Al-khwarizmi 
Engineering   

Journal 

Al-Khwarizmi Engineering Journal, Vol. 4,  No. 2, PP 1- 9 (2008) 

 

 

Hydrodynamics, Mass and Heat Transfer  

in Reactive Distillation 
 

Dr. Majid  S. Radhaa, Dr. Khalid  A. Sukkar
*
, Dr. Jamal  M. Ali,  

Dr. Zaidoon M. Shakoor, and Niran Manwel 
*Department of Chemical Engineering, University of Technology, Baghdad, Iraq 

 

(Received 17 Septemper 2007; accepted 13 February 2008) 

 

 

Abstract 

      The ethyl acetate synthesis via heterogeneous reactive distillation is studied experimentally using ethanol and acetic 

acid. Three types of cation exchanging resins were used as catalysts: Zerolit 225, Zerolit 226 and Ambylite 400. 

Experiments were carried out in two units of the same dimensions. Each unit consisted of three sections: rectifying, 

reactive and stripping sections of heights (60+25+20) cm respectively and 2.5cm column diameter. The first unit 

(column-A-) was a fractionation type and the second unit (column-B-) was packed column. The packing type was 
hollow glass cylinders with 10 mm height, and 4, 5 mm inner and outer diameter respectively.  

      The experiments were carried out by using two operation modes. The semi-batch and continuous operation mode. 

In the first part of present investigation, the semi-batch mode was used to evaluate the catalyst type and to evaluate the 

performance of reactive distillation unit configuration (Fractionation and packed column). Results show that, the 

column-B- gave higher conversion rates than column-A-. This is attributed to the high surface area available for liquid 

vapour contact in packed type column, which leads to increasing mass transfer rates.  On the other hand, Ambylite 400 

catalyst showed higher activity for esterification reaction than other two types of catalysts.  

      The second part of work continued with column -B- only. It is well known that, the esterification process is 

regarded one of exothermic reactions. Therefore, the monitoring of the temperature distribution along column axial for 

all three types of catalysts showed that the temperature distribution was essentially the same due to steady state 

operation in continuous operation mode. On the other hand, the effect of reflux ratio on temperature distribution was 
clearly noted, that is as the reflux ratio increased the temperature distribution along the column was reduced for each 

type of catalysts. 

      On the other hand, the experimental results point that, as a reflux ratio increases the conversion rates of acetic acid 

is increased too because such increasing is related to high mass transfer rates between  vapour and liquid along reactive 

distillation column.  

 

Keywords: Reactive Distillation; Esterification; Ethyl acetate; Heterogeneous Catalysts.  

 

 

Introduction 
      The combination of chemical reaction with 

distillation in only one unit is called reactive 

distillation [1]. The performance of reaction with 
separation in one piece of equipment offers 

distinct advantages over the conventional, 

sequential approach. Especially for equilibrium 
limited reactions such as etherification, 

esterification and ester hydrolysis reactions, 

conversion can be increased far beyond chemical 

equilibrium conversion due to the continuous 
removal of reaction products from the reactive 

zone. This may lead to an enormous reduction of 

capital   and investment costs and may be 

important for sustainable development due to a 
lower consumption of resources. Therefore, the 

main advantages of reactive distillation 

equipment can be summarized as follows [2, 3]: 

- higher conversion, selectivity and yield 
- avoid equilibrium restrictions 

- removal of side reactions 

- removal of recycling streams 
- avoidance of non-reactive azeotropes 

- reduction of number of units (investment cost) 

- reduction of energy demands (heat integration). 
      Figure (1) shows the general construction of 

reactive distillation unit, which includes three 



Khalid  A. Sukkar                              Al-Khwarizmi Engineering Journal, Vol. 4, No. 2, PP 1-9 (2008) 

 

 2 

main sections named rectifying, reactive and 
stripping sections [2]. 

      Esters are an important class of chemicals, 

having applications in a variety of areas such as 
solvents, plasticizers, pharmaceuticals and 

intermediates. Among them, ethyl acetate 

(EtAc) is an important organic solvent widely 

used in the production of varnishes, ink, 
synthetic resins, and adhesive agents. This ester 

is typically produced from the reaction of acetic 

acid (HAc) and ethanol (EtOH) [4,5]. 
  

  

 
 

Fig. 1. General Construction of Reactive 

Distillation. 
 

      Both homogenous and heterogeneous 

catalysts could be used in reactive distillation 
column to produce EtAc. Sulfuric acid is 

generally used in homogenous catalysis. 

Heterogeneously catalyzed reactions involve the 
use of acidic polymeric catalysts such as ion 

exchange resins. However, the use of 

heterogeneous catalysts has become more 

common in recent times because of its significant 
advantages over homogenous catalyst. The use of 

heterogeneous catalyst allows for easy and 

inexpensive product removal from reaction 
mixture by filtration or centrifugation. Moreover, 

heterogeneous catalyst can withstand a wider 

range of temperatures and pressures [1, 5]. 

      The overall reaction between acetic acid and 
ethyl alcohol over a catalytically active resin is 

as follows: 

   

 

    This reaction is reversible, and the equilibrium 
composition is a weak function of temperature. 

The reaction is acid catalyzed by using the cation 

exchange resins catalysts [2, 3, 5]. 
      Tang et al. [6] studied the process which 

contains sulfuric acid as catalyst (homogeneous 

reaction) using an reactive distillation column 

with an overhead decanter and a stripping 
column. Highly pure EtAc product was obtained 

and all the outlet streams met product and 

environmental specifications. Tang et al. [7] 
provide generalization for the study of design of 

reactive distillation with acetic acid as one feed. 

Chang and Seider [8] concluded that a 

continuous reactive distillation column cannot 
produce pure ethyl acetate at the top due to the 

ternary minimum boiling azeotrope of ethyl 

acetate, ethanol and water, which prevents a 
desired overall reaction conversion. Bock et al. 

[9] propose a different configuration of a 

reactive distillation column followed by a non-
reactive recovery column to produce pure ethyl 

acetate under excess reactants. 

      Research in catalysis by ion exchange resins is 

undoubtedly interesting, not only from a purely 
physicochemical point of view but also in terms of 

the advantages of these types of catalyst over the 

conventional ones. Ion exchange resins increase 
the product yield, keep their activity a long time, 

and do not pollute. Ion exchange resins separate 

from reaction media easily and they regenerate 
easily for reuse in chemical processes [10,11, 12, 

13].  

However, there is a limited work in literature 

about the performance of reactive distillation 
column that uses heterogeneous catalysts. On the 

other hand, the design, operation and optimization 

of reactive distillation require the knowledge of 
the hydrodynamics, mass as well as heat transfer 

characteristics and their interactions. Therefore, 

due to the complex interactions between chemical 

reaction,  heat, and mass transfer, the  present 
work aims to study the performance of reactive 

distillation column in esterification reaction to 

produce ethyl acetate by using heterogeneous 
catalysts. 

 

Experimenral Work 
      Figure (2) shows a view of the experimental 

apparatus, while, Figure (3) shows the schematic 

diagram of two reactive distillation experimental 

set-up. The first system is (column-A-) which is a 
fractionation type distillation column made of 

Perspex Glass. The height of the column was 105 

cm (three sections: rectifying 60 cm, reactive 25 
cm, and stripping 20 cm) and 2.5cm column 



Khalid  A. Sukkar                              Al-Khwarizmi Engineering Journal, Vol. 4, No. 2, PP 1-9 (2008) 

 

 3 

diameter. On the other hand, the second column 
(column-B-) was packed column made of QVF 

glass of the same dimensions of the first column. 

The rectifying and stripping sections were filled 
with hollow cylinder glass packing (non-reactive 

packing of 10 mm height, and 4, 5 mm inner and 

outer diameter respectively) with voidage fraction 

of 0.66. The middle sections of the both columns 
were filled with 30 gm of the catalyst.  

      The  top of  each  column  was  connected  

with  a   condenser  where a coolant (T= 20°C) 
was circulated to condense vapor from the 

reactive distillation column. The condensate was 

passed into a solenoid valve. A multi-timer was 

used as a reflux ratio controller. The bottom of 
each column was connected to a reboiler 

(2000cm
3
 three neck flask). Heat supply required 

for the reboiler was regulated by a variable 
transformer via adjustable voltage.  

      The temperature along the columns axial were 

determined by manufacturing an interface system 
(Computerized Temperature Measurement 

System) which have sixteen copper-constantan 

thermocouples (T type) (eight thermocouples for 

each column). This interface is programmed and 
run by a computer (P4), which converts the 

measured voltages to the corresponding 

temperatures with the help of appropriate software 
in Excel Program. The temperature in each section 

of the column was noted after starting the 

reaction, and steady state was achieved when the 
temperatures in various sections of the column 

were stabilized. 

 

 
 

Fig. 2. General View of Experimental Apparatus. 

 

Materials and Catalysts 
    Three types of catalysts (cation exchange 

resins) were used in the present investigation, 

Zerolit 225, Zerolit 226, and Ambylite 400 
purchased from BDH. The particle sizes and the 

total surface area of the resins used are given in 

Table (1). The wet catalyst was first washed with 
methanol to remove any water that might be 

sorbed in the resin catalyst. This step aided in 

avoiding the collapse of the resin pore structure in 
the subsequent drying process. Then, dried under 

vacuum by gentle heating for 6 hours at 100°C. 

The prepared catalyst was stored in a desiccator in 

the presence of silica gel. 
      Acetic acid (99.8%) and ethanol (99.5%) were 

purchased from Scharlau Company. Table (2) 

shows the boiling points of feed and products 
compounds. 

 
Table 1  

Properties of Cation Exchange Resins Used in 

Present Investigation. 

Catalyst 
Average Particle 

Size dp (mm) 

Surface Area 

(m
2
/g) 

Zerolit 225 0.65 26.2 

Zerolit 226 0.54 21.5 

Ambylite 400 1.11 34.8 

 
Table 2 

Boiling Points of Feed and Products Compounds. 

No. Compound Boiling point, °C  

1 EtOH 78.31 

2 HAc 118.01 

3 H2O 100.0 

4 EtAc 77.20 

 

Experimental Procedure 
      The experiments were carried out in order to 

achieve an optimum column configuration for the 
production of ethyl acetate in a reactive 

distillation column. Therefore, two modes of 

reactive distillation operation were used in the 
present investigation: semi-batch and continuous 

operation mode.  

 

 
 

 

 
 

 

 
 

 

 

 
 



Khalid  A. Sukkar                              Al-Khwarizmi Engineering Journal, Vol. 4, No. 2, PP 1-9 (2008) 

 

 4 

 

 
Fig. 3. Experimental Units: A- Fractionation RD,  and B- Packed RD System. 

 

Semi-Batch Operation Mode 
      The semi-batch mode was used to evaluate the 

catalyst type and to evaluate the performance and 
design of reactive distillation unit configuration 

(Fractionation column-A- and Packed column -B). 

Therefore, a batch of 1000 cm
3
 of EtOH was used 

in the settle (reboiler), while the acetic acid was  
fed  at  the top of the reactive section by using 

dosing pump with flow rate of 5 cm
3
/min. The 

operation conducted under total reflux condition 
and atmospheric pressure.  

 

Continuous Operation Mode 
      The continuous operation mode was used to 

investigate the flowing parameters: 

1- the performance  of catalyst type, 2- reflux 
ratio, and 3- temperature distribution along RD 

column. On the other hand, in continuous 

operation, two dosing pumps were used to feed 

the reactants to RD. The acetic acid was fed at the 
top of the reactive section, while the EtOH fed at 

the lower part of the reactive section. Therefore, 

for each test (17.12) mole of HAc was fed to 
(17.12) mole of EtOH (i.e the mole ratio of 

HAc/EtOH =1). The reactants were introduced 

into the reactive distillation column at room 
temperature and atmospheric pressure. The 

reaction was carried out until reaching steady 

state. Top and bottom products were sampled and 
their concentrations were measured every 1 hr. 

The products were analyzed in a gas 

chromatograph (Shimadzu GC-2014) by TCD 
with a capillary column (S.G.E., length = 25 mm, 

I.D.= 0.22 mm,   film= 0.2μm). 

 

Results and Discussion 

Semi-Batch Operation Mode  
      The design and operation of reactive 
distillation systems are considerably more 

complex than those involved in either 

conventional reactors or conventional distillation 
columns. The introduction of separation process 

within the reaction zone leads to complex 

interactions between vapour-liquid equilibrium, 
vapour-liquid mass transfer, intra-catalyst 

diffusion and chemical kinetics.  

      From the acetic acid recovery point of view, 

the optimal configuration should give the highest 
conversion of acetic acid with a minimum 

concentration of acetic acid at the top, as well as a 

minimum concentration of ethyl acetate at the 
bottom. Therefore, in order to evaluate the type of 

catalysts used in present investigation, the effect 

of the catalyst on the extent of conversion is 
presented in Figures (4) and (5) for column-A- 



Khalid  A. Sukkar                              Al-Khwarizmi Engineering Journal, Vol. 4, No. 2, PP 1-9 (2008) 

 

 5 

and column-B- respectively under semi-batch 
operation mode.  

 

 
 

Fig. 4. Influence of Catalyst Type on Esterification 

of HAc with EtOH to EtAc in Fractionation RD  

Under Semi-Batch  Operation Mode. 

 

      The comparison between the catalyst 
performance of Figures (5) and (6) shows that, the 

packed column RD (column-B-) gives higher 

rates of conversion of HAc to EtAc with reaction 

time than that of fractionation RD (column-A-). 
This indicates that, the column-B provides an 

excellent heat and mass transfer between the 

liquid and vapour phases which arise from its 
structure of ordered flow channels. Furthermore, 

the packings helps to promote mixing and 

distribution of ascending vapour and descending 

liquid phases in RD due to high total surface area 
of packing. On the other hand,  the packing 

column leads to a better separation of products 

from reactants for such equilibrium limited 
reactions. These results are in agreement with the 

work of Saha et al. [2] and Tang et al. [6]. 

      Therefore, the second part of the present 
investigation will continue by using just packed 

column (column-B-) only with continuous 

operation mode, because the high surface area that 

was provided in such column. 
 

Temperature Distribution in RD 
       Esterification process is regarded one of 

highly exothermic reactions, therefore, benefits of 

heat integration are obtained because the heat 

generated in the chemical reactions is used for 
vaporization. On the other hand, the reactants and 

products must have suitable volatility to maintain 

high concentrations of reactants and low 
concentrations of products in the reaction zone. 

Therefore, in esterification process the 

temperature distribution and liquid-vapour 
interaction must be known. 

 
 

Fig. 5. Influence of Catalyst Type on Esterification 

of HAc with EtOH to EtAc in Packed RD Under 

Semi-Batch Operation Mode. 

 

      Figure (6) shows the comparison between the 

temperature distribution of the three types of 
catalysts used for esterification reaction under 

constant conditions of: (catalyst weight = 30g, R= 

2, and HAc/EtOH=1). The temperature in the 
bottom was about 84°C. It rapidly changes around 

the interface of reaction and separation zones. The 

temperature in rectifying zone is about 77.5°C, 

which is the azeotropic temperature. From the 
same figure, it is clear that, the temperature 

distribution along column axial for all three types 

of catalysts show an increase in the region of 
reaction zone because the generated heat from 

exothermic reaction. On the other hand, the 

temperature distribution up to condenser is 
essentially the same due to steady state operation. 

According to Table (2), the boiling points of HAc 

and H2O are higher enough, therefore, such 

compounds exist in the stripping zone and 
reboiler.  

      In order to study the effect of reflux ratio on 

the temperature distribution along the RD column, 
Figures (7),  (8),  and  (9)  show  the  effect  of  

the  four levels of reflux ratio R (1, 2, 3, and 5) on 

the temperature distribution under constant 

operation conditions. For all three types of 
catalysts, these figures show that, there an inverse 

relationship between R and temperature 

distribution for all types of catalysts. Therefore, as 
the reflux ratio increases the temperature 

distribution level along the column axial 

decreases. The explanation of such behavior is 
based on phenomenon of interaction between 

liquid-vapour equilibrium in reactive distillation. 

 



Khalid  A. Sukkar                              Al-Khwarizmi Engineering Journal, Vol. 4, No. 2, PP 1-9 (2008) 

 

 6 

 
 

Fig. 6. Comparison of Temperature Distribution 

Levels  Between Catalyst Types Along RD Column. 

 

 

 
 

Fig. 7. Temperature Distribution Along RD Column 

Using Amb. 400 Catalyst at Different Reflux Ratios. 

 

 

 
 

Fig. 8. Temperature Distribution Along RD Column 

Using Zerolit 225 Catalyst at Different  

Reflux Ratios. 

 

 
 

Fig. 9. Temperature Distribution Along RD Column 

Using Zerolit 226 Catalyst at Different Reflux Ratios. 

 

Effect of Reflux Ratio 

      The effect of the reflux ratio of the organic 
phase (of the top product) was investigated to 

determine the conversion of acetic acid from its 

aqueous solution. The ranges of reflux ratio 
values reported by various investigations [1,2, 10] 

vary between 1 and 6. The present experiments 

were conducted at values of reflux ratio 0.5, 1, 2, 

3, and 5. In all experimental runs, the feed mole 
ratio of HAc to EtOH was kept at the optimum 

ratio of 1:1. All other operating conditions were 

kept constant. There was an increase in acetic acid 
conversion from 32% to about 53-65% when the 

reflux ratio of the organic phase was raised from 

0.5 to 5 for all types of catalysts as shown in 

Figure (10).  In other words, as the reflux ratio 
increased from 0.5 to 3 the weight percentage of 

ethyl acetate production of distillate increased 

clearly due to high conversion rates of HAc to 
EtOH. 

      On the other hand, Figure (10) shows that the 

Ambylite 400 catalyst gives the highest 
conversion rates of HAc than other two types of 

catalysts for all reflux ratios studied. This is due 

to the high surface area of Ambylite 400 catalyst 

34.8 m
2
 that is available for chemical reaction 

than that of 26.2 and 21.5 m
2
 for Zerolit 225 and  

Zerolit 226 respectively. 

 



Khalid  A. Sukkar                              Al-Khwarizmi Engineering Journal, Vol. 4, No. 2, PP 1-9 (2008) 

 

 7 

  
Fig. 10. Effect of Reflux Ratio on % Conversion of 

HAc to EtOH. 

 

Conclusions  

      Combining catalytic reaction and separation in 
the same reactor can improve the conversion and 

selectivity for much equilibrium limited reactions 

reduce capital cost and also enhance catalyst 

lifetime. 
      In semi-batch operation mode, results pointed 

out that, the column-B- (packed) shows higher 

conversion rates than that of column-A- 
(fractionation). This is attributed to the high 

surface area available for liquid vapour contact in 

packed type column, which leads to increase in 

the rates of mass transfer. On the other hand, 
Ambylite 400 catalyst shows higher activity for 

esterification reaction than other two types 

(Zerolit 225 and  Zerolit 226).  
      Esterification process is regarded one of 

highly exothermic reactions, therefore, the 

temperature distribution along column axial for all 
three types of catalysts is essentially the same due 

to steady state operation in continuous operation 

mode. On the other hand, the effect of reflux ratio 

on temperature distribution is clearly noted, that 
as the reflux ratio increases the temperature 

distribution along the column is reduced for all 

types of catalysts. 
      The experimental results point out that, as a 

reflux ratio increases the conversion rates of 

acetic acid increases. This is due to high mass 
transfer rates between  vapour and liquid. 

Therefore, increasing reflux rates enhances 

separation and recycles unreacted reactants to the 

reaction zone and, thereby, increases conversion. 
 

 

 

Nomenclature 
Column-A    A Fractionation type reactive  

                      distillation column with rods trays.  

Column-B    Packed reactive distillation  
                      column. 

Conv.%        Percentage conversion 

dp                  Particle diameter of the catalyst  
                      [mm] 

EtAc             Ethyl acetate 

EtOH            Ethyl alcohol (Ethanol) 
HAc              Acetic acid  

H2O              Water 

R                   Reflux ratio 

RD                Reactive distillation   

 

Acknowledgment 

      The authors gratefully acknowledge the 
financial support provided for this work by 

Ministry of Higher Education and Scientific 

Research/ Scientists and Creators Dept.-Baghdad-

Iraq. 

 

References  

[1] Kloker, M., Keing, E. Y., Gorak, A., 
Markusse, A. P., Kwant, G. and Moritz, P., 
“Investigation of different column 
configurations for the ethyl acetate synthesis 
via reactive distillation”, Chemical 
Engineering and Processing, 43, 791-801 
(2004). 

[2] Saha, B., Chopade, S. P. and Mahajani, S. M., 
“Recovery of dilute acetic acid through 
esterification in a reactive distillation 
column”, Catalysis Today, 60, 147-157 
(2000). 

[3] Xu, Z. P. and Chuang, K. T., “Kinetics of 
acetic acid esterification over ion exchange 
catalysts”, The Canadian Journal of Chemical 
Engineering, 74, 493-500 (1996). 

[4] Aiouache, F. and Goto, S., “Reactive 
distillation-pervaporation hybrid column for 
tert-amyl alcohol etherification with ethanol”, 
Chemical Engineering Science, 58, 2465- 
2477 (2003). 

[5] Bianchi, C. L., Ragaini, V., Pirola, C. and 
Carvoli, G., “A new method to clean 
industrial water from acetic acid via 
esterification”, Applied Catalysis B: 
Environmental, 40, 93-99 (2003). 

[6] Tang, Y. T., Huang, H.P., and Chien, I. L., 
"Design of a Complete Ethyl Acetate Reactive 
Distillation System", J. Chem. Eng. Japan, 36, 
1352-1363 (2003). 

[7] Tang, Y. T., Huang, H.P., and Chien, I. L., 
"Plant-Wide Control of a Complete Ethyl 
Acetate Reactive Distillation Process",  J. 



Khalid  A. Sukkar                              Al-Khwarizmi Engineering Journal, Vol. 4, No. 2, PP 1-9 (2008) 

 

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Chem.  Eng.  Japan, 38, No.2,  130-146 
(2005). 

[8] Chang, Y. A., and Seider, J. D., “Simulation 
of continuous reactive distillation by a 
homotopy-continuation method,” Chem. Eng. 
Sci., 12, 1243-1255, (1988). 

[9] Bock, H., Jimoh, M. and Wozny, G., 
“Analysis of reactive distillation using the 
esterification of acetic acid as an example,” 
Chem. Eng. Technol., 20, 182-191, (1997). 

[10] Gangadwala J., Mankar, S., Mahajani, S., 
Kienle, A. and Stein, E., “Esterification of 
acetic acid with butanol in the presence of 

ion-exchange resins as catalysts”, Ind. Eng. 
Chem. Res., 42, 2146-2155 (2003). 

[11] Gangadwala, J., Kienle, A., Stein, E. and 
Mahajani, S., “Production of butyl acetate 
by catalytic distillation: process design 
studies”, Industrial and Engineering 
Chemistry Research, 43, 136-143 (2004). 

[12] Teo, H. T. R. and Saha, B., 
“Heterogeneously catalysed esterification of 
acetic acid with iso-amyl alcohol: kinetic 
studies”, Journal of Catalysis, 228, 174-182 
(2004).   

 
 

 

 
 

 

 
 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 



Khalid  A. Sukkar                              Al-Khwarizmi Engineering Journal, Vol. 4, No. 2, PP 1-9 (2008) 

 

 9 

  

 دراســــة سهوكيــــة واوتقال انكتهة وانحرارة في أعمذة انتقطـــير رات انمفاعـــم
 

جمال ماوع عهي. د, خانذ عجمي سكر.د*, ماجذ سهيم رضاعه. د  

ويران ماووئيم , زيذون محسه شكور.د  
 انؼـشاق– بـغــذاد / انضايؼــت انخكُٕنٕصٛـت / لغـــى انُٓذعـت انكٛـًٛأٚــت*

 
انخالصة 

 Reactive Distillation باعخخذاو حمُٛت انًفاػم رٔ انخمطٛش Ethyl Acetate حى دساعت ػًهٛت ححضٛش خالث االرٛم  فٙ ْزا انبحذ       

 حٛذ حى اعخخذاو رالرت إَٔاع يـٍ انؼـٕايم انًغاػذة . باعخخذاو االٚزإَل ٔحايط أنخهٛك كًٕاد أٔنٛت نهخفاػم ٔاعخخذاو انؼٕايم انًغاػذة انصهبت

Cation Exchanging Resinsْٙ ٙٔانخ  : Zerolit 225, Zerolit 226 , and Ambylite 400 . ٍٛخالل انبحذ حى بُاء يُظٕيخٍٛ سٚادٚخ

 بأسحفاػاث Rectifying, Reactive and Stripping sectionكم يُظٕيت حخكٌٕ يٍ رالد يُاطك ْٙ . بأبؼاد يٕحذة إلصشاء انخضاسب

 فٙ حصًًٛٓا  كَٕٓا ححخٕ٘ ػهٗ صٕاَٙ َٕع (-Column-A)اػخًذث انًُظٕيت األٔنٗ .  عى لطش نهؼًٕد2,5عى ػهٗ انخٕانٙ ٔ (60+25+20)

(Trays (Fractionation , أيا انًُظٕيت انزاَٛت (Column-B-) ٕفصًًج ػهٗ أَٓا ػًٕد حمطٛش يحش((Packed Distillation Column 

.  يهى5 يهى ٔلطش خاسصٙ 4يهى ٔلطش داخهٙ 10ححخٕ٘ ػهٗ حشٕاث صصاصٛت اعطٕاَٛت انشكم بطٕل 

 ٔانًُظ  Semi-batchانًُظ األٔل ْٕ ػًم َصف انٕصــــبت:       أصشٚج انخضاسب باعخخذاو ًَطٍٛ يٍ انخشغٛم ػهٗ أعاط يشٔس انًٕاد األٔنٛت

حٛذ اعخخذو انًُظ األٔل نغشض حمٛٛى كفاءة انؼٕايم انًغاػذة انًغخخذيت ٔححهٛم ٔحمٛٛى أداء .  Continuousانزاَٙ ْٕ األعهٕب انًغخًش

حٛذ أظٓشث انُخائش أٌ انًُظٕيت انزاَٛت .  األحٙ اعخخذيٍ فٙ انبحذ(Fractionation and packed column) انخصًًٍٛٛ نهًُظٕيخٍٛ

Column-B- ٗأػطج يؼذالث كفاءة ٔححٕل ػانٛت َحٕ انُٕاحش انًشغٕب بٓا أكزش يٍ انًُظٕيت األٔن Column-A- . ْٔزا فٙ حمٛمت األيش ٚؼٕد

ٔانز٘ ٚؤد٘ , إنٗ انًغاحت انغطحٛت انؼانٛت نهحشٕاث ٔانخٙ حٕفش يغاحت حاليظ صٛذة بٍٛ انبخاس انصاػذ ٔانغائم انز٘ ُٚضل يٍ أػهٗ انبشس

 أػطٗ فؼانٛت أػهٗ  فٙ حفاػم Ambylite 400يٍ َاحٛت أخشٖ أظٓشث انُخائش أٌ انؼايم انًغاػذ َٕع  . بطبٛؼت إنٗ صٚادة يؼذالث اَخمال انكخهت

.  االعخشة يٍ انُٕػٍٛ اٜخشٍٚ

حٛذ حؼذ حفاػالث االعخشة يٍ . فمظ ٔباألعهٕب انخشغٛهٙ انًغخًش-Column-B       يٍ َاحٛت أخشٖ حى اػخًاد انؼًم باعخخذاو انًُظٕيت 

ٔنٓزا يخابؼت حٕصٚغ دسصاث انحشاسة ػهٗ طـــٕل انبشس ٔنألَٕاع انزالرت يٍ انؼٕايم انًغاػذة أظٓشث انُخائش باٌ , انخفاػالث انباػزت نهحشاسة

ٔيٍ خالل . ْٔزا ٚؼضٖ إنٗ حانت االعخمشاس انخشغٛهٙ فٙ أعهٕب انخشغٛم انًغخًش, انخٕصٚغ انحشاس٘ حمشٚباً يخغأ٘ نضًٛغ انؼٕايم انًغاػذة

أظٓشث انُخائش اَّ كهًا صادث يؼذالث انشاصغ كهًا اَخفضج ,  ػهٗ حٕصٚغ دسصاث انحشاسة فٙ انبشسReflux Ratioدساعت حأرٛش َغبت انشاصغ 

.   يؼذالث حٕصٚغ انحشاسة داخم انبشس ٔنضًٛغ األَٕاع يٍ انؼٕايم انًغاػذة

حٛذ ًٚكٍ حفغٛش يزم ْزِ انضٚادة ػهٗ , أشاسث انُخائش انؼًهٛت إنٗ ال اَّ بضٚادة لٛى انشاصغ فاٌ يؼذالث ححٕل حًط أنخهٛك عٕف حضداد       

 .  أعاط انخحغٍ انحاصم بًؼذالث اَخمال انكخهت بٍٛ انبخاس انصاػذ ٔانغائم انُاصل فٙ بشس انخمطٛش رٔ انًفاػم