CHAPTER 3 MODELLING AND ANALYSIS OF THE PACKED COLUMN
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1 37 CHAPTER 3 MODELLING AND ANALYSIS OF THE PACKED COLUMN Absorption in a chemical process refers to a mass transfer between gas and liquid which transfers one or more components from the gas phase to the liquid phase. Absorption occurs in two reaction processes, namely physical and chemical absorption. Physical absorption takes place when there is no chemical reaction between the solute and the solvent. Absorption with chemical reaction involves removing the impurities from gas phase and dissolving them into a liquid phase by making a chemical reaction between them. In this work, aqueous solutions are used as absorbent with which the absorption takes place by means of chemical reaction in the liquid phase. The absorption process is described by the mathematical model based on a two-film theory of gas-liquid absorption. The two film theory proposed by Whitman (1923) is the simplest theory designed for mass transfer analysis. The schematic visualization of two film theory is shown in Figure 3.1. The two film theory is expressed by considering the following assumptions: 1. The rate of mass transfer depends on the rate of migration of a molecule in each gas or liquid phase. 2. The two-film model involves an assumption that the gas and liquid phases are in unstable contact with each other and separated by an interface area where they meet.
2 38 3. The model proposes that a mass-transfer zone (film) takes place in the gas and liquid phases on either side of the interface. 4. Complete mixing takes place in gas and liquid phases and the interface is at equilibrium with respect to pollutant molecules transferring in or out of the interface. From the above assumptions, the two film theory is derived as, N A = k g (P AG AI ) (3.1) N A = k l (C AI AL ) (3.2) where N A -rate of transfer of component A, k g -mass-transfer coefficient for gas film, k l -mass-transfer coefficient for liquid film, P AG -partial pressure of solute A in the gas, P AI -partial pressure of solute A at the interface, C AI -concentration of solute A at the interface, and C AL -concentration of solute A in the liquid. Figure 3.1 implies that all resistance to movement occurs when the molecule is diffusing through the bulk gas phase and bulk liquid films which make interfacial area between liquid and gas phase. Hence, p AG is changed into p AI. In the same way, the concentration in the liquid changes from C AI to C AL when the mass transfer occurs. From the above equations, it is clear that the value for a mass transfer coefficient increases, and then the amount of pollutant transferred from the gas to the liquid increases.
3 39 Figure 3.1 Two-film theory 3.1 MATHEMATICAL MODELLING The efficiency of an absorption process depends on the solubility of the gaseous contaminant in a liquid phase. For most gases, the absorber provides a high degree of turbulent contact and a long residence time to achieve high absorption efficiency. The two most common high-efficiency absorbers are plate and packed column. Both of these devices are used extensively to control gaseous pollutants. The most commonly used device for absorption process is a packed column, since packed area in the column is used to develop more interfacial area between gas and liquid which increases the absorption rate (Coulson & Richardson 1991). The schematic arrangement of the packed column is shown in Figure 3.2. It consists of a cylindrical column, liquid sprayer, gas and liquid
4 40 inlet, gas distributor and a packed bed. The liquid solvent is allowed to enter the column at the top through a liquid distributor and then it flows down through the surfaces of the packing materials. The gas phase enters at the bottom of the column, which flows upward through the packing materials, through which mass transfer takes place from the gas to liquid films. The surfaces of the packing are much helpful for the mass transfer by increasing the mass transfer area. The performance of the column depends on the maintenance of good liquid and gas distribution throughout the surface area by properly designing the parameters of the column such as Liquid / Gas (L m /G m ) ratio, diameter, packing height and total height. In addition, the type of packing material and absorbent used influence the performance of the packed column. Gas outlet Liquid inlet Liquid Sprayer Packed Bed Gas inlet Gas Distributor Liquid outlet Figure 3.2 Schematic of packed column
5 Determination of L m /G m Ratio The first task of designing a packed column is to determine the minimum flow rate of liquid and gas entering into the column. In the present research work, hydrogen peroxide (H 2 O 2 ) is considered as an absorbent for SO 2 emission control process. During the mass transfer between SO 2 and H 2 O 2, H 2 O 2 becomes aqueous sulphuric acid solution while recirculating in the packed column. Hence, aqueous sulphuric acid is taken as the liquid for physical modelling. The minimum liquid and gas requirement are determined based on solubility of gas (SO 2 ) in a liquid (aqueous sulphuric acid) which determines the amount of pollutant absorbed from the gas phase to liquid phase. It is a function of both temperature and pressure. In this experimental study, the temperature is maintained as constant, hence the solubility is effected by the pressure. At equilibrium conditions, the solubility is expressed as the amount of solute absorbed into liquid phase being equal to the amount coming out of the resultant solution. Hence no mass transfer takes place between the gas and the liquid phase and the concentration of both the gas and the liquid phases are same. It means that the concentration of the pollutant at the outlet stream is almost zero. The mostly used method for analysing the solubility data is to use an equilibrium diagram (Coulson & Richardson 1991). It is a plot between mole The mole fraction of SO 2 in gas phase is computed by dividing the partial pressure of SO 2 (P SO2 ) by the total pressure (P TOT =101kPa) of the packed column and it is expressed as
6 42 P SO2 Y= P (3.3) TOT Also, the mole fraction of SO 2 in liquid is determined by dividing the moles of SO 2 dissolved into the liquid by the total moles of aqueous sulphuric acid and it is expressed as Moles of SO in H SO X (3.4) = Moles of SO 2 in H 2 SO 4 +Moles of H 2 SO 4 The principle for solubility of a gas in a liquid is formulated by William Henry in 1803, called as Henry's law and it used to determine the relation between solubility of gas and liquid and it is expressed as Y mx (3.5) where m is the Henry's constant. It is determined from the slope of the equilibrium line ( Y/ X) between X and Y. The values of X and Y need to be determined by an experimental approach. Based on the literature study reported by Hayduk et al (1988), the experimental results of absorption of SO 2 into aqueous sulphuric acid are taken to calculate X and Y which are given in Table 3.1. The table shows the values of solubility of SO 2 in 100 gm of aqueous H 2 SO 4 solution for different SO 2 partial pressures. Based on the equations 3.3, 3.4 and 3.5, the values of X, Y and m are calculated and provided in the Table 3.1.
7 43 Table 3.1 Solubility data for SO 2 absorption in aqueous sulphuric acid Partial pressure of SO 2 (P SO2 kpa) Solubility of SO 2 /100 gm of aqueous H 2 SO 4 solution Mole fraction of SO 2 in the liquid phase (X) Mole fraction of SO 2 in the gas phase (Y) m=(y/x) constant From the tabulated values, an equilibrium diagram is plotted between X and Y as shown in Figure 3.3. From the Figure 3.3, it is clear that the equilibrium line is linear; hence the slope value ( is used to predict the solubility of SO 2 into aqueous sulphuric acid solutions (Manyele the mass-transfer rate by controlling the liquid phase (Coulson & Richardson 1991). Hence, m = 1.21 is chosen for further analysis Mole fraction of SO2 in aquous H2SO4 (X) Figure 3.3 Equilibrium diagram for SO 2 -H 2 SO 4 solubility
8 44 Another factor to be considered while determining the liquid flow rate into the column is flooding. It is the gas velocity at which the liquid droplets become entrained in the exiting gas stream and it is expressed as K 4 ml G m m (3.6) where, K 4 -Flooding factor (0.6 to 0.8); G m -Gas mass flow rate (kg/sec); L m -Liquid mass flow rate (kg/sec) and m - nt. For a constant flow rate of gas, the increase in liquid flow rate causes the liquid to fill completely in the packing and stops the liquid flow into the packed area. From the Equation (3.6), by considering G m = 40 m 3 /hr (or) kg/sec (assumed value to determine required liquid flow rate), 4 = 0.7, then the minimum liquid flow rate is obtained as L m = G m *K 4 / m = kg/sec = lph (3.7) Hence, the liquid flow rate to the packed column (L m ) is chosen as 150 lph approximately for experimental analysis Determination of Column Diameter Column diameter has the direct influence on the liquid and gas velocity inside the packed column. When the diameter of the column decreases, the gas flow rate inside the column increases gradually which produces flooding. It is overcome by increasing the diameter of the packed column. However, as the diameter increases, the cost of the packed column also increases. Hence, the column diameter should be optimized and it is calculated for 70% of the flooding velocity to achieve the highest economical pressure drop and good liquid and gas distribution (Coulson & Richardson 1991).
9 45 The flooding velocity is calculated by Sherwood correlation which is shown in Figure 3.4. From the Figure 3.4, the flooding factor (K 4 ) is identified for the corresponding pressure drop (F LV ) in the packed column and it is used to calculate the column diameter. The pressure drop (F LV ) is represented as F LV L G m m G L (3.8) G gas (SO 2 ) density (1.21 kg/m 3 ), L -liquid (aqueous H 2 SO 4 ) density (1850 kg/m 3 ), G m -molar flow rate of gas ( kg/sec) and L m -molar flow rate of liquid ( kg/sec). Thus, the calculated pressure drop (F LV ) is Figure 3.4 Flooding and pressure drop correlation For the absorber design, the recommended design value of liquid pressure drop (mm per m packed area) is between15 to 50. Hence for the present design, the pressure drop line is selected as 21 (mm per m packed
10 46 area). From the Figure 3.4, the flood factor (K 4 ) is identified as 0.7 for of F Lv and 21 mm per m of packed area of pressure drop line. From the flooding factor, the gas mass flow rate / column cross sectional area ( V ) is determined and it is expressed as * w V K ( ) 13.1 F ( / ) * 4 w G L G 0.1 P L L 0.5 (3.9) where FP G gas density =1.21 kg/m 3 L liquid density = 1850 kg/m 3 L liquid viscosity = Ns/m 2 packing factor for 25mm polypropylene pall ring =170 (Coulson 2005). Based on the above parameters, the calculated gas mass flow rate / column cross sectional area ( V ) is kg/m 2 s. * w The area of the packed column (A) is calculated as G A (3.10) V m * w where, G m = molar flow rate of gas ( kg/sec). From A, the required diameter of the column is computed as 150 mm for experimental analysis Determination of Packed Height and Total Height The packed height directly refers to the depth of packing material needed to accomplish the required removal efficiency. The total height and packing height of the column are interrelated and both the parameters are used
11 47 to determine the total liquid hold up time inside the packed column. The higher the liquid hold up time, better the removal efficiency. Computation of packed height (Z) of the column is expressed as Z=H OG N OG (3.11) where N OG represents the number of transfer units and H OG represents height of transfer units. The concept of transfer unit has the following assumptions. 1. Absorption process takes place in a series of stages. 2. The liquid and gas stream leaving out of the stages are at equilibrium. These stages are visualised using the height of transfer unit (H OG ). Though packed column is a continuous contact equipment, it is considered as discrete equipment in order to calculate mass balance in the packed column. The number of transfer unit for gas phase is calculated graphically by Colburn diagram and it is represented as, N OG Y mx mgm mg Y mx L L 1 2 ln mg L m m m m m (3.12) where N OG -number of transfer unit; Y 1 -mole fraction of SO 2 in entering the column (5000 ppm); Y 2 -mole fraction of SO 2 leaving the column (assumed as 50 ppm); m -slope of the equilibrium line (1.21); X 2 -mole fraction of liquid entering the column, G m -molar flow rate of gas ( kg/sec), and L m -molar flow rate of liquid ( kg/sec). The packed column height at different flow rate was estimated by Coulburn in 1939 (Coulson & Richardson 1991). The procedure gives fast
12 48 estimation of packed height at different flow rates. It provides the relationship between number of transfer unit N OG and (Y 1 /Y 2 ) for various absorption factor (mg m /L m ) as shown in Figure 3.5. From the figure 3.5, the identified N OG is 3.6 for Y 1 /Y 2 =7.1 and mg m /L m = 0.7. The height of transfer unit (H OG ) for gas phase is determined based on experimental analysis or based on the results revealed by different authors. For many industrial applications, H OG is taken between 0.3 m to 1.2 m (Perry 1997). A typical value of H OG for 25 mm packing material is 0.3 to 0.6 m. For the present work, polypropylene pall ring with 25 mm diameter is considered. Hence, H OG is taken as 0.3. Figure 3.5 Colburn diagram From the Equation (3.11), packed height is calculated as 1080 mm and it is approximated into 1000 mm for experimental analysis. Based on the packed height, to study the effect of increasing packed area, the total height of
13 49 packed column is taken as 2500 mm including 500 mm for connecting gas distributor and 500 mm for connecting spray tower. From the physical modelling, the selected packed column parameters are listed below for CFD modelling: Diameter of the column : 150 mm Total height of the column : 2500 mm Packed Height : 1000 mm Minimum Inlet liquid flow rate : 150 lph Minimum Inlet gas flow rate : 40 m 3 /hr 3.2 CFD MODEL DEVELOPMENT AND ANALYSIS Computational Fluid Dynamics (CFD) is used as a tool to analyse the mass transfer and transport behaviour between the two phases such as gas phase and liquid phase in a packed column. Absorption of SO 2 in a packed column is a complex process that contains both mass transfer and a chemical reaction (Gomez et al 2007). For a better understanding of such complex mass transfer, modelling and analysis part of the packed column is needed. This simulation study comprises Computational Fluid Dynamics (CFD) modelling and simulation of a packed column. The CFD model is developed based on the parameters computed from the mathematical modelling. The simulation runs are carried out with the absorbents such as water and H 2 O 2 to analyse the SO 2 removal efficiency. The following steps are involved in the design and analysis of packed column using CFD.
14 50 Definition of the geometry (physical bounds) of the packed column Meshing (Discretization of volume occupied by the fluid into cells called as mesh) Definition of physical modelling (such as the equations of mass, momentum and species conservation) Definition of boundary conditions (specifying the fluid behaviour and properties at the boundaries of the packed column) Simulation through solving the equations iteratively and CFD simulation results of the packed column Definition of Geometry The first step involved in the CFD analysis is the definition of the geometry (physical bounds) of the packed column. Based on the parameters such as total height, packed height, diameter, gas flow rate and liquid flow rate (determined based on the mathematical modelling detailed in section 3.1.1), modelling of the packed column is developed using GAMBIT The solid model and wire frame model of the packed column shown in Figure 3.6 are designed with 150 mm inner diameter, 160 mm outer diameter, 2500 mm total height and 1000 mm packed height.
15 51 Figure 3.6 Modelling of a packed column Meshing Meshing is the process of splitting the entire fluid flow domain into discrete cells. Each element is called as a node or cell. The mesh classification is based upon the connectivity of the mesh and it is classified as structured, unstructured and hybrid mesh. A structured mesh is characterized by regular connectivity and an unstructured mesh is characterized by irregular connectivity. Compared to structured mesh, the storage requirements for an unstructured mesh are substantially larger since the neighbourhood connectivity is explicitly stored. A hybrid mesh contains structured portions and unstructured portions. For meshing the packed column, hybrid mesh is used since it consists of structured portions such as the wall of the column, packed tower, gas distributor and unstructured portions such as packed material with a random arrangement. The entire column is considered as solid volume and meshed with tetrahedral element. The fluid path is considered as the face and meshed with
16 52 triangular element. Meshing of the packed area is complicated due to its random arrangement, more number of packing elements and smaller size of 1000 mm packed height, HYPERMESH software is used for meshing and defining the fluid path accurately. Figure 3.7 and 3.8 illustrate the random arrangement of packing material developed using HYPERMESH. Figure 3.9 shows the meshed liquid sprayer of 150 mm diameter with spray nozzles of 5 mm. Figure 3.10 exemplifies gas distributor with three stage gas distributions of 150mm, 140 mm and 130 mm diameters to promote the gas transfer through the packed area rapidly. The gas distributors are designed in such a way that the liquid droplets would not enter the gas distribution chamber. Figure 3.7 Solid arrangement of packing material Figure 3.8 Wire frame model of packing material
17 53 Figure 3.9 Hypermeshed liquid sprayer Figure 3.10 Hypermeshed gas distributor Definition of Physical Modelling The next step involved in the CFD modelling is the definition governing equations such as definition of mass, momentum and species conservation. equations: The following assumptions are made before defining the governing
18 54 1. A synthetic SO 2 gas is used in the place of flue gas and the flow is assumed to be incompressible. 2. Temperature is considered as constant throughout the column. Based on the assumptions given by Ebrahimi et al (2003) and Bravo et al (2002), flue gas is cooled by water before entering the column. The liquid considered for the analysis is H 2 O 2, which is subjected to change in temperature when it reacts with SO 2. The temperature of the inlet liquid loop is maintained at constant rate by placing the heat exchanger on the liquid loop (Marraco et al 2009). Therefore, the temperature of liquid and gas is assumed to be equal during the absorption analysis. 3. The reaction taking place between gas and liquid is more in packed area as compared to the other area of the column. Hence, packed area is considered for reaction analysis while the reaction over the wall of packed column is not considered for analysis. Momentum equations The main task of fluid dynamics inside the packed column is to find the velocity of the field describing the flow. The basic equations representing the fluid flow are represented by conservation of mass, energy and momentum since these natural quantities are conserved under their application conditions. The flow in the packed column is multi phase. Flue gas is a continuous phase exchanging properties with disperse liquid phase. Eulerian- Eulerian model is used to simulate each domain. This model is formulated by a set of differential equations whose solutions are the functions for which the
19 55 given function is stationary. Each point in a domain exists with a certain volume fraction and each has distinct properties defined by a set of equations such as mass, momentum and species transportation equations (Marocco 2010). by its volume fraction is represented by r. r v. r t m (3.13) phase, v = ( v, v, v is the volume fraction of the phase- diffusion coefficient and m is the mass- -transfer rates between two phases are neglected in this mass- conservation equation, since the transfer of chemical species in SO 2 absorption process does not have a major impact on the overall mass balance, but those are included in the equations for the mass fraction of the transferred species. The momentum equation for the i th component of the phase velocity vector v is given as d dt y r v i. r v i v. v i r r v r S i x i (3.14) where S is the different source terms, such as drag or body forces. The momentum equation for the gas phase is given by,
20 56 P v Y r r g. r v. gv r. r v g g g gi A gi g g g gi g g g i xi where g i the i th component of the gravity vector. The momentum equation for the liquid phase is similar to the equation of momentum of gas phase and it is given as P. lrl v v. lv l li rl rl vli r r g x li l l l l i i The species conservation equation for species A is given as t r Y. r Y v. Y r. Y r Y S A A A A A A (3.15) where Y A is the diffusion coefficient, Y is the mass fraction A the source term for chemical reaction in the column. S A is Continuity equations A continuity equation describes the transport of mass and momentum quantities that are conserved during the reaction conditions. The continuity equation for gas and liquid phase in steady state is given by. r v Y. r 0 (3.16) A -face void fraction.
21 57 Mass transfer equation between gas and liquid The present study considers only the mass transfer taking place between SO 2 in the flue gas and the H 2 O 2 in the liquid phase. The mass flow rate of SO 2 is very low as compared to the total mass flow into the packed column and hence it does not have the impact on continuity equation on gas phase. Mass transfer of SO 2 involves both gas side and liquid side mass transfer resistances. For low dissolved gas concent applied and the equation for molar rate of SO 2 mass transfer is written as S =S +S =C +C (3.17) k,mass k,h2o 2 k,so 2 H2O2 SO2 where S k is the droplet mass source (kg/s) for SO 2 and H 2 O 2, m SO2 is the concentration of SO 2 in liquid (mol/m 3 ), m H2O2 is the concentration of H 2 O 2 in liquid bulk (mol/m 3 ). Absorption chemistry involves mass transfer resistance between liquid and gas phases. Since the concentration of SO 2 in the gas phase is very minimum (5% by volume), He transfer based on two-flim theory as presented in the Equation (3.1) and it is rewritten as N K ( P mc ) (3.18) SO2 SO2 SO2 SO2 where N SO2 -Rate of mass transfer of SO 2, K SO2 -SO 2 gas mass transfer coefficient, P SO2 -Partial pressure of SO 2 in gas, H SO2 - SO 2, C SO2 -concentration of SO 2 in the liquid.
22 58 After evaluation of these source terms, the conservation equations are solved again and again. The resulting flow and concentration fields are used to calculate the updated source terms until convergence Definition of Boundary Conditions Boundary definition is important to specify the fluid behaviour and property of the packed column. Both inlet and outlet gas flow rates are defined as mass inlet flow; column is defined as wall and the packaging material is defined as solid volume and fluid faces. The solver model used is the species transportation which allows the model to mix and transport chemical species by solving conservation equations describing convection, diffusion and reaction sources for each component species CFD Simulation Results The mathematical model described in section 3.1 is applied to the CFD simulation of the packed column. From the developed CFD model, simulation results are obtained for water as an absorbent and H 2 O 2 as an absorbent. For the simulation studies, the parameters defined for the packed column are shown in Table 3.2. Table 3.2 Parameters for CFD analysis S.No Parameter Value 1 Operating pressure kpa 2 SO 2 mass flow rate kg/s 3 H 2 O 2 mass flow rate kg/s 4 Inlet molar concentration of SO kmol/m 3 5 Inlet molar concentration of H 2 O kmol/m 3
23 59 A steady state liquid flow is considered for simulation studies. To obtain the converged solution, the injection of the liquid phase and continuous phase are turned on. After reaching the stable liquid-gas flow in the packed column, SO 2 absorption equation (based on two film theory) and chemical equations are activated and solved based on momentum and continuity equations as detailed in section The effect of the chemical reaction on SO 2 absorption based on the two-flim theory (Equations (3.17) and (3.18)) and the absorption of H 2 O 2 and SO 2 from the gas phase are implemented by calculating the mass transfer process for SO 2 from the continuous phase to the discrete phase. For a fixed L m /G m ratio (150 lph/40 m 3 /hr), SO 2 distribution field at the outlet portion of the gas stream is calculated, and the removal efficiency of SO 2 is defined as 1 -C SO2 (out)/c SO2 (in). Water as an absorbent The developed CFD model of a packed column is tested for the SO 2 removal efficiency when water is used as an absorbent. Figure 3.11 illustrates that the SO 2 initial concentration fed into the packed column is kmol/m 3. Absorption takes place only in the packed area where the gas-liquid interfacial area is more. Absorption starts at the region where high gas-liquid interaction takes place, which is at the packed area. Since water is used as an absorbent, the reaction between water and sulphur dioxide is immediate and permanent, provides 46% of SO 2 removal efficiency.
24 60 SO 2 outlet molar concentration kmol/m 3 Figure 3.11 CFD simulation result for water as an absorbent The Figure 3.11 also indicates that the concentration of SO 2 is contrasted with inlet and outlet of the packed area. This is due to the fact that the strong gradient of SO 2 concentration is absorbed below the packed area. The concentration of SO 2 is less at the top of the packed area after the gas liquid absorption takes place. Hence, less SO 2 concentration gradient is shown at the top of the packed column. At the outlet of packed area, the Figure 3.11 illustrates less gradients of SO 2 concentration since the small volume is defined as the cell which enhances the contact between gas and liquid. Therefore, the mass transfer at high volume takes place. Since the effect of the wall is not considered for analysis there is a high SO 2 concentration gradient results on the wall of the column.
25 61 H 2 O 2 as an absorbent Figure 3.12 shows the CFD simulation result for H 2 O 2 with 0.1M as its initial concentration. The figure 3.12 shows that the co-current section of the packed column gives more SO 2 removal efficiency than the counter current section. Though the SO 2 concentration in the flue gas is a smaller counter-current section, a packed area is used to enhance the contact between liquid and gas phases resultantly increasing the mass-transfer. SO 2 outlet molar concentration kmol/m 3 Figure 3.12 CFD simulation result for H 2 O 2 as an absorbent The Figure 3.12 indicates that the concentration of SO 2 is not uniform below and above the packed area which is due to mass transfer changes. Also the Figure 3.12 ensures that the concentration of SO 2 existing close to the outlet chamber has a lower SO 2 concentration. The Figure 3.12 shows the strong gradient at the inlet of the packed area, since SO 2 concentration in the inlet
26 62 gas is more. The behaviour of the HSO 3, SO 2 3 species in the gas and liquid phase increases the absorption rate. The concentration of the absorber (H 2 O 2 ) increases as SO 2 is absorbed in the packed column. The absorption performance of H 2 O 2 tremendously increases relative to the pure water. H 2 O 2 with 0.1M involves increasing the absorption rate with SO 2 up to n th iterations simulated using CFD and the removal efficiency obtained is 94.33%. From the CFD simulation analysis, it is clear that the parameters of the packed column selected based on the mathematical modelling produces removal efficiency of 94.33%. Moreover hydrogen peroxide can be used as an absorbent for the packed column as an attractive alternative solution to obtain maximum removal efficiency with no secondary pollutant resulting into the atmosphere. Simulation runs are estimated depending on the concentration of H 2 O 2 since further experimental analysis is focused on H 2 O 2 based desulphurization process. The CFD simulation results clearly show that the developed physical modelling parameters are well-suited to improve the removal efficiency of SO 2 more than 95% when hydrogen peroxide is used as an absorbent. Based on the simulation results, the modelling parameters are ensured for designing the lab scale experimental setup. 3.3 PACKED COLUMN FOR EXPERIMENTAL ANALYSIS Photographic view of the pilot plant packed column is developed based on CFD simulation results and mathematical modelling as shown in Figure The packed column is fabricated with acrylic material and its specifications which include: three stage gas distributor at the bottom for gas inlet with the diameter of 150 mm, packing material for 1m height, liquid sprayer at the top of the column with the diameter of 120 mm, diameter of the column with 150 mm and total height of the column with 2500 mm. Further experimental studies are carried out with the developed packed column detailed in the subsequent chapters.
27 63 Liquid Inlet Gas Outlet Spray Tower Packing Material (pp rings) Gas Distributor Gas Inlet Liquid Outlet Figure 3.13 Photographic view of the packed column
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