Iraqi Journal of Chemical and Petroleum Engineering 

 Vol.12 No.1 (March 2011)  
ISSN: 1997-4884 

 

 

Oily Wastewater Treatment Using Expanded Beds of Activated Carbon and 

Zeolite 

Sawsan A. M. Mohammed, Ibtihage Faisal and Maha M. Alwan  

Chemical Engineering Department – College of Engineering – University of Baghdad – Iraq              

 

 

ABSTRACT 

Two types of adsorbents were used to treat oily wastewater, activated carbon and zeolite. The 

removal efficiencies of these materials were compared to each other. The results showed that 

activated carbon performed some better properties in removal of oil. The experimental methods 

which were employed in this investigation included batch and column studies. The former was used 

to evaluate the rate and equilibrium of carbon  and zeolie adsorption, while the latter was used to 

determine treatment efficiencies and performance characteristics. Expanded bed adsorber was 

constructed in the column studies. In this study, the adsorption behavior of vegetable oil (corn oil) 

onto activated carbon and zeolite  was examined as a function of the concentration of the adsorbate, 

contact time, adsorbent dosage and amount of coagulant salt(calcium sulphate) added . The 

adsorption data was modeled with Freundlich and Langmuir adsorption isotherms. and it was found 

that the adsorption process on activated carbon and zeolite fit the Freundlich isotherm model. The 

amount of oil adsorbed increased with increasing the contact time, but longer mixing duration did 

not increase residual oil removal from wastewater due to the coverage of the adsorbent surface with 

oil molecules. It was found that as the dosage of adsorbent increased, the percentage of residual oil 

removal also increased. The effects of adsorbent type and amount of coagulant salt(calcium 

sulphate) added on  the breakthrough curve were studied in details in the column studies. Expanded 

bed behavior was modeled using the Richardson-Zaki correlation between the superficial velocity of the feed 

stream and the void fraction of the bed at moderate Reynolds number. 

Keywords:  Oil removal; adsorption; expanded beds; wastewater treatment; zeolite,   activated 

carbon. 

 

 

Iraqi Journal of Chemical and 

Petroleum Engineering 

 

University of Baghdad 

College of Engineering 



Oily Wastewater Treatment Using Expanded Beds of Activated Carbon and Zeolite 

 

Vol.12 No.1 (March 2011) 

INTRODUCTION 

     One of the most challenging problems 

today is the removal of oil from wastewater. 

large amounts of wastewater are generated by 

industrial companies that produce or handel 

oil and other organic compounds, both 

immiscible and miscible in water. Oily 

wastewater discharged into the environment 

causes serious pollution problems since the 

biodegradability of oil is very low and oily 

wastewater hinders biological processing at 

sewage treatment plants. 

Petroleum and petrochemical plants are 

potential oil sources for pollution inland water 

caused by runoff from oil fields, refineries 

and process effluent [1].  

Removal of dissolved and emulsified oils is 

achieved by using activated carbon or 

membrane filtration. The effluent from those 

operations contains almost no oil. Several 

types of sorbents have been studied for the 

removal of oil from water by a packed bed 

filter such as sawdust, activated carbon, peat, 

bentonite, and organoclay [2]. 

      Current technologies for oil removal 

include filtration, gravity separation, induced 

floatation, ultrafiltration, adsorption, and 

biological treatment. An oil and water mixture 

can be classified as free oil for oil droplets 

larger than 150 μm, dispersed oil with oil 

droplets in the range of 20-150 μm, and 

emulsified oil with oil droplets smaller than 

20 μm. A wastewater, where the oil in the oil-

water mixture is not present in the form of 

droplets is said to be soluble [3]. 

  The principles of liquid-solid fluidization 

have been extensively studied. A key work in 

the field was presented by Richardson and 

Zaki [3] more than 50 years ago. The equation 

predicts a linear correlation between the 

logarithms of superficial fluid velocity (
0

V ) 

and the void fraction of the bed ( )1(
s
 for 

fluidized bed [4]. 

 
ts

VnV log1loglog
0

     ……….    (1)                     

where 
s
 and 

t
V are the solid fraction of the 

expanded bed and the terminal settling 

velocity of the particle at infinite dilution 

 0
s
 , respectively. 

      The superficial velocity 
0

V  is determined 

by dividing the volumetric flow rate of the 

feed stream by the cross sectional area of the 

column.  

The solid fraction 
s
  of the expanded bed at 

height H can be obtained by: 

 
H

H
s

0

0
                   …………      (2)                                        

Where
0
 , and

0
H , are the solid fraction and 

height of the bed at zero flow stream, 

respectively.  

Wen and Yu [5] estimated the terminal 

velocity at moderate Reynolds number using 

the following equation: 

 
p

ll

lp

t
d

g
V

31
22

225

4













 





   ……….... (3) for 

0.4<Re<500   

     The main objective of this research is to 

remove oil from water using activated carbon 

and zeoilte as the adsorbents. The effect of 



Sawsan A. M. Mohammed, Ibtihage Faisal and Maha M. Alwan 

 

 

 Vol.12 No.1 (March 2011) 
 

process variables such as adsorbent dosage, 

contact time, and amount of coagulant 

salt(calcium sulphate) added on the removal 

efficiency of oil was studied in order to 

determine the optimum process conditions. 

The adsorption equilibrium data were 

obtained to investigate which isotherm model 

provided the best fit for the adsorption 

process. 

EXPERIMENTAL PROCEDURE 

      The adsorbents used in this study were 

granular activated carbon and zeolite. The 

characteristics of adsorbents  are reported in 

table (1). 

Table (1): Major characteristics of adsorbents. 

Property Activated 

carbon 

Zeolite  

Density, kg/m
3
 1350 1545 

BET surface area, m
2
/g 1100 630 

Bed porosity 0.45 0.25 

particle diameter (dp), mm 0.8 0.25 

 

Adsorption Isotherm Measurements 

     Oil in water emulsion samples were 

prepared by mixing corn oil in distilled water 

with initial concentrations (C0) ranged 5000-

24000 ppm. Equilibrium studies were 

conducted at room temperatures by 

employing the batch adsorption technique. 

Weighed amounts of adsorbent (2-8  g) were 

taken in conical flasks containing 100 ml of 

oily water of known concentration (ρl=977 

kg/m
3
 for the highest concentration). The 

solutions were agitated at 150 rpm using a 

Teflon coated half-inch bar on a Corning 

magnetic stirrer for a specified period of 

contact time ranged 5-25 min. upon 

equilibrium, the solutions were filtered and 

the concentration of residual oil was 

measured using a UV spectrometer 

(Shimadzu model 160A) with an absorbance 

wavelength of 450 nm.  

 

Column Studies 

      The schematic representation of 

experimental set-up is shown in Fig.(1); it 

consists of a glass column of 2.45 cm internal 

diameter and a height of 75 cm. The column 

was packed with adsorbent to a height of 8 

cm. The adsorbent particles are supported by 

a wire mesh fitted at the column bottom.  

 

 

 

 

 

 

 

 

 

 

 

 

 

 

Fig.1: Schematic diagram of expanded bed 

(1.adsorber, 2 flow meter, 3.pump, 4.feed 

tank, 5. treated effluent tank, 6.sampling 

point, 7.to drain, 8.feed. 

 

The flow rate of wastewater was 50 L/h. The 

effluents from the bed were analyzed for oil 

content at chosen intervals of time until 

breakthrough occurs. The minimum fluidized 

velocity for particles (Vmf) had been estimated  

 

2 

3 

4 

5 

6 

7 

1 

8 



Oily Wastewater Treatment Using Expanded Beds of Activated Carbon and Zeolite 

 

Vol.12 No.1 (March 2011) 

 

to be (1.410 
- 3 

m/s) for activated particles 

and (2.110 
– 4

 m/s) for zeolite using the 

following equation [6]: 

 

 

 
 

















 7.330408.07.33

2

3

2

l

lplp

lp

l

mf

gd

d
V







 ….…   (4)                                     

 

 

The height of the bed was measured over a 

certain range of feed velocities. 

 

RESULTS AND DISCUSSION 

 

Adsorption Isotherms 

The successful representation of the dynamic 

adsorptive separation of solute from solution 

onto an adsorbent depends upon a good 

description of the equilibrium separation 

between the two phases. 

 

Adsorption equilibrium is the amount of 

solute being adsorbed onto the adsorbent. At 

this point, the equilibrium solution 

concentration remains constant. By plotting 

solid phase concentration against liquid phase 

concentration, it is possible to depict the 

equilibrium adsorption isotherm. Fig.(2) 

shows the equilibrium values of oil adsorbed 

per unit weight of adsorbent qe versus the 

liquid phase sorbate concentration at 

equilibrium Ce. It can be seen that the 

adsorption capacity increased until an 

equilibrium concentration was obtained. This 

confirms a favorable adsorption system. 

Fig.2 :Equilibrium adsorption of oil on activated 
carbon and zeolite at 30°C with 2 grams of 
adsorbent and a mixing time of 20 min. 

 

      There are many theories relating to 

adsorption equilibrium [7],[8],[9].The 

isotherms of the oil adsorption by activated 

carbon and zeolite were represented by 

applying the Freundlich and Langmuir 

adsorption models. 

 

 

Langmuir isotherm 

     The Langmuir isotherm theory assumes 

monolayer coverage of adsorbate over a 

homogenous adsorbent surface. Therefore, at 

equilibrium, upon reaching a saturation point, 

no further adsorption can occur. In equation 

(5), qo is the maximum amount of adsorption 

corresponding to complete monolayer 

coverage and   KL is the Langmuir constant . 

  eL

eo

e
CK

Cq
q


       ………..    (5)                                 

                                                                

The linea r expression of Eq. (5) can be 

written in the following form:  

0

1

2

3

4

5

6

7

8

9

10

0 5000 10000 15000

qe
mg/g

Ce (ppm)

activate
d carbon
zeolite



Sawsan A. M. Mohammed, Ibtihage Faisal and Maha M. Alwan 

 

 

 Vol.12 No.1 (March 2011) 
 

e

ooLe

e
C

qqKq

C












11
     ………  (6)                                                     

A linearized plot of (
ee

qC ) vs. Ce is shown 

in Fig. (3). 

     It was found that in Fig. (3), the Langmuir 

isotherm did not fit the data with a correlation 

coefficient much lower than 1.0 throughout 

the experimental range of oil concentrations 

studied for both activated carbon and zeolite.  

The Langmuir equation is applicable to 

homogeneous sorption where the sorption of 

each molecule has equal sorption activation 

energy.  

 
 

 

Fig.3: Linearized Langmuir isotherm for oil 
adsorption by activated carbon and zeolite. 

 

Freundlich isotherm 

     The Freundlich expression is an 

exponential equation and therefore, assumes 

that the amount of adsorbate adsorbed 

increases infinitely with an increase in 

concentration.  

       
fn

eFe
CKq

1
    ……….    (7)                                                                           

 

      In this equation, KF and 1/nf are the 

Freundlich constants. This expression is 

characterized by the heterogeneity factor, 1/nf, 

and thus the Freundlich isotherm may be used 

to describe heterogeneous system 

[10],[11].To determine the constant KF and 

1/nf, the linear form of the equation as shown 

below may be used to plot ln(qe) against ln 

(Ce) as: 

       

      
efFe

CnKq ln1lnln    ………     (8)                                        

 Fig. (4) Shows the Freundlich plot and gives 

a straight line. It is clearly shown that the 

Freundlich isotherm model fits the analyzed 

data well  for both adsorbents with correlation 

coefficient (R
2
) values of 0.9601 for activated 

carbon and 0.8949 for zeolite. The isotherm 

for activated carbon is represented as: 

      
988.03

109.1
ee

Cq


           ……….    (9)                                                                    
     

    

                       

     The Freundlich model assumes that the 

uptake of any adsorbate occurs on a 

heterogeneous surface by multilayer 

adsorption and that the amount of adsorbate 

adsorbed increases infinitely with an increase 

in concentration. The heterogeneity factor 1/nf 

was 0.988 and nf value was 1.012. it is known 

that when the nf value is greater than 1.0, 

conditions are favorable to adsorption. 

Freundlich isotherm for zeolite is represented 

as: 

957.04
108.3

ee
Cq


    ……….     (10)                                                            

Hence it is clearly proved that oil adsorption 

by activated carbon and zeolite agrees well 

with the Freundlich adsorption model. 

R² = 0.193

3000

3500

4000

4500

0 10000 20000

C
e
/q

Ce (ppm)

zeolite

R² = 0.250

400

500

600

700

0 2000 4000 6000 8000

C
e
/q

Ce(ppm)

activated 
carbon



Oily Wastewater Treatment Using Expanded Beds of Activated Carbon and Zeolite 

 

Vol.12 No.1 (March 2011) 

 

 

 

Fig.4: Linearized Freundlich isotherm for oil adsorption by activated carbon and 

zeolite. 

 

Table (2): Freundlich and Langmuir parameters of adsorption isotherms for the 

removal of oil by activated carbon and zeolite. 

  

 Freundlich isotherm Langmuir isotherm 

Adsorbent  nf (-) KF 

(g/l)
1/nf

 

Correlation 

coeff. (R
2
) 

qo(mg/g) KL(g/l) Correlation 

coeff. (R
2
) 

Activated 

carbon 

1.012 1.9*10
-3 

0.9617 55.25 3.6*10
-5 

0.2504 

Zeolite  1.04 3.8*10
-4 

0.8949 19.01 1.5*10
-5 

0.1934 

 

 

Effect of Mixing  Time 

 In the adsorption systems contact time plays 

an important role. In order to study the 

kinetics and dynamics of adsorption of oil by 

activated carbon and zeolite, the adsorption 

experiments were conducted and the extent of 

oil removal was obtained at various contact 

time ranged 5-25 min at fixed oil 

concentration ( 24000  ppm) with a fixed 

dosage of adsorbent (2 g) and 150 rpm.  

 

The influence of contact time on residual oil 

removal using activated carbon and zeolite as 

adsorbents is shown in Fig.(5) . By increasing 

contact time, the residual oil molecules have a 

longer residence time for adsorption on the 

adsorbent surface area. At equilibrium, the 

surface of the adsorbent was covered with oil 

molecules; therefore a longer mixing time 

does not increase residual oil removal from 

y = 0.988x -2.717
R² = 0.961

y = 0.957x -3.410
R² = 0.894

-0.4

-0.2

0

0.2

0.4

0.6

0.8

1

1.2

3 3.5 4 4.5 5

lo
g

 q
e

log Ce

activated 
carbon

zeolite



Sawsan A. M. Mohammed, Ibtihage Faisal and Maha M. Alwan 

 

 

 Vol.12 No.1 (March 2011) 
 

wastewater. Fig.(5) shows that when the 

mixing time was increased from 20 min. to 25 

min., the reduction value of residual oil was 

only increased by less than 1000 ppm for 

activated carbon while the value of residual 

oil remains unchanged at  10000 ppm  for 

zeoilte. This indicates that zeoilte became 

saturated faster than activated carbon. 

 

 

 

 

Fig.5: The influence of mixing time on the 

sorption of residual oil with 2g of adsorbent at 

30°C and 150 rpm. 

Effect of Adsorbent Loading 

     Different quantities of adsorbent were 

added to oily water samples ranged 2-8 g with 

initial concentration of oil 20000  ppm and 

contact time 20 min. It was found that as the 

dosage of adsorbent was increased, the 

percentage of residual oil removal also 

increased, as shown in Fig.(6). Adsorption is 

a surface related phenomenon, at equilibrium 

most of the oil molecules were adsorbed on 

the surface and in the intermolecular pores of 

the adsorbent. It takes about 8 g of activated 

carbon to reduce the initial residual oil 

concentration of 20000 ppm to a final 

concentration of zero ppm while the final 

concentration is 10000 ppm for the same 

weight of zeolite. Similar observation has 

been reported by Ahmed et al [1]. 

 

 

Fig. 6: Effect of dosage of adsorbent on the 

reduction of residual oil at a mixing time of 

20 min. at 30°C. 

Expanded Bed Experiments 

Break-through Curve 

     Successful design of a column adsorption 

process requires prediction of the 

concentration-time profile or breakthrough 

curve for the effluent.  

Effect of adsorbent type 

     Based on Fig. (7), activated carbon  

performed better adsorption properties than 

zeolite in the removal of oil. Activated carbon 

differs in their adsorption efficiencies. It is 

very important to know the nature of 

pollutants to be removed from contaminated 

0

5000

10000

15000

20000

25000

30000

0 10 20 30

R
e

si
d

u
a

l 
o

il
 c

o
n

ce
n

tr
a

ti
o

n
(p

p
m

)

time (min)

activated 
carbon

zeolite

0

2000

4000

6000

8000

10000

12000

14000

16000

18000

0 5 10

R
e

si
d

u
a

l o
il

 c
o

n
ce

n
tr

a
ti

o
n

 (
p

p
m

)

Wt. of absorbant (g)

activated 
carbon

zeolite



Oily Wastewater Treatment Using Expanded Beds of Activated Carbon and Zeolite 

 

Vol.12 No.1 (March 2011) 

media before deciding what a specific sorbent 

to select. In many applications, an activated 

carbon exhibits a sufficient capacity towards 

existing, especially organic water pollutants, 

however zeolite may adsorb some metals and 

ammonia more selectively [12]. 

 

 

 

 Fig. 7: Effect of adsorbent type and  the 

amount of coagulant salt on breakthrough 

curve (C0=24000 ppm, Q=50 L/hr). 

Effect of the amount of coagulant salt 

     Data for the ratio of oil concentration at 

the outlet of the bed and the concentration of 

the inlet stream (C/C0) as a function of time, 

for beds with varying amounts of coagulant 

salt are shown in Fig.(7). It is observed that 

the addition of  higher amount of calcium 

sulphate is essential to achieve larger oil 

removal. The dissolved salt ions compress the 

electric double layer around droplets, 

neutralize repulsive forces among them and 

between droplets and activated carbon 

particles and, hence, enhance coalescence of 

oil droplets. Moreover, the lack of 

electrostatic repulsion improves the physical 

adsorption of the oil droplets on the carbon 

surface. The oil droplet size is increased and 

its charge neutralized, so that the disperse 

phase can be retained in the filter media 

interstices. Furthermore, some authors have 

pointed out that calcium salts activates the 

sorption sites of sorbent materials in the 

removal of different unwanted materials from 

water [13] , [14].   

The Richardson-Zaki exponent constant  

        The effects of superficial velocity (
0

V ) 

of the feed stream on the bed expansion (

0
HH ) were measured. The bed expansion 

factor was limited below 4 as recommended 

by Reichent et al.[15], for proper performance 

of expanded beds. 

 

Fig.8:Effect of the superficial velocity of fluid 

on the bed expansion. 

Although Coulson et al.[16], provided 
0s

 , 

values for spherical particles of various sizes, 

 
0s

 value for the bed was measured as 

0

0.1

0.2

0.3

0.4

0.5

0.6

0.7

0.8

0.9

1

0 20 40 60

C
/C

0

t (min)

activated 
carbon

zeolite

activated 
carbon +2g 

CaSO4.2H2O

activated 
carbon +4g 

CaSO4.2H2O

0

0.5

1

1.5

2

2.5

3

3.5

0 0.01 0.02 0.03 0.04

H/H0

V0(m/s)

activated 
carbon

zeolite



Sawsan A. M. Mohammed, Ibtihage Faisal and Maha M. Alwan 

 

 

 Vol.12 No.1 (March 2011) 
 

follows. In the column the particles were 

settled  

in distilled water. The water contained inside 

the void fraction of the sedimented bed was 

drained off. The volume of the drained water 

was measured and divided by that of the total 

sedimented bed to determine the void 

fraction,  of the bed. Finally,  
0s

 values 

determined by 1-  were 0.55 for activated 

carbon and 0.75 for zeolite [17]. 

      Fig.(9) shows the Richardson – Zaki plot 

for the experimental data. The line in the 

figure have a slope (n value) of 3.27 and the 

terminal velocity is 0.063 m/s for activated 

carbon and (n) value of 1.311 and the terminal 

velocity is 0.017 m/s for zeolite. 

 

 

 

Fig.9: Richardson-Zaki plot  for the bed 

expansion  

     The exponent n is a function of terminal 

particle Re. Based on bed expansion data, the 

equation recommended for the range of 

terminal particle Re  used is [18],[19]: 

  
1.0

Re45.4


n   for 1< Re <500  ……...  (11)                              

The validity of Richardson- Zaki equation has 

been confirmed with the experimental data for 

activated carbon better than for zeolite (ncalc.= 

3.08 for carbon and ncalc.= 4.88 for zeolite). 

This allow further investigation of the 

hydrodynamics for zeolit system such as to 

predict segregation phenomena in the 

expanded bed. 

   Fig. (10) demonstrates that the calculated 

bed expansion, (
0

HH ) cal using   Eqs. (3) 

and (1) are in good agreement with 

experimentally measured values of the bed 

expansion (
0

HH ) exp for activated carbon 

more than that for zeolite. 

 
Fig.10: Comparison of bed expansion 

calculated (H/H0) cal, with those of  

experimentally determined values, 

(H/H0) exp.  

 

 

CONCLUSIONS 

   The following conclusions are drawn from 

the above-discussed results: 

1. The adsorption process of oil on 
activated carbon and zeolite fits well 

with Freundlich isotherm. 

2. The amount of oil adsorbed increased 
with the increase in contact time. At 

equilibrium, the surface of the 

adsorbent was covered with oil 

y = 3.266x -1.206
R² = 0.982

y = 1.311x -1.762
R² = 0.976

-3

-2.8

-2.6

-2.4

-2.2

-2

-1.8

-1.6

-1.4

-1.2

-1

-0.36 -0.31 -0.26 -0.21 -0.16 -0.11 -0.06 -0.01

lo
g

V
0

log(1-Фs)

activated 
carbon

zeolit

1

1.5

2

2.5

3

3.5

4

1 1.5 2 2.5 3 3.5

(H
/H

0
) 

ca
l.

(H/H0)exp

activated 
carbon

zeolite



Oily Wastewater Treatment Using Expanded Beds of Activated Carbon and Zeolite 

 

Vol.12 No.1 (March 2011) 

3. molecules; therefore a longer mixing 
time does not increase residual oil 

removal from wastewater. 

4. It was found that as the dosage of 
adsorbent was increased, the 

percentage of residual oil removal also 

increased. 

 

For expanded bed experiments 

 

 

1. Activated carbon  performed better 
adsorption properties than zeolite in 

the removal of oil 

      

2. It is observed that the addition of 
higher amount of calcium sulphate is 

essential to achieve larger oil removal.  

      The break point time is obtained                                   

earlier without the addition of the 

coagulant. 

 

3. The validity of Richardson-Zaki 
equation has been      confirmed  with 

the experimental data for activated 

carbon better than for zeolite. 

 

 

NOMENCLATURE 

C The concentration of oil at time t (ppm) 

C0The concentration of oil at time zero    

(ppm) 

Ce     Equilibrium concentration of oil (ppm) 

p
d    Particle diameter (m) 

g       Acceleration of gravity (m/s
2
) 

H      Height of the expanded bed (m) 

0
H    Height of bed at zero flow stream (m) 

KF       Freundlich constant(g/l)
1/nf

  

KL        Langmuir constant (g/l) 

 n  Richardson- Zaki exponent constant (-) 

1/nf      Heterogeneity factor 

qe        Amount of oil adsorbed per unit  

weight of adsorbent (mg/ g) 

q0  Maximum amount of adsorption (mg/g) 

0
V     Superficial velocity (m/s) 

mf
V  Particle minimum fluidization velocity 

(m/s)  

t
V     Terminal settling velocity (m/s) 

Re    Particle Reynolds number (-) 

Greek letters 

l
    Density of fluid (kg/m

3
) 

s
   Density of particle (kg/m

3
) 

l
  Dynamic viscosity of fluid (kg/m.s) 

s
        Solid fraction of the expanded bed (-)    

0
        Solid fraction of the bed at zero flow 

stream (-) 

          Void fraction of the bed (-) 

  

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and Sumathi S., 2005"Adsorption of 

Residual oil from Palm Oil Mill 

Effluent Using Rubber Powder", 

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pp.371-379.  

2. Alther G. R., 1995"Organically 
Modified Clay Removal Oil From 

Water", Waste Management, V.15, 

No.8, pp.622-628. 



Sawsan A. M. Mohammed, Ibtihage Faisal and Maha M. Alwan 

 

 

 Vol.12 No.1 (March 2011) 
 

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Oily Wastewater Treatment Using Expanded Beds of Activated Carbon and Zeolite 

 

Vol.12 No.1 (March 2011) 

 

 

 

معالجة مياه التصريف السيتية باستخذام اعمذة االمتساز المتمذدة مه الكاربون المنشط 

 والسيواليت

:الخالصة  

حٌ في هزٓ اىذساست ٍعاىجت ٍيآ اىخصشيف اىضيخيت بىاسطت االٍخضاص عيى اىناسبىُ اىَْشط واىضيىاليج واسخخذٍج طشيقت 

حيث اسخخذٍج االوىى اليجاد ٍعذه وعالقت االٍخضاص ىيضيج عيى . االٍخضاص رو اىذفعاث وباسخخذاً االعَذة اىَخَذدة

اىَخغيشاث اىخي حٌ دساسخها . اىناسبىُ اىَْشط واىضيىاليج بيَْا اسخخذٍج اىثاّيت اليجاد مفاءة عَييت اىَعاٍيت وايجاد االداء

صيج )ىضيىث اىْباحيت هسيىك االٍخضاص   في هزٓ اىذساست ، حٌ فحص. هي حشميض اىَادة اىََخضة واىضٍِ ومَيت اىَادة اىَاصة

 (مبشيخاث اىناىسيىً)مَيت اىَيح و ة  اىََخضمَيت اىَادةعيى اىنشبىُ اىَْشط واىضيىاليج مذاىت ىيخشميض ، و (اىزسة

 ٍعادىت فشويْذىش ووجذ أُ. وىْنَيش فشوّذىيخش حٌ حَثيو اىْخائج باسخخذاً عالقاث االٍخضاص ثابخت دسجت اىحشاسة .ضافاىٌ

 . اىضيىاليجو اىنشبىُ اىَْشط عيى حضاص عَييت االًحْطبق عيى

حٌ . اُ مَيت اىضيج اىََخض حضداد ٍع صيادة صٍِ اىخَاط ومزىل وجذ اُ صيادة اىَادة اىَاصة سخضيذ ٍِ ّسبت اصاىت اىضيج

 .ايضا دساست حاثيش ّىع اىَادة اىَاصة اىَسخخذٍت عيى ٍْحْي اىَقاوٍت

 صامي بيِ اىسشعت اىفشاغيت واىجضء اىبيْي ىيعَىد في –حٌ حَثيو حصشف االعَذة اىَخَذدة باسخخذاً ٍعادىت سيخشاسدسِ 

 .حذود ٍعخذىت ٍِ سقٌ سيْىىذص

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 



Sawsan A. M. Mohammed, Ibtihage Faisal and Maha M. Alwan 

 

 

 Vol.12 No.1 (March 2011)