FILTRATION

IntroductionFiltration may be defined as the separation of solids from liquids by passing a suspension through a permeable medium which retains the particles.

Figure 1. Schematic diagram of filtration system

The fine apertures necessary for filtration are provided by fabric filter cloths, by meshes and screens of plastics or metals, by beds of solid particles .

In some cases, a thin preliminary coat of cake, or of other fine particles, is put on the cloth prior to the main filtration process .

Types of filtration

1. Surface filters

2. Depth filters

1.Surface filtersused for cake filtration in which the

solids are deposited in the form of a cake on the up-stream side of a relatively thin filter medium.

Figure2. Mechanism of cake filtration

2.Depth filtersused for deep bed filtration in which

particle deposition takes place inside the medium and cake deposition on the surface is undesirable.

Figure 3. Mechanism of deep bed filtration

The fluid passes through the filter medium, which offers resistance to its passage, under the influence of a force which is the pressure differential across the filter .

rate of filtration = driving force/resistance

The filter-cake resistance is obtained by multiplying the specific resistance of the filter cake, that is its resistance per unit thickness, by the thickness of the cake.

The resistances of the filter material and pre-coat are combined into a single resistance called the filter resistance .It is convenient to express the filter resistance in terms of a fictitious thickness of filter cake. This thickness is multiplied by the specific resistance of the filter cake to give the filter resistance.

Factor affected on filtration

Pressure drop ( ∆P ) Area of filtering surface ( A ) Viscosity of filtrate ( v ) Resistance of filter cake ( α ) Resistance of filter medium ( R m ) Properties of slurry ( μ , ฯลฯ )

rate of filtration = driving force/resistance

-(P) or Pressure

drop

Filter cake ()

Filter medium (Rm)

Viscosity ()

Filtration Equation Flow of fluid through packed bed : Application of

Carman-kozeny’s equation

โดย k1 = constant = 4.17 for particles with definite size and shape

= viscosity of filtrate (Pa.s)v = linear velocity based on filter area

(m/s) = void fraction หรือ porosity of cakeL = thickness of cake (m)S0 = specific surface area of

particle area per volume of solid particle (m2/m3)

Pc = pressure drop in cake (N/m2)

3

20

21 )1(

svk

L

Pc

Substitute v in term of volume (V)

A = filter area (m2) V = volume of filtrate at t sec L = thickness of filter cake Cs = kg of solid/m3 of filtrate

P = density of solid particle in cake (kg/m3)

A

dtdVv

Substitute L in term of height of cake (L)

Obtain:

p

s

A

VCL

)1(

ms RAVCP

dt

dV

A

1

Specific cake resistance ()

โดย = Void fraction S0 = specific surface area of

particle (m2)

)Pressure,,( 0Sf

nP)(0

nP)(10

Specific cake resistance; Their specific resistance change with pressure drop across the cake ∆pc. In such cases, an average specific cake resistance av should can be determine from

If the function = (∆pc) is known from pilot filtration tests, bomb filter test or from the use of a compressibility cell.

An experimental empirical relationship can be used over a limit pressure range

Where 0 : the resistance at unit applied pressure drop

n : a compressibility index obtained from experiments

(n = 0 for incompressible substance)

n

cp )(0

nPc)(10

Filter medium resistance; R

Normally be constant but may vary with time (as a result of some penetration of solid into the medium) and sometimes may also change with applied pressure (because of the compression of fiber in the medium).

As the overall pressure drop across an installed filter include losses not only in the medium but also in the associated piping and in the inlet and outlet ports

It is convenient in practice to include all these extra resistances in the value of the medium resistance R.

Constant pressure filtration Equation is useful because it covers a

situation that is frequently found in a practical filtration plant.

We could predict the performance of filtration plant on the basis of experimental results.

If a test is carried out using constant pressure, collecting and measuring the filtrate at measured time intervals

Filtration Equations for Constant – Pressure Filtration

At t = t secAt t = t sec

PRm

A

V

P

Cs

AV

t

2/

Determine and Rm

Filtration equation for Constant rate Filtration

For incompresible cake: Kv and C are constant

dV/dt = constant = V/t

P

t

Slope Y-intercept

From constant rate equation the pressure drop required for any desired flow rate can be found. Also, if a series of runs is carried out under different pressures, the results can be used to determine the resistance of the filter cake.

Ex1. Constant pressure

Filtration area = 0.01 m2 A

Solution density = 1,062 kg/m2

Solution viscosity = 1.610-3 Pa.s

Filtration pressure = 200 kPa P

Solid concentration = 3 kg/m3 Cs

Determine specific filter cake resistance and filter medium resistance

Time (sec)Time (sec) Volume (cmVolume (cm33))

00 00

1414 400400

3232 800800

5555 12001200

8080 16001600

107107 20002000

Y = aX + C

Y axis = tA/V

X axis = V/A

Slope = Cs/2P

Y intercept = Rm/P

The solution

Time (sec)Time (sec) Volume (cmVolume (cm33)) Volume (mVolume (m33)) tA/VtA/V V/AV/A

00 00 00 00 00

1414 400400 0.00040.0004 350350 0.040.04

3232 800800 0.00080.0008 400400 0.080.08

5555 12001200 0.00120.0012 458.33458.33 0.120.12

8080 16001600 0.00160.0016 500500 0.160.16

107107 20002000 0.00200.0020 535535 0.200.20

y = 1175x + 307.67

R2 = 0.9912

0

100

200

300

400

500

600

0 0.05 0.1 0.15 0.2 0.25

V/A

tA/V

kgm

P

CsSlope

/10792.9

1175)10200(2

)3()106.1(

11752

10

3

3

mR

R

P

Rercepty

m

m

m

/110845.3

67.30710200

)106.1(

67.307int

10

3

3

Ex2. Constant rate

A slurry containing 25.7 kg dry solids/m3 of filtrate across the filter medium area 2.15 m2 at a constant rate of 0.00118 m3/s. If the pressure drop was observed 4,000 and 8,500 Pa after 150 and 450 seconds of filtration, respectively. The viscosity of filtrate was 0.001 Pa.s

Determine the specific cake resistance and filter medium resistance.

t

V

A

Rmt

t

V

A

CsP

At

RmV

tA

CsVP

tRm

AV

Cs

PAV

dtRm

AV

Cs

PAdV

tConsRm

AV

Cs

PA

dt

dV

.

tan

2

2

2

2

The solution

P (Pa)

t (sec)

t

V

A

Rercepty

t

V

A

CsSlope

m

int

2

2

(1)

(2)

(4)

(3)

y = 15x + 1750

R2 = 1

0

1000

2000

3000

4000

5000

6000

7000

8000

9000

0 100 200 300 400 500

t (sec)

P (

Pa)

P (Pa)P (Pa) t (sec)t (sec)

4,0004,000 150150

8,5008,500 450450

mR

R

t

V

A

Rercepty

kgm

t

V

A

CsSlope

m

m

m

/110189.3

175015.2

)00118.0()001.0(

1750int

/10938.1

1515.2

)00118.0)(7.25()001.0(

15

9

9

2

2

2

2

Filtration Equipment

The basic requirements for filtration equipment are:

mechanical support for the filter medium

flow accesses to and from the filter medium

provision for removing excess filter cake.

In some instances, washing of the filter cake to remove traces of the solution may be necessary.

Pressure can be provided on the upstream side of the filter, or a vacuum can be drawn downstream, or both can be used to drive the wash fluid through.

Filtration equipment: (a) plate and frame press (b) rotary vacuum filter (c) centrifugal filter

1.Plate and frame filter press

In the plate and frame filter press, a cloth or mesh is spread out over plates which support the cloth along ridges but at the same time leave a free area, as large as possible, below the cloth for flow of the filtrate.

The plates with their filter cloths may be horizontal, but they are more usually hung vertically with a number of plates operated in parallel to give sufficient area.

In the early stages of the filtration cycle, the pressure drop across the cloth is small and filtration proceeds at more or less a constant rate.

As the cake increases, the process becomes more and more a constant-pressure one and this is the case throughout most of the cycle.

When the available space between successive frames is filled with cake, the press has to be dismantled and the cake scraped off and cleaned, after which a further cycle can be initiated.

The plate and frame filter press is cheap but it is difficult to mechanize to any great extent.

Filtration can be done under pressure or vacuum. The advantage of vacuum filtration is that the pressure

drop can be maintained whilst the cake is still under atmospheric pressure and so can be removed easily.

The disadvantages are the greater costs of maintaining a given pressure drop by applying a vacuum and the limitation on the vacuum to about 80 kPa maximum.

In pressure filtration, the pressure driving force is limited only by the economics of attaining the pressure and by the mechanical strength of the equipment

BAS stainless steel plate and frame filter press

2.Rotary filters

In rotary filters, the flow passes through a rotating cylindrical cloth from which the filter cake can be continuously scraped.

Either pressure or vacuum can provide the driving force, but a particularly useful form is the rotary vacuum filter.

The rotary vacuum drum filter

A suitable bearing applies the vacuum at the stage where the actual filtration commences and breaks the vacuum at the stage where the cake is being scraped off after filtration. Filtrate is removed through trunnion bearings.

Rotary vacuum filters are expensive, but they do provide a considerable degree of mechanization and convenience.

3.Centrifugal filters

Centrifugal force is used to provide the driving force in some filters.

These machines are really centrifuges fitted with a perforated bowl that may also have filter cloth on it.

Liquid is fed into the interior of the bowl and under the centrifugal forces, it passes out through the filter material.

Centrifugal filters

4.Air filters Filters are used quite extensively to

remove suspended dust or particles from air streams.

The air or gas moves through a fabric and the dust is left behind. These filters are particularly useful for the removal of fine particles.

The air passing through the bags in parallel. Air bearing the dust enters the bags, usually at the bottom and the air passes out through the cloth

A familiar example of a bag filter for dust is to be found in the domestic vacuum cleaner. Some designs of bag filters provide for the mechanical removal of the accumulated dust.