
the permeate and retentate of rejected compounds specifically for humic substances.
IR spectra for humic substances, polysaccharides and proteins
The presence of unsaturated compounds would generally produce a distinct color
and can therefore, be detected by UV-Vis (Bruchet et
al., 1990). The UV254 absorbance is sensitive to aromatic
components and is an indicator for both humic acid and fulvic acid presence.
Sample will first be filtered through 0.2 μm to remove particulate matter
and DI is used as a blank. Difference in reading of UV254 absorbance
between feed and permeate indicates the quantity of rejected humic substance
by the membrane. The SUVA or specific ultraviolet absorbance is a ratio of UV
at the wavelength of 254 nm and DOC. High SUVA means high aromaticity or hydrophobicity
of sample in that limited DOC. Permeate from membrane filtration process which
is found with high SUVA value is conforming that most of the rejected compounds
are non-humic and that resulted in high value of UV254 in the permeate.
Earlier studies reported that SUVA of NOM from natural waters or ground waters
was in the range of 2.4-4.3 to 4.4-5.7 L mg-1 m, respectively (Krasner
et al., 1996; Gray et al., 2004).
The molecular weight distribution of NOM was normally determined using high
performance liquid chromatography (HPSEC) with online UV and DOC detection (Schafer
et al., 2000). The HPSEC contains a porous gel that allows separation
of molecules based on their mass and MW. Smaller molecules will access most
of the pore volume while larger molecules that cannot pass the pores will be
eluted first. Subsequently non-humic compound with large molecular weight such
as carboxylic protein and polysaccharides will exhibit significant DOC peaks
but with low area of UV254 peak. On the other hand, humic fraction
such as humic acid and fulvic acid will exhibit high peaks with molecular mass
between 500 daltons to 2000 daltons with high UV response.
diagram of HPO, TPI and HPI fractionation
The most common technique for isolation of NOM fractions are gel filtration,
ultrafiltration and adsorption using non-ionic macro-porous ion exchange resins
DAX-8 and XAD-4 (Bowen et al., 1995). The surface
water is fractionated into hydrophobic (HPO) which is DAX-8 adsorbable, transphilic
(TPI) fraction which is XAD-4 adsorbable and hydrophilic (HPI) components which
pass through the DAX-8 and XAD-4 resin without any adsorption Fig.
5. Application of pyrolysis and GC/MS tool as an analytical method to characterized
complex organic matter had been successfully employed by Speth
et al. (2000) and Jarusutthirak et al.
(2002). A recent study done by Speth et al. (2000)
using pyrolysis with GC/MS showed that hydrophilic fraction of NOM were the
major foulants for a river water filtration. Pyrolysis-GC/MS method was developed
by Bruchet et al. (1990). This tool is useful
for characterizing NOM in terms of biopolymers such as polysaccharides, polyhydroxyaromatics,
amino sugar and protein. Pyrolysing process would casue refractory compounds
to release volatile fragments, which are separated and analyzed by GC/MS. Those
fragments are then characterized by relative percentages according to their
biopolymer. However, pyrolysis -GC/MS technique is considered as a semi quantitative
technique due to variation of fragments characteristics with their biopolymer
structures. Beside that almost 50% of the total peaks would be classified as
miscellaneous and the standards used also may not be effectively representing
the classes of required compounds. The ATR-FTIR and DOC fractionation methods
using non-ionic macro-porous ion exchange resins such as DAX-8 and XAD-4 have
been the most popular techniques used by many researches to characterize the
NOM. But the ATR-FTIR may generate unreliable IR spectra readings due to overlapping
bands. In addition, the DOC fractionation through ion exchange resins (DAX-8
and XAD-4) would exhibit total DOC recovery of less than 100%. This result can
be reasoned due to improper elution procedure of DOC from the resins or the
employed commercial NOM does not represent actual NOM in natural environment
as it would vary with season and origin.
FOULING MECHANISMS IN SURFACE WATER TREATMENT
The extent of rejection of solutes by membrane is the most critical parameter
in membrane filtration. For a clean membrane the extent of rejection is largely
influenced by pore size whereas for a fouled membrane it is determined by the
electrostatic interactions between the solute and membrane. Fouling of membrane
is likely to happen in many instances due to a number of mechanisms such as
pore blocking of solutes, cake deposition and precipitation of inorganic and
organic particles at the membrane surface. Bowen et al.
(1995) elucidated the consecutive steps of membrane blocking in flux decline
during MF as follows: (1) the smallest pores are blocked by all particles arriving
to the membrane, (2) the inner surfaces of bigger pores are covered, (3) some
particles arriving to the membrane cover other already arrived particles while
others directly block some of the pores and (4) a cake starts to be built. The
NOM fouling mechanisms on membrane processes are different and are dependent
upon membrane types. For MF, pore plugging, pore blockage and cake formation
were found responsible for fouling that reduces pore size and increases rejection.
In case of UF, internal pore adsorption reduces the internal pore diameter and
enhances rejection while in NF the fouling mechanism is mostly governed by cake
deposition and concentration polarization. Many researchers suggest humic substances
play a vital role in irreversible fouling of membranes. Maartens
et al. (1998) claimed UF membranes can remove NOM from natural brown
water up to 98% but this progress impacted in flux decline in permeate volume
that was due to irreversible fouling mechanism. Hydrophobic interaction between
the hydrophobic NOM fraction and a hydrophobic membrane may cause more flux
decline than that of hydrophilic membrane. The NOM with variety of organic fractions
of different hydrophobicity, hydrophilicity, molecular weight, sizes and charge
densities would give different interactions in membrane filtration. Yuan
and Zydney (1999) have found that NOM adsorbed both inside the pores and
on the membrane surface to form a cake layer. A cake layer formation is generally
known to occur during surface water filtration using tight UF, NF and RO while
pore blockage or direct adsorption is usually happened when using the MF. A
cake layer formation is caused by electrochemical interaction and the degree
of accumulation is depending on a balance between convective transport of solutes
towards the membrane and back diffusion transport. Transport of large particle
by drag force (convective force) is governed by an orthokinetic mechanism (inertial
lift and shear induced diffusion). Inertial lift induced by wall effect tends
to reduce larger particle to the membrane especially at high CFV. Furthermore,
the shear-induced diffusion is found to increase back transport of particles.
Both of inertial lift and shear-induced diffusion involving backtransport are
functions of particle size. The larger the particle the higher possibility it
will be back transported (Chellam and Weisner, 1997).
On the other hand, back transport of small particle is controlled by Brownian
diffusion, which has less effect compared to inertial lift and shear induced
diffusion. Subsequently large particle in cake tend to produce less resistance
for the same mass of deposited. Turcaud et al. (1990)
described that NOM fouling was primarily governed by pore adsorption and gel
formation. In their study, they experienced 25% flux reduction for the first
5 min of 1 nm UF hollow fibre of 10 mg L-1 humic acid filtration
and a further declination of flux (55%) after 300 min. They concluded the first
5 min rapid declination was due to irreversible adsorption of humic acid foulant.
The continued flux decline was claimed to cause by humic acid gel deposition
(reversible fouling) by convective transport.
MEMBRANE FOULING CONTROL
Membrane fouling is the prime bottleneck that retards the membrane effectiveness
and wide application. Usage of suitable fouling control techniques will result
in longer membrane life and low operation cost. Fouling control comprises physical
and chemical procedures. Physical methods such as intermittent backwashing,
application of critical flux, critical TMP, intermittent suction operation,
low TMP, high Cross Flow Velocity (CFV) and hydrodynamic shear stress scouring
effect produce only temporary recovery of membrane flux and require high energy
consumption. On the other hand, application of effective chemical cleaning agents
such as NaOCl, NaOH, HCl and HNO3 have been proven to completely
recover the initial membrane permeability. However, these procedures are expensive,
can cause severe membrane damage, chemical contamination and may produce toxic
by-product wastes. In practical engineering chemical cleaning is very effective
in removing the deposited foulant and can be adopted as a long term solution
for inevitable fouling but this procedure is out of focus of this study. Backwash
technique is dependent on the nature of fouling mechanism and only suitable
in back flushing weak adhered cake layer. In the case of pore plugging and pore
adsorption (irreversible fouling), consumption of chemical agent is more favourable.
Surface water pretreatment prior to membrane filtration can be done either by
adjusting the solubility of NOM or reducing the NOM concentration using precoagulation.
Aluminium-based or iron-based coagulants had long been used to remove NOM in
the conventional method. Subsequently pretreatment of coagulation prior to membrane
filtration had also been employed to enhance the permeate quality as MF and
UF alone are inadequate. Since, MF/UF has their own limitations due to their
larger Molecular Weight Cut off (MWCO) to the relative molecular mass of NOM,
pretreatment processes such as coagulation and PAC would definitely help to
improve these weaknesses and capable to meet water quality requirements for
NOM removal. However, Turcaud et al. (1990) stated
coagulation pretreatment could only reduce the rate of reversible fouling but
not the irreversible fouling of low molecular weight polysaccharide compounds.
Carroll et al. (1999) found that coagulation
can be used as an efficient pretreatment to improve NOM removal and minimize
fouling in MF of surface water. Coagulation of colloidal material and NOM are
found to reduce the rate of fouling by aggregating fine particles that result
in improving cake permeability, less dense, highly porous flocs and precipitation
or adsorption of dissolved material into flocs. Increased in particle size by
coagulation help to reduce foulant penetration into pores and forming a higher
permeability cake on the membrane surface. Besides that coagulation can also
be used to assemble microorganisms with coagulated matters though it is not
as effective as other disinfectant agent. Maartens et
al. (1998) suggested alteration of pH and application of metal-ions
as pretreatments techniques of feed water as to reduce fouling of polysulfone
UF membrane that was caused by Natural Brown Water (NBW). The NBW with pH 7
managed to sustain at 69% of its original flux after 300 min filtration whereas
NBW with pH 2 was only 33%. In their experiment of using coagulants as pretreatment
agents, they hypothesized that presence of Al3+ and Ca2+
in the NBW would help to block the functional groups of NOM by forming large
precipitated organic material of metal-ions and hence, influence the potential
of adsorptive behavior of NOM membrane-binding activities. However, results
of their study indicated precoagulation with metal-ions could not prevent membrane
fouling but as a matter of fact resulted in an increased of NOM adsorption and
a much worse irreversible fouling mechanism. They explained the increased fouling
to the greater adsorption of NOM to the PSF membrane (40 kDa) caused by metal-ions
Fouling of NOM happens by many factors and mechanisms. Factor affecting NOM and membrane interactions include NOM characteristics, operating conditions, membrane characteristics and solution chemistry. The NOM fouling occurs when dissolved organic or inorganic solute adsorbs or deposits on the membrane. Adsorption mechanism happens more instantaneous and rapid compared to cake formation but depending on the membrane properties, ionic strength, pH and presence of divalent cation. Solute deposition or gel formation occurs parallel with the magnitude of a convective flux and the extent of concentration polarization. Hydrophobicity and electrostatic interactions between solute and membrane are also reported to be the dominant factors that affect the extent of NOM fouling. Presence of electrolyte composition, low pH and high ionic strength had been found to strongly enhance the degree and rate of fouling. The MF and UF are drinking water treatment processes, which are particularly suitable for the removal of suspended solids and colloidal materials such as bacteria, algae, protozoa and inorganic particulates. However, this type of filtration mode is less successful for the removal of dissolved contaminants especially NOM in the surface water. Coagulation had been introduced to address this weakness as it is proven effective for decreasing hydraulic resistance, increasing critical flux and improving NOM removal. There is still controversy over on how the NOM affects the membrane fouling mechanisms. Some studies suggested that charge interaction and adsorptive behavior are the responsible factors that control the NOM fouling whereas others claimed convective and diffusive particle transport that mainly dominate fouling in NOM filtration. As a matter of fact many earlier studies were done using various types of membranes and were operated at high fluxes in their experiment with regards to NOM fouling. These conditions would contribute to physical accumulation due to convection, diffusion and adsorptive fouling. As a result it as difficult to distinguish the dominant factor that responsible to the fouling. Hence, further study needs to be carried out in order to clarify this ambiguity and help in proper selection of membrane property, membrane configuration, pretreatment and operating conditions.
Aiken, G.R., D.M. McKnight, K.A. Thorn and E.M. Thurman, 1992. Isolation of hydrophilic organic acids from water using noniomic macroporous resin. Org. Geochem., 18: 567-573.
Berberidou, C., S. Avlonitis and I. Poulios, 2009. Dyestuff effluent treatment by integrated sequential photocatalytic oxidation and membrane filtration. Desalination, 249: 1099-1106.
Direct Link |
Beyer, M., B. Lohrengel and L.D. Nghiem, 2010. Membrane fouling and chemical cleaning in water recycling applications. Desalination, 250: 977-981.
Bowen, W.R., J.I. Calvo and A. Hernandez, 1995. Steps of membrane blocking in flux decline during protein microfiltration. J. Membr. Sci., 101: 153-165.
Direct Link |
Bruchet, A., C. Rosseau and J. Mallevialle, 1990. Pyrolysis-GC-MS for investigating high-molecular weight THM precursorsand other refractory organics. J. AWWA., 82: 66-74.
Buetehorn, S., F. Carstensen, T. Wintgens, T. Melin, D. Volmering and K. Vossenkaul, 2010. Permeate flux decline in cross-flow microfiltration at constant pressure. Desalination, 30: 985-990.
Carroll, T., S. King, S.R. Gray, B.A. Bolto and N.A. Booker, 1999. The fouling of microfiltration by NOM after coagulation treatment. Water Sci., 34: 2861-2868.
Chellam, S. and M.R. Wiesner, 1997. Particle back-transport and permeate flux behaviour in crossflow membrane filters. Environ. Sci. Tech., 31: 819-824.
CrossRef | Direct Link |
Clever, M., F. Jordt, R. Knauf, N. Rabiger, M. Rudebusch and R.H. Scheibel, 2000. Process water production from river by ultrafiltration and reverse osmosis. Desalination, 131: 325-336.
Combe, C., E. Molis, P. Lucas, R. Riley and M.M. Clark, 1999. The effect of CA membrane properties on adsorptive fouling by humic acid. J. Membr. Sci., 154: 73-87.
CrossRef | Direct Link |
Fan, L., J.L. Harris, F.A. Roddick and N.A. Booker, 2001. Influence of the characteristics of natural organic matter on the fouling of microfiltration membranes. Water Res., 35: 4455-4463.
Gray, S.R., C.B. Ritchie and B.A. Bolto, 2004. Effect of fractionated NOM on low pressure membrane flux declines. Water Sci. Tech., 4: 189-196.
Direct Link |
Her, N., G. Amy and C. Jarusutthirak, 2000. Seasonal variation of nanofiltration (NF) foulants: Identification and control. Desalination, 132: 143-160.
Hong, S. and M. Elimelech, 1997. Chemical and physical aspects of natural organic matter (NOM) fouling of nanofiltration membrane. J. Membr. Sci., 132: 152-181.
Howe, K.J., K.P. Ishida and M.M. Clark, 2002. Use of ATR/FTIR spectrometry to study fouling of microfiltration membranes by naturals waters. Desalination, 147: 251-255.
Jarusutthirak, C., G. Amy and J.P. Croue, 2002. Fouling charateristics of wastewater effluent organic matter (EFOM) isolates on NF and UF membranes. Desalination, 145: 247-255.
Jones, K.L. and C.R. O'Melia, 2000. Protein and humic acid adsorption onto hydrophilic membrane surfaces: Effect of pH and ionic strength. J. Membr. Sci., 165: 31-46.
Kaiya, Y., Y. Itoh, K. Fujita and S. Takizawa, 1996. Study on fouling materials in the membrane treatment process for potable water. Desalination, 106: 71-77.
Kol, D.S. and K. Konieczny, 2003. Application of coagulation and conventional filtration in raw water pretreatment before microfiltration membrane. Desalination, 162: 61-73.
Krasner, S.W., J.P. Croue, J. Buffle and E.M. Perdue, 1996. Three approaches for characterizing NOM. J. Am. Water Works Assoc., 88: 66-79.
Direct Link |
Ladner, D.A., A. Subramani, M. Kumar, S.S. Adham and M.M. Clark, 2010. Bench-scale evaluation of seawater desalination by reverse osmosis. Desalination, 250: 490-499.
Lee, J.D., S.H. Lee, M.H. Jo, P.K. Park, C.H. Lee and J.W. Kwak, 2002. Effect of coagulation conditions on membrane filtration characteristics in coagulation-microfiltration. Environ. Sci. Technol., 34: 3780-3788.
Lin, C.F., T.Y. Lin and O.J. Hao, 1999. Effects of humic substance characteristics on UF performance. Water Res., 34: 1097-1106.
Maartens, A., P. Swart and E.P. Jacobs, 1998. Humic membrane foulants in natural brown water: Characterization and removal. Desalination, 15: 215-227.
Maartens, A., P. Swart and E.P. Jacobs, 1999. Feed-water retreatment methods to reduce membrane fouling by natural organic matter. J. Membr. Sci., 162: 51-62.
Mallevialle, J., C. Anselme and O. Marsigny, 1989. Effect of Humic Substances on Membrane Process. In: Aquatic Humic Substances, Suffet, I.H. and P. MacCarthy (Eds.). ACS., Washington, pp: 749-767.
Mariam, T. and L.D. Nghiem, 2010. Landfill leachate treatment using hybrid coagulation-nanofiltration processes. Desalination, 250: 677-681.
Mayani, M., C.D.M. Filipe and R. Ghosh, 2010. Cascade ultrafiltration systems integrated processes for purification and concentration of lysozyme. J. Membr. Sci., 347: 150-158.
Mo, L. and X. Huang, 2003. Fouling characteristics and cleaning stratergies in a coagulation-microfiltration combination process for water purification. Desalination, 159: 1-9.
Direct Link |
Neubrand, W., S. Vogler, M. Ernst and M. Jekel, 2010. Lab and pilot scale investigations on membrane fouling during the ultrafiltration of surface water. Desalination, 250: 968-972.
Nilson, J.A. and F.A. di Giano, 1996. Influence of NOM composition on nanofiltration. J. AWWA., 88: 53-66.
Direct Link |
Schafer, A.I., A.G. Fane and T.D. Waite, 2000. Fouling effect on rejection in the membrane filtration of natural waters. Desalination, 131: 215-224.
Schafer, A.I., U. Schwicker, M.M. Fisher, A.G. Fane and T.D. Waite, 2001. Microfiltration of colloids and natural organic matter. J. Membr. Sci., 171: 151-172.
She, Q., C.Y. Tang, Y.N. Wang and Z. Zhang, 2009. The role of hydrodynamic conditions and solution chemistry on protein fouling during ultrafiltration. Desalination, 3: 1079-1087.
Speth, T.F., A.M. Guses and R.S. Summers, 2000. Evaluation of nanofiltration pretreatments for flux loss control. Desalination, 130: 31-44.
Stevenson, F., 1982. Humus Chemistry. John Wiley and Sons, New York.
Thurman, E.M., 1985. Organic Geochemistry of Natural Waters. Martinus Nijhoff/Dr W. Junjk Publishers, Dordrecht, The Netherlands, ISBN: 978-94-009-5095-5, Pages: 497.
Turcaud, V.L., M.R. Wiesner and J.Y. Bottero, 1990. Fouling in tangential-flow ultrafiltration: The effect of colloids size and coagulation pretreatment. J. Membr. Sci., 52: 173-190.
Wiesner, M.R. and P. Aptel, 1996. Mass Transport and Permeate Flux and Fouling in Pressure Driven Process. In: Water Treatment: Membrane Processes, Malleviella, J. (Ed.). McGraw-Hill, New York.
Youravong, W., Z. Li and A. Laorko, 2010. Influence of gas sparging on clarification of pineapple wine by microfiltration. J. Food Eng., 96: 427-432.
Yuan, W. and A.L. Zydney, 1999. Humic acid fouling during microfiltration. J. Membr. Sci., 157: 1-12.