1. International Journal of Research in Advent Technology, Vol.2, No.3, March 2014
E-ISSN: 2321-9637
39
Preparation, Characterization and Application of Ultra
Filtration (UF) Membranes
Rajesh Tripathy
Department of Chemical Engineering, G H Patel College of Engineering & Technology,
BakrolRoad,Vallabh Vidyanagar-388 120.Gujarat. India.
Email: rajeshchemtech@gmail.com
Abstract-In recent years, membranes and membrane separation techniques have grown from a simple laboratory
tool to an industrial process with considerable technical and commercial impact. Today, membranes are used on a
large scale to produce potable water from the sea by reverse osmosis, to clean industrial effluents and recover
valuable constituents by electro dialysis to fractionate micro molecular solutions in the food and drug industry by
ultra filtration, to remove urea and other toxins from blood stream by dialysis in an artificial kidney, to recover
valuable products from waste like protein from waste whey and to release drugs such as scopolamine, nitroglycerine
etc. at a predetermined rate in medical treatment.Although membrane processes may be very different in their mode
of operation in the structures used as separating barriers. In many cases, membrane processes are faster, more
efficient and more economical than conventional separation techniques such as distillation, extraction, adsorption,
and absorption.[1,8]
Index Terms-commercial impact, scopolamine, nitroglycerine, ultrafiltration
1.0 INTRODUCTION
Membranes have gained an important place in
chemical technology and are used in a broad range of
applications. The key property that is exploited is the
ability of a membrane to control the permeation rate of
a chemical species through the membrane. In
controlled drug delivery, the goal is to moderate the
permeation rate of a drug from a reservoir to the body.
In separation applications, the goal is to allow one
component of a mixture to permeate the membrane
freely, while hindering permeation of other
components. This paper provides a general
introduction to membrane science and technology and
cover Preparation, Characterization and Application of
Ultra Filtration (UF) Membranes, that is topics that are
basic to all membrane processes, such as transport
mechanisms, membrane preparation, and boundary
layer effects, cover the industrial membrane separation
processes, which represent the heart of current
membrane technology .Carrier facilitated transport is
covered next, followed by reviewing the applications
of membranes. The paper closes with that describes
various minor or yet tobedeveloped membrane
processes, including membrane reactors, membrane
contactors for the separation of protein from different
west, before disposal.
1.1 Membrane Separation Processes
All the membrane technologies are essential separation
technologies depending upon size of the constitutes to
be separated or on the ionic charges or absence of
charges, diffusion into the matrix or some such
transport phenomena. Keeping this in mind it is
essential to mention here that none of the membrane
technologies destroy the pollutants; they either separate
or concentrate them for further easy handling.
Membranes can be classified into 4 categories
depending on the size of the materials they remove
from the carrier liquid. The 4 categories, listed from
the largest to the smallest pore size, are
(a)Micro Filtration (MF)
(b)Ultra Filtration (UF)
(c)Nano Filtration (NF)
(d)Reverse Osmosis (RO)
a) Microfiltration (MF):MF is a low-pressure
membrane process (0.3 to 3.3 bar) that removes
particulate material ranging in size from 0.1 to 1.0
microns (1,000 to 10,000 angstroms) and larger. MF is
used for separating suspended or colloidal materials
from a feed stream. Water, salts, and selected
macromolecules pass through the semi-permeable
membrane, and suspended solids are progressively
concentrated. In the case of water, bacteria (like
Escherichia coli, Cryptosporidium parvum, or Giardia
lamblia) can be separated from water with this

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technique. The salient features of the process are that it
involves no phase change and it is relatively a low
energy process.
b) Ultrafiltration (UF):UF is a low-pressure membrane
process (0.5 to 10 bars) that separates materials in the
0.001 to 0.1 micron range (10 to 1,000 angstroms). UF
is used for the separation of high molecular weight
dissolved materials (solute). Water, salts, and low
molecular weight species selectively pass through the
semi-permeable membrane, and macromolecules and
suspended solids are retained (progressively
concentrated). UF separates bacteria and viruses from
the water stream that MF passes because the pore size
is smaller.
c) NanoFiltration (NF):NF is a high-pressure
membrane process used for separating materials less
than 0.001 microns (10 angstroms) in size. NF is used
for the separation of dissolved materials (solute). Less
expensive, NF is not as fine a filtration as RO, but it
also requires less energy to perform the separation (i.e.
less operation & maintenance cost). In water, NF is
very effective in removing hardness (multiple-charged
ions), total dissolved solids, and natural organic
material (Disinfection-By-Product DBP precursor
material) with MF pre-filtration. NF is also known, in
the water markets, as the "Membrane softening".
d) Reverse osmosis (RO):RO membranes have the
smallest pore structure, with pore diameter ranging
from approximately 5-15 A0 (0.5 nm - 1.5 nm). The
extremely small size of RO pores allows only the
smallest organic molecules and unchanged solutes to
pass through the semi-permeable membrane along with
the water. Greater than 95-99% of inorganic salts and
charged organics will also be rejected by the membrane
due to charge repulsion established at the membrane
surface.
2.0 MATERIALS FOR MEMBRANE
MANUFACTURING
Pressure driven membrane separation processes fall
into four broad categories: microfiltration,
ultrafiltration, nanofiltration and reverse osmosis. The
materials used for the preparation of these membranes,
their morphological characteristics as well as their
applications are different from each other.
Morphologically the membranes are essentially porous
in nature. Pore size in case of microfiltration
membranes is in the order of 200 A0 (0.02 microns) to
1,00,000 A0 (10 microns); in ultrafiltration the pore
size is between of 20A0-200A0; in nanofiltration it is
in the range of 10A0-20A0 and in the case of reverse
osmosis it is between 1A0-10A0. Mechanisms of
separation are also different for these membrane
processes. While size based separations occur in case
of microfiltration and ultrafiltration, membrane-solute
interaction is the basis in nanofiltration and reverse
osmosis. Application wise, microfiltration is used for
the separation of solutes having molecular weight more
than 3,00,000 Daltons, ultrafiltration is used for solutes
in the range of 500-3,00,000 Daltons, nanofiltration is
used for separation of solutes with a molecular weight
range of 300-500 Daltons and reverse osmosis is used
for the separation of solutes with molecular weight up
to 300Dalton. Microfiltration is used for separation of
suspended materials, coarse colloids, etc.,
ultrafiltration is useful in case of separation of soluble
macromolecules, sugars, proteins, etc., nanofiltration is
used in the separation of multivalent ions and reverse
osmosis is used for the separation of ionic solutions.
The membranes are predominantly polymeric in nature
and is thin sheet like materials having typical thickness
of the order of 100 microns. It forms a physical barrier
between the fluids on either side, yet keeping
communication between them. The crucial feature of a
particular membrane is its selective permeability to
certain species for which certain force is needed for the
movement of species through the membrane. The
overall driving force in the transport of species across
the membrane is the chemical potential gradient, which
is the sum of existing gradients such as concentration,
pressure and electrical potential. In RO, water
molecules are forced through the membrane by
applying pressure. Material used for membranes are
predominantly polymeric in nature. For RO, polymers
such as cellulose acetate, polyamide, polyimide
deposited on polysulphone base support etc. are used,
whereas in ultrafiltration, the membrane used is made
up of polysulfone and poly acrylonitrile.[7]
2.1 Membrane Materials:
These can be classified as (a) inorganic and (b)
polymeric.

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(a) Inorganic: Typical are gamma-alumina, alpha-alumina,
borosilicate glass, pyrolyzed carbon,
Zirconia/s. steel Zirconia/ carbon, etc. Other types of
ceramic membranes are also being developed.
Inorganic membranes have certain advantages over
polymeric ones, like temperature and chemical
stability. The cost of these materials and packing
density (area /volume ratio) being the main restriction
towards their large -scale applications.
(b) Polymeric: typical materials, for Ultrafiltration are
polysulphones, polyethersulphone cellulosic materials
polyvinylidenefluoride, polyacrylonitrile, polyamides,
etc the membranes are typically made by the phase
inversion method. Behavior, performance, and
limitations of some of the polymeric membrane are
given below [1,2]
1) Cellulose Acetate (CA)
Raw material used is cellulose, which undergoes
acetylation in presence of acetic anhydride, acetic acid
and sulphuric acid. It is extensively used in UF studies
as it is easy to fabricate less costly high salt retention
and relatively high flux .The raw material cellulose is a
renewable source. But it also has some drawbacks.
Firstly it has fairly narrow range and maximum
temperature recommended is 30 0C. This creates
problems in maintaining sanitary condition and give
lower flux .The PH range is also restricted between 2-
8. Under acidic conditions polymer hydrolyses &
structural integrity is lost. Under highly alkaline
condition, deacetylation occurs, which will affect
selectively, permeability. Also cellulose acetate has a
poor resistance to chlorine .It also undergoes
compaction and creep to a slightly greater extent
pressure. Cellulose acetate is also biodegradable and
hence storage properties.
2) Aromatic polyamides (PA)
It is also an important material for UF .It is
characterized by the having an amide bond in its
structure (--CONH--). In general they show good
temperature resistance even up to 80 0C .The PH
resistance is also good between range 3-11 at 25 0C
.PA membranes are not biodegradable. Cleaning PA
with acid caustic solutions is feasible but they are more
sensitive to chlorine to CA and only polybenimidazole
appears to show some resistance.
3) Polysulfone (PS)
PS is most widely used in UF. These membranes are
characterized by having in its structure
diphenylenesulfonerepeating units.It has wide
temperature limits from 750C –1250C. Wide PH
tolerance from 1-13. It has fairly good resistance and
also it is not biodegradable. It is easy to fabricate
membranes n wide variety of configurations and wide
range of pore sizes. Cleaning using acids and bases and
disinfections, using chlorine and H2O2 are feasible. PS
is also resistant to strong oxidizing agent. Polysulfone
has the apparent low-pressure limit.
4) PAN (Polyacrylonitrile)
PAN is hydrophilic in nature. It is not affected by
boiling water .It is not affected by weak acids, weak
alkalis but affected by strong acids & alkalis. It can be
used up to 180 0C.Oxidising agent & common organic
solvents have little effect. PAN membranes are hard,
relatively insoluble & high melting material.
5) Polyethersulfone (PES):
PES is an amorphous material with a translucent amber
tint. It has excellent dimensional stability and very
good electrical insulation properties. It is also
characterized by its creep resistance - substantial loads
can be carried for long periods at temperatures up to
180°C - and thermal stability PES parts can be used for
thousands of hours up to 200°C with no significant loss
of strength. It has relatively high water absorption and,
in common with many other plastics, drying is
essential before e.g. thermoforming. It has poor fatigue
characteristics and is prone to environmental stress
cracking but has good long-term thermal ageing
resistance and reasonable radiation resistance.
2.2 Selection Of Material
It is evident that for selecting a membrane material
which would be the best choice, it is necessary to
consider operating condition like temperature,
pressure; the nature of feed stream i.e. the pH,
viscosity, density etc. and other factors like solid
contents clean ability.
Although the inorganic materials are having more
temperature and pressure resistant, they can be used in
very high or very low pH, we have chosen polymer
membrane for casting and to study performance
because polymer membranes are flexible in nature and
can be casted in any shape but not the inorganic
materials. Inorganic membranes are more tough cannot
be casted easily.

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There are many polymer membrane materials as
discussed above but we have chosen polyethersulfone
as a casting material because lot of study is done on
other materials but polyethersulfone is not yet explored
much as compared to other materials.
Before going into details of the casting and
performance study we will see some important
physical and chemical properties of the
polyethersulfone.
Membrane materials characteristics
a. The ideal membrane has the following
characteristics:
b. High water flux rates
c. High salt rejection
d. Tolerance to chlorine and other oxidants
e. Resistance to biological attacks
f. Resistance to Fouling by colloidal and
suspended material
g. Inexpensive
h. Mechanical strength
i. Chemical stability
2.3 Membranes Used in present work :
Polymeric
- polysulfone/poly(ether
sulfone)/sulfonatedpolysulfone
- poly(vinylidene fluoride)
- polyacrilonitrile
- cellulosics
- polyimide/poly(ether imide)
- aliphatic polyamides
- polyetheretherketone
Ceramic
- alumina (Al2O3)
- zirconia (ZrO2)
Solvent Used:
-Dimethylformamide(DMF)
-N, N-Dimethylacetamide.(DMAC)
-Dimethylsulfoxide (DMSO)
-N-Methylpyrrolidone(NMP)
-Morfoline
3.0Membrane Preparation Technique
Anumber of different techniques are available to
prepare synthetic membranes. Some of these
techniques can be used to prepare organic (polymeric)
as well as inorganic membranes. The most important
techniques are:
a. Sintering
b. Stretching
c. Track-etching
d. Phase Inversion
e. Coating
Most commercially available membranes are obtained
by phase inversion. This is a very versatile technique
allowing all kind of morphologies to be obtained. This
preparation technique is detailed as follows. Phase
inversion is a process where a polymer is transformed
in a controlled manner from a liquid to a solid state.
The process of solidification is very often initiated by
the transition from one liquid state in to two liquids
(liquid0liquid demixing). At a certain stage during
demixing one of the liquid phases (high polymer
concentration phase) will solidify so that matrix is
formed. By controlling the initial stage of phase
transition the membrane morphology can be controlled,
i.e., porous as well as nonporous membranes can be
prepared. It covers different techniques like
a. Solvent evaporation
b. Precipitation by controlled evaporation
c. Thermal precipitation
d. Precipitation from the vapour phase
e. Immersion precipitation
The most commercially available membranes are
prepared by immersion precipitation: a polymer
solution (polymer + solvent) is cast on a suitable
support and immersed in a coagulation bath containing
a nonsolvent. Precipitation occurs because of the
exchange of the solvent and nonsolvent. The
membrane structure ultimately obtained results from
the combination of mass transfer and phase separation.

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3.1 Phase Inversion Process Of Membrane
Manufacture:
This refers to a method of manufacturing asymmetric
membranes that result in a “solvent cast structure,
which owes it porosity to immobilization of the
polymer gel prior to complete solvent evaporation or
depletion. This is accomplished by not allowing the
cast solution to evaporate to dryness before its structure
is set; partial solvent loss occurs so that the solution
separates into two interspersed liquid phases. One of
these phases represents the voids. As evaporation is
allowed to continue, gel structure is set”. [1,8]
The steps involved in preparation of Polysulfone
membrane are,
a. Preparation of polymer solution.
b. Casting
c. Gelation
d. Annealing.
Preparation of polymer solution
The major constituents of Polysulfone membrane are
classified into three types a) polymer base b) solvent
and c) swelling agents (magnesium perchlorate or
formamide). In addition few more chemicals may be
added imparts certain properties of the membranes.
Sometimes filler chemicals are also added with co-polymers
to form better polymer chain links and
improve mechanical strength. A clean, dry, glass
beaker, washed with hydrochloric acid, is taken. It is
then rinsed with acetone and kept to dry. The specific
quantity of Polysulfone is poured into the beaker,
which is followed by dimethylformamide. The stirring
is stated at this point in order to get a homogeneous
material. The remaining chemicals are then added
slowly under continuous stirring using a glass stirrer.
Proper care was taken to prevent the evaporation of
solvents during the process. The polymerization was
carried out for 4-5 hours. After this period, a viscous
solution with lots of air bubbles trapped in it is
obtained. The air bubbles trapped in it are removed by
keeping the solution still for 3-4 hours. Thus a clear
viscous solution is obtained
Casting:
The casting of Polysulfone membrane is done in a
module. E.g. Flat sheet membranes are made by
drawing the polymer solution over a glass plate using a
“thin layer chromatography unit”. When this solution
is cast and the solvent allowed to evaporate, it results
in an increased concentration of polymer at the
solution/ air interface, since solvent is lost more rapidly
from the surface. The polymer essentially goes out of
solution at the surface and forms the so-called skin
layer that is characteristic of asymmetric membranes.
(This phenomenon is analogues to “case hardening” in
products that have been rapidly dried.). After the skin
forms, the remaining solvent in the bulk of the mixture
evaporates more slowly. Eventually the swelling agent
in the mixture starts separating out as a different phase,
resulting in two phases within the substructure: the
polymer solvent as the concentrated phase and the
swelling agent as the dispersed phase.
Gelation:
The polymer film this formed is further consolidated
by a process of gelation. Here, the polymer chain is
uniformly linked and distributed in the proper
orientation for flow of permeate. Gelation is obtained
by keeping the membrane in water at a low
temperature of about 5-6 oC.
Annealing:
The polymer film thus produced, having a hard crust
layer on spongy porous support, is still mechanically
weak and highly compressible. With application of
pressure the pores can be easily stretched. These are
hardened with consequent shrinkage of pores by means
of proper heat treatment of the membrane. This can be
achieved by the process of annealing.The peeled sheet
is immersed in hot water for a period of five minutes;
the membrane is maintained at 70oC. Product flux and
solute rejection can be controlled buy a process
condition of this step. Higher temperature causes a
decrease in flux of product water and an improvement
in solute rejection and vise –versa. Since the degree of
rejection can be adjusted by changing the heating
temperature, this step is very important in membrane
preparations.
3.0 RESULTS AND DISCUSSION
3.1 Analysis of Protein Solution
To study the performance of ultrafiltration membrane
experimentation is done on dairy whey /milk/protein
solution .In this report, to study the performance of PS
membrane which are casted in laboratory, the standard
protein solution is used. The concentration of BSA
protein solution used for experimentation is 0.5%.

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0.4
0.35
0.3
0.25
0.2
0.15
0.1
0.05
0
0 0.2 0.4 0.6
Absorbance
protein conc. (%)
Series2
Linear
(Series2)
First of all protein solution is prepared, then by biuret
method calibration chart is plotted. Then this
calibration chart is used for determination of
concentration of permeate. The standard protein
solution is prepared as follows,
1. Preparation of standard BSA solution
Take 50 mg of BSA protein powder in conical flask
and dilute it in 10 ml of distilled water. Then the
standard protein solution i.e. the solution having 0.5 %
concentration will be ready for membrane
characterization. First of all by using this BSA solution
one can plot a calibration curve, which will be helpful
for the analysis of permeate obtained stirred cell
apparatus.
3.2. Analysis of BSA by Biuret Method
a) Preparation of biuret reagent:
Dissolve 9 gms. of sodium potassium tartarate in
approximately 400 ml of 0.2 N NaOH. Dissolve
separately 3 gm of CuSO4.H2O in minimum quantity of
distilled water & transfer slowly with constant stirring
to sodium potassium tartarate. Then add 5 gm of
potassium iodide & adjust the whole solution to 1000
ml by addition of 0.2 N NaOH.
b) Preparation of calibration chart:
Six test tubes were taken. A sample of BSA solution of
0.5% concentration and water were prepared in six test
tubes according to the table given. And four ml of
biuret reagent was added in each test tube. Incubate
this solution at room temperature for ½ an hour and
absorbance was measured at 530 nm for the respective
samples in spectrophotometer. The respective
absorbance with different concentration of protein
solution is shown in table 5.1. Now the absorbance at
the respective concentration is known so the calibration
curve between absorbance and protein concentration is
drawn as shown in figure 1.
Table .1 Calibration chart.
Std
.BS
A
ml
Distille
d
water
ml
Biuret
Reage
nt
ml
Protein
concentrati
on (wt/vol)
%
Absorban
ce
At 530 nm
0.0 1.0 4 0.0 --
0.2 0.8 4 0.1 0.094
0.4 0.6 4 0.2 0.2
0.6 0.4 4 0.3 0.217
0.8 0.2 4 0.4 0.283
1.0 0.0 4 0.5 0.333
Figure 1. Calibration Curve
From this calibration curve concentration of permeate
(less than 0.5% concentration) can be obtained. This
calibration curve has a limitation that conc. more than
0.5% can not be taken in a feed as the curve shows
straight line nature up to 0.5% concentration.
3.3 Stirred cell Apparatus
Construction:
The stirred cell apparatus consist of [1]
a. Cell cylinder
b. Pressure gauge
c. Compressor
d. Magnetic stirrer
A] Cell cylinder: It consists of
a. Pressure inlet: For applying pressure to feed.
b. Pressure release valve: To release pressure in
the cell cylinder.
c. Transparent acrylic body.
d. O – ring: To fit the membrane on membrane
support.
e. Stirring bar: For stirring of solution.
f. Membrane
g. Membrane support: To fit the membrane in
cell cylinder.
h. Filtrate out: To collect the permeate.
B] Pressure gauge: It is used to apply the pressure
inside the cell.
C] Compressor: Compressed air is sent at 1 – 2 kg/cm2
in cell cylinder.
D] Magnetic stirrer: Cell cylinder is mounted on
magnetic stirrer which in tern is used to stir the stirring
bar placed inside the cell cylinder.

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Figure 2. (a) Stirred cell Apparatus schematic diagram
Figure 2.(B)Working model of Stirred cell
ApparatuswithUltrafiltration of BSA Protein solutions.
Working:
Part A: Measurement of Distilled water flux.
Take 50-60 ml of distilled water in stirred cell. Start
magnetic stirrer. Maintain moderate rpm. Start Air
compressor and maintain the pressure on the pressure
gauge as 1 Kg/Cm2 .As soon as the pressure is
developed, start the stopwatch. Note down Time
required to collect 1 ml of permeate. Take 30-40
readings.
Part B: Measurement of BSA Protein solution flux/
milk flux/Whey Flux.
Take 50-60 ml of known concentration of protein
solution/whey/milk as feed solution in stirred cell. Start
magnetic stirrer. Maintain moderate rpm. Start Air
compressor and maintain the pressure on the pressure
gauge as 1 Kg/Cm2 .As soon as the pressure is
developed, start the stopwatch. Note down Time
required to collect 1 ml of permeate. Take 30-40
readings.
Part C: Measurement of volume concentration factor.
The stirred cell experiment as mentioned in
measurement of BSA protein solution flux was
performed. After 5 minutes amount of permeate
collected was noted and after each 4 ml time required
was noted. 3-4 readings were taken.
VCF is calculated by,VCF= volume of feed / volume
of rententate
Part D: Measurement of Rejection
The standard stirred cell experiment for BSA protein
solution was performed and after 4 ml time required to
collect permeate was noted and flux is calculated. The
absorbance of each 4ml permeate was noted and
overall absorbance was noted. Permeate concentration
was calculated from the calibration curve.
The Rejection is calculated by R = 1-Cp / Cf
Where,Cp: Concentration of permeate in % wt / vol
Cf: Concentration of feed in % wt / vol
4.0 MEMBRANE CHARACTERIZATION
1. Thickness:
The thickness of standard UF membrane ranges from
20 – 100 micron. The thickness of casted membrane is
measured with the help of micrometer screw gauge at
different points on the membrane and the average
thickness is calculated. It is used in the measurement of
pore diameter and porosity.
2. Porosity:
Porosity is the ratio of pore volume of the membrane to
the total volume of membrane.
It is calculated as follows,
1. Take wt. of wet membrane (in water).
2. Dry the membrane in oven for few minutes & take
its dry weight.
3. Take the difference & multiply with density of water
that will give you the pore volume of membrane.
4. From area & thickness of membrane calculate
volume of membrane.

8. International Journal of Research in Advent Technology, Vol.2, No.
5. Ratio of pore volume to membrane volume will give
you porosity.
Porosity = pore volume/ membrane volume
5 .0 MATERIALS AND METHODS
5.1. Materials
Polysulfone (PS) in powder form was obtained from
M/s. Gharda Chemicals Company, India. The solvents
used for membrane making are N,N
formamide (DMF) and were of reagent grade.
Polyethylene glycol (PEG), Polyvinyl Pyrrolidone
(PVP K-30) of different molecular weights and
piperazine (AR grade) were locally procured and used
as additives.
5.2. Preparation of membrane
In airtight glass bottle, a specified quantity of polymer
was taken and then a known quantity of
the solvent was added. The solution w
for several hours for complete dissolution.Calculated
quantities of additives were subsequently added and
the solution was homogenizedand kept for deairation.
The solution viscosity was measured using a standard
Brookfield viscometer.The dope solution thus obtained
was spread over a smooth glass plate with the help of a
knife edge. The thickness of the membranes was
controlled by varying the thickness of adhesive tapes at
the sides of the glass plate. The glass plate was kept in
an environment of controlled temperature and humidity
during membrane casting. No deliberate solvent
vaporation period was allowed. The glass plate was
subsequently immersed in a gelling bath, which is
generally demineralized water maintained at a known
temperature otherwise as mentioned in the
text.Immediately phase inversion starts and after
fewminutes thin polymeric film separated out from the
glass. It was repeatedly washed with demineralized
water and wet stored. The actual thickness of the
membranes was measured using a micrometer.
Table 2. Dope solution compositions
Dop
e PS
Compositio
n in Wt. %
PS
Solutio
n DMF
Additiv
M 1 16 84.9
M 2 16 80.6
M 3 16 74.3
E-ISSN: 2321-9637
N-dimethyl
nt was kept agitated
ope ent therwise e 1
Wt. %
Additiv
e 2
Wt. %
0 3.5
4 3.5
10 3.5
Sl No Volume
DW 1 ml
M 1.1
BSA 1 0-5
BSA 2 05--10
BSA 3 10--15
BSA 4 15-20
M 1.2
P Whey1 0-5
P Whey2 05--10
P Whey3 10--15
P Whey4 15-20
Results of M-1
in ml
Time in
Sec
Table 3.Effect of the time on the
Membrane Flux
Figure 3.Effect of the time on the performance of
Membrane Flux
Figure 4.Effect of the time on the performance of
Membrane Flux
3, March 2014
46
performance of
model M 1.1
model M 1.2
Flux
lt/hr.m2
190 20.105
212 18.019
267 14.307
295 12.94
308 12.4
493 7.74
520 7.34
551 6.93
606 6.303

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Table 4. Effect of the Pressure on the performance of
Membrane Flux
Sl No
Pressure
kg/cm2
Time in
Sec
Flux
lt/hr.m2
M1.3
DW 1 0.50 306 12.48
DW 2 1.00 190 20.1
DW 3 1.20 180 21.22
DW 4 1.40 163 23.43
M1.4
BSA 1 0.50 277 13.79
BSA 2 1.00 213 17.93
BSA 3 1.20 185 20.64
BSA 4 1.40 160 23.87
25
20
15
10
5
Figure 5.Effect of the Pressure on the performance of
Membrane Flux M 1.3
30
25
20
15
10
5
Figure 6.Effect of the Pressure on the performance of
Membrane Flux M 1.4
Results of M-2
Table 5.Effect of the time on the performance of
Membrane Flux
Sl No
Volume in
ml
Time in
Sec
Flux
lt/hr.m2
DW 1 ml 19 201.05
M 2.1
BSA 1 0-5 52 73.46
BSA 2 05--10 70 54.57
BSA 3 10--15 90 42.44
BSA 4 15-20 103 37.08
M 2.2
P Whey1 0-5 109 35.046
P Whey2 05--10 151 25.29
P Whey3 10--15 163 23.43
P Whey4 15-20 174 21.95
80
70
60
50
40
30
20
10
Figure 7..Effect of the time on the performance of
Membrane Flux M 2.1
40
35
30
25
20
15
10
5
Figure 8.Effect of the time on the performance of
Membrane Flux M 2.2
M 1.3
0
0.00 0.20 0.40 0.60 0.80 1.00 1.20 1.40 1.60
Pressure in Kg/cm2
F lu x
M 1.4
0
0.00 0.20 0.40 0.60 0.80 1.00 1.20 1.40 1.60
Pressure in Kg/cm2
F lu x
M 2.2
0
0 20 40 60 80 100 120 140 160 180 200
Time in Sec
F lu x
M 2.1
0
0 20 40 60 80 100 120
Time in Sec
Flux

10. International Journal of Research in Advent Technology, Vol.2, No.
Table 6.Effect of the Pressure on the performance of
Membrane Flux
Figure 9. Effect of the Pressure on the performance of
Membrane Flux M 2.3
Figure 10.Effect of the Pressure on the performance of
Membrane Flux M 2.4
Sl No
Pressure
kg/cm2
Time
in Sec
M 2.3
DW 1 0.50 33
DW 2 1.00 19
DW 3 1.20 16
DW 4 1.40 12
M 2.4
BSA 1 0.50 148
BSA 2 1.00 58
BSA 3 1.20 52
BSA 4 1.40 50
E-ISSN: 2321-9637
Results of M-3
Table 7. Effect of the time on the performance of
Membrane Flux
Sl No
Volume
in ml
DW 1 ml
M 3.1
BSA 1 0-5
BSA 2 05--10
BSA 3 10--15
BSA 4 15-20
M 3.2
P Whey1 0-5
P Whey2 05--10
P Whey3 10--15
P Whey4 15-20
Figure 11. Effect of the time on the performance of
Membrane Flux M 3.1
Figure 12. Effect of the time on the performance of
Membrane Flux M 3.2
Flux
lt/hr.m2
115.75
201.05
238.75
318.33
25.81
65.85
73.462
76.4
3, March 2014
48
Time
in Sec
Flux
lt/hr.m2
26 146.92
90 42.44
144 26.52
160 23.87
179 21.34
192 19.89
230 16.6
283 13.49
310 12.32
.

11. International Journal of Research in Advent Technology, Vol.2, No.
Results of M-3
Table 8.Effect of the Pressure on the performance of
Membrane Flux
Sl No
Pressure
kg/cm2
Time
in
Sec
M 3.3
DW 1 0.50 38
DW 2 1.00 26
DW 3 1.20 20
DW 4 1.40 18
M 3.4
BSA 1 0.50 87
BSA 2 1.00 75
BSA 3 1.20 64
BSA 4 1.40 60
Figure 13.Effect of the Pressure on the
Membrane Flux M 3.3
E-ISSN: 2321-9637
Flux
lt/hr.m2
100.52
146.92
191
212.22
43.9
50.93
59.93
63.66
performance of
3, March 2014
Figure 14.Effect of the Pressure on the performance of
Membrane Flux M 3.4
6.0 CONCLUSION AND FUTURE SCOPE
Aseries ofUtrafiltration PS membrane was successfully
casted & performance was studied for M– M
1,M– 2 and
M – 3 (distinction based on polymer concentration and
additive concentration and the effect with different
solvents).Stirred cell operation was performed with
standard Bovoin Serum Albumin (BSA) protein
solution (0.1 % concentration).,Distilled water flux,
Dairy Waste with different pressure range starting from
0.5-1.4 kg /cm2.We have observed that for three
membranes as the time increases flux goes on
decreases due to fouling.Rejection increases with
increase in PS concentration in ultrafiltration
membrane. Presence of additives improves the
viscosity of the solution. The pure water permeation
rate is found to be significantly higher for M
compared to M-1.Incorporation of additives in the
casting solution generally increase the water
permeation rate. It can be observed from the several
castings that exposure to higher ambient humidity
gives more porous membranes with higher water
permeation rate in all the cases it happens due to partial
phase separation during membrane casting. It can be
seen that the permeate flux as well as solute separation
increase in applied pressure range studied.We have
studied two characteristics (thickness, porosity) of
casted membranes & remaining characteristics of the
membrane can be studied in future.
REFERENCES
[1] “Encyclopedia of Polymer science and
Technology” 3rd Edition Vol
[2] Mark C. Potter; Handbook of industrial
membrane technology, No Yes publications.
[3] Mohr; Membrane application and research in
food processing.
[4] Richardson Coulson; chemical engineering,
volume 2, second edition; Tata McGraw hill
publishers, USA.
[5] KatarzyanaMajewska-
1989, Elseveir science publishers, Page no. 83
95.
[6] Synthetuc Polymeric Membrane
,Robert E.Kistinkg and Irvine California, A
Wiley-Interscience Publication
[7] Miss. ShilpaChitnis, Miss. Deval Desai, Miss
VinayaPrabhu; A project report on Kinetic study
of PAN membrane by phase inversion
49
ence M-2 as
eate Vol-3 Page(184-245)
Nowak; Desalination,
–
,2nd Edition
ience inversion, 1997 – 98.

12. International Journal of Research in Advent Technology, Vol.2, No.3, March 2014
E-ISSN: 2321-9637
50
[8] MunirCheryan; Ultrafiltration and Microfiltration
handbook; 1998; Tchnomic publishing company.
[9] Wenli Han, Harry P Gregar, Eli M. Pearce;
Acrylonitrile copolymers, synthesis
characterization and formation of ultrafiltration
membranes; capanneli et al (1983); Page no. 1271
– 1277.
[10] B. W. Baker, Membrane Technology &
Applications, John Wiley & Sons, Ltd.