© 2022 IIETA. This article is published by IIETA and is licensed under the CC BY 4.0 license (http://creativecommons.org/licenses/by/4.0/).
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In various industrial processes such as petroleum refineries, crude oil must be heated to the required temperature. Here a study of a heat exchanger problem of a catalytic naphtha reforming unit of an SKIKDA refinery (RA1K) is carried out. In this unit the feed (naphtha and recycle gas) is required to enter the first reactor of the reaction section at 471℃, while the feed inlet temperature at the reactor is only 450℃. This problem appeared after starting the unit with a mass flow of 60% of the naphtha. The essential device for heating the charge before entering the reactor is shellandtube heat exchanger. In the present study, the Kern method is used to check the heat exchanger in the design and experimental cases. The Aspen HYSYS software has been used to study the influence of various naphtha mass flow rates on the thermal performance of a heat exchanger. The outlet feed temperature was examined for each mass flow rate of naphtha (i.e., 60, 70, 80, 90 and 100%). The simulation results show the important role of the studied parameters in the thermal performance enhancement of heat exchanger, where the case of a mass flow of 60% of the naphtha, the temperature 471℃, provided for by the design, is obtained with an H_{2}/HC ratio of 4.68.
heat exchanger, HYSYS simulation software, H_{2}/HC ratio, kern method, mass flow rate effect
Petroleum refineries obtain their energy needs through direct fuel fire for process heat and steam generation (for process use). Energy conservation is receiving a lot of attention as a result of the rising cost of energy. Heat exchangers can be used to recover otherwise lost thermal energy. It has the potential to lower the total amount of thermal energy consumed in industrial operations [1]. A heat exchanger is a device that transfers heat between two or more process fluids. Heat exchangers are used in a variety of industrial applications. Many different types of heat exchangers have been invented for use in chemical processing facilities [2]. In petroleum refineries, shell and tube heat exchangers are frequently employed as cooling or preheating systems [3, 4]. A shell and tube heat exchanger is constituted of tubes, shell, front and rear heads, baffles, and other components. Traditionally, shell and tube heat exchangers are designed using correlation based approaches such as the BellDelaware method and the Kern method [5]. These approaches form the basis of the existing shell and tube heat exchanger design [6]. Shell and tube heat exchangers can be singlephase, or twophase. A singlephase exchanger maintains the fluid's phase constant throughout the operation (e.g. liquid water enters, liquid water leaves) while a twophase exchanger will generate a phase change throughout the heat transfer operation (e.g. steam enters and liquid water leaves) [7]. As a result, understanding fluid flow and heat transfer in heat exchangers is critical for improving heat exchanger design. However, the experimental method is very costly and timeconsuming. With the advancement of computer technology, it is now feasible to use numerical methods to model a complex fluid flow and heat transfer process. The development of process simulation software for such petroleum related processes will give better advice for plant operations and lead to greater economic advantages. So far, the process simulation system has gone through various phases of development, beginning with a simulation object designed primarily for light hydrocarbon processing and progressing to a simulation object designed for a liquidgas twophase process and a liquidgassolid threephase process. In recent years, simulation has integrated dynamic and steady state technologies, and it has been widely employed in the research, design, and manufacturing departments. Typical commercial process simulation software consists of ChemCAD, AVEVA PRO/II, PetroSim, VMGSim and Aspen plus [8, 9]. ASPEN HYSYS is the one, which is used extensively. Many studies used Aspen HYSYS software to optimize industrial unit operating conditions. Hou et al. [10] used the Aspen Plus platform to optimize a catalytic reforming process unit. Zhang et al. [11] and Wang et al. [12] simulated the CO_{2} hydrate formation conditions in the process of gas phase CO_{2} pipeline transportation using HYSYS software. AlLagtah et al. [13] proposed certain modifications to an existing factory for the gas softening process in order to increase its profitability and durability by means of an optimization tool in Aspen HYSYS. Finally, Taqvi et al. [14] improved the efficiency of the distillation column for the acetone manufacturing unit using optimization techniques supplied by the Aspen Plus simulator.
On the other hand, Aspen HYSYS can solve the problem of determining the flow rate of cold and hot streams going through the heat exchanger in various stream conditions. In this simulation software, the heat exchangers are highly flexible as they can solve the problem of pressures, temperature and heat flows. Heat exchanger model can be selected for analysis purpose in Aspen HYSYS, it is able operate a heat exchanger and simulate the heat transfer process that occurs inside the heat exchanger [15]. Several researchers have used commercial simulators like Aspen HYSYS to simulate the fluid flow and heat transfer in heat exchangers. Yandrapu et al. [16] developed a model to simulate the production of methyl chloride. Using Aspen HYSYS, energy analysis improved the total utilities saving potential up to 36% by adding two new heat exchangers to the existing design. Yang et al. [17] proposed a simulationbased targeting method is proposed for placing of heat pumps in heat exchanger networks to minimize energy consumption, similar to HYSYS. Janaun et al. [15] modelled a heating unit to heat air for paddy drying in the heat exchanger, Aspen HYSYS was utilized to determine the minimum flow rate of hot water required.
In this context, we present here a study for a heat exchanger at the catalytic naphtha reforming unit (Magnaforming unit) of the SKIKDA refinery (RA1K). In this study, the thermal characteristics of the shell and tube heat exchanger in twophase flow (liquidgas) were investigated. In addition, the model has been utilized for investigating the effect of different walking parameters (mass flow rate, inlet temperature, gas/liquid ratio) on the thermal performance of heat exchanger using Aspen HYSYS software.
2.1 Description
The selected case study is the Catalytic Naphtha Reforming Unit (Magnaforming unit) of the SKIKDA refinery (RA1K). The process flow sheet is shown in Figure 1. Naphtha is sent to the reaction section from the naphtha pretreatment section. The naphtha is mixed with hydrogen rich recycle gas then, the feed (liquid naphtha and recycle gas) is pumped to heat exchanger at a temperature of 92℃, the feed temperature is raised to 454℃ through the heat exchanger, then fed to the furnace to reach a temperature of 471℃, and finally pumped to the first reactor of the reaction section. A large number of reactions occur in catalytic reforming over bifunctional catalysts, such as dehydroisomerization and dehydrogenation of naphthenes to aromatics, dehydrocyclization of olefins to aromatics, dehydrocyclization of paraffins to aromatics, dehydrogenation of paraffins to olefins, isomerization of alkyl cyclopentanes and substituted aromatics and hydrocracking of paraffins and naphthenes to lower hydrocarbons. In the first reforming reactor, the dehydrogenation of naphthenes is swift and strongly endothermic, a significant temperature drop occurs [18].
At the inlet of the first reactor of the reaction section at the catalytic reforming unit, the design temperature of 471°C was never reached after the startup of the unit with a mass flow of 60% of the naphtha, where 43687 kg/h).
The essential devices for heating the feed before entering the reactor are the furnace and the heat exchanger. The operation of the furnace is good, it gives a ∆T = 22°C instead of 17℃, the feed entering the heat exchanger on the shell side with a temperature of 95℃ instead of 92℃ and leaving with a temperature of 427℃ instead of 454℃. So there is a temperature loss of 27℃. The objective of this case study is to evaluate and optimize the heat exchanger to increase the temperature of the feed at the inlet of the first reactor. The main heat exchanger is analyzed using simulation software Aspen HYSYS.
2.2 Consequences of temperature decrease in refinery heat exchanger
The naphtha reforming process seeks to increase Low Research Octane (RON), the temperature and the H_{2}/HC ratio are the most important process factors. However, in order to optimize high octane products, certain processes operate at greater temperatures. As reformate RON increases with reactor temperature, for instance, an increase in RON from 90 to 95 should result in a temperature rise of about 23 ℃/RON, depending on the feedstock. This approach has been used in the SKIKDA refinery (RA1K) case study presented in this work. Low temperature at the reactor inlet causes: (1) incomplete chemical reactions, especially the dehydrogenation reaction of naphthenes to aromatics (the main reaction for the formation of aromatics where the octane number increases). (2) Decreased catalyst efficiency. (3) Higher energy consumption in the furnace to raise the temperature of the feed.
Figure 1. Simple flowchart for the case study
The catalytic naphtha reforming unit of the SKIKDA refinery uses a stainless steel shell and tube heat exchanger, the geometric parameters are summarized in Table 1. The feed (liquid naphtha and hydrogen rich recycle gas) goes through the shellside, whereas effluents from flows reactor 4 on the shellside (Figure 2), this process is a countercurrent heattransfer process. Given that the main target of the estimation is the outlet temperature, plant data (inlet temperatures and mass flow rates) were used for both parameter estimation and a check of simulations. The sharp drop in shellside flow rates could possibly be responsible for this large decrease in the temperature. In the present study, shell and tube heat exchanger is used to study the various parameters. Data sets utilized for developing this process model were obtained during normal operation.
Figure 2. Diagram of a typical shell and tube heat exchanger
Table 1. Shell and tube heat exchanger geometry
Variables 
Dimension 
Number of tubes (N_{T}) 
1039 
Length of tube (L_{T}) 
7000 mm 
Number of shell passes (N_{P}) 
1 
Number of tube passes (n_{p}) 
1 
Tube outside diameter (d_{0}) 
25.4 mm 
Tube inside diameter (d_{i}) 
21.184 mm 
Shell diameter (D_{s}) 
1375 mm 
Pitch (P) 
32.5 mm 
Distance between baffles (b) 
615 mm 
Tube bundle geometry 
Triangular 
In this research work, Kern method has been used to check shell and tube heat exchanger in the design and experimental cases [1921]. Calculations on the side of the tube and the shell have been performed to determine heat transfer coefficient, Overall heat transfer coefficient, overall thermal conductance etc. [2224]. The mathematical formulas used for the calculations will be presented later on in this article. Then, the Aspen HYSYS software has been used to study the influence of various naphtha mass flow rates and the H_{2}/HC ratio on the thermal performance of a shell and tube heat exchanger.
5.1 Energy balance
According to the first principle of thermodynamics, the heat transfer rate (Q) must also equal the rate of heat lost by the hot fluid stream and gained by the cold fluid stream, the energy balance equations for shellandtube heat exchangers are presented below [23]:
Q_{h} = Q_{c} (Energy Balance Equation)
$m_h C_{p, h}\left(T_{h, \text { in }}T_{h, \text { out }}\right)=m_c C_{p, c}\left(T_{c, \text { out }}T_{c, \text { in }}\right)$ (1)
where, T_{in} and T_{out} are the temperatures of the fluid at the inlet and the outlet respectively.
5.2 Heat transfer rate
5.2.1 Tube side
Figure 3. The vapor fraction of the heat exchanger inside tubes plotted as a function of the temperature
The vapor fraction of the heat exchanger inside tubes plotted as a function of the temperature is shown in Figure 3. Tube side heat exchanger keeps the fluid (effluent) phase constant throughout the process, steam enters and steam leaves. The rules for singlephase flow are then applied. The heat transfer rate of effluents is calculated as:
$Q_h=m_h C_{p, h}\left(T_{h, \text { in }}T_{h, \text { out }}\right)$ (2)
5.2.2 Shell side
In shellside the heat exchanger, two phases are present: a gas phase containing hydrogen and a liquid phase containing naphtha. The vapor fraction of the heat exchanger inside shell plotted as a function of the temperature is shown in Figure 4. As more heat is added the Naphtha progressively changes phase from liquid to vapor while maintaining the temperature at T_{v} =149℃ (design case).
Figure 4. The vapor fraction of the heat exchanger inside shell plotted as a function of the temperature
The rules for twophase flow are then applied. The heat transfer rate of feed is calculated as [25]:
$Q_c=\left[\left(m_v C_{p, v}\right)+\left(m_l C_{p, l}\right)\right]\left(T_vT_{c, \text { in }}\right)+L_v m_l+m_T C_{p, T}\left(T_{c, \text { out }}T_v\right)$ (3)
5.3 Heat transfer coefficient
5.3.1 Tube side heat transfer coefficient
The tube side heat transfer coefficient (h_{i}) can be determined as follows [19]:
$\mathrm{h}_{\mathrm{i}}=\mathrm{j}_{\mathrm{h}} \frac{\lambda_{\mathrm{i}}}{\mathrm{d}_{\mathrm{i}}}\left(\frac{\mathrm{C}_{\mathrm{pi}} \mu_{\mathrm{i}}}{\lambda_{\mathrm{i}}}\right)^{\frac{1}{3}}$ (4)
λ_{i} is the thermal conductivity, Cp_{i} is the speciﬁc heat, μ_{i} is the viscosity of the fluid in tube side at wall temperature, its value is not known a priori but it is calculated at (T_{m}).
The average fluid temperature (T_{m}) on the tube side was calculated using:
$T_m=\frac{\mathrm{T}_{\mathrm{in}}+\mathrm{T}_{\mathrm{out}}}{2}$ (5)
where, j_{h} is dimensionless thermal factor according to Kern method can be obtained from Figure A1 in Appendix.
Re is the Reynolds number in tube side, defined as in Eq. (6). It represents the vapor phase only flowing alone in the complete crosssection of the tube at the total mass velocity.
$\operatorname{Re}=\frac{\mathrm{G}_{\mathrm{t} \mathrm{d}_{\mathrm{i}}}}{\mu}$ (6)
G_{t} is the mass velocity, also known as mass flux, is defined by the mass flow rate divided by the total crosssectional area, is calculated as Eq. (7).
$\mathrm{G}_{\mathrm{t}}=\frac{\mathrm{m}_{\mathrm{t}}}{\mathrm{a}_{\mathrm{t}}}$ (7)
a_{t} is tube side ﬂow cross sectional area (m^{2}) per tube pass, expressible as:
$a_t=\frac{N t \pi i^2}{n_p 4}$ (8)
5.3.2 Shell side heat transfer coefficient
Many researchers proposed nondimensional correlations for forced convective heat transfer on different heat exchangers. Mandrusiak and Carey [24]; Wen and Ho [26]; Qiu and Zhang [27]. The general correlation for boiling heat transfer is given by Eq. (9). The correlation is represented using the LockhartMartinelli parameter X. In their research, they defined X as X_{tt}, where the liquid and vapor flowed turbulently. The subscript tt indicates that both phases are turbulent. Modes of calculating the LockhartMartinelli parameter for one of the two fluids moving in the laminar regime (X_{lt}, X_{tl}, X_{ll}) have been provided in the literature, but they are not necessary in this study.
McNaught [28] noted out that the relationships all ignore the interacting effects of vapor shear and inundation, and proposed that shellside condensation at high vapor velocities be considered as twophase forced convection. He therefore presumed that the high vapor velocity data can be correlated with Eq. (9).
$\frac{\mathrm{h}_{\mathrm{tp}}}{\mathrm{h}_{\mathrm{l}}}=\mathrm{a}\left(\frac{1}{\mathrm{X}_{\mathrm{tt}}}\right)^{\mathrm{b}}$ (9)
The Martinelli parameter X_{tt} is defined as [24]:
$X_{t t}=\left(\frac{1y}{y}\right)^{0.9}\left(\frac{\rho_{\mathrm{v}}}{\rho_1}\right)^{0.5}\left(\frac{\mu_1}{\mu_{\mathrm{v}}}\right)^{0.1}$ (10)
The singlephase heat transfer coefficient for liquid alone can be calculated by using the DittusBoelter/McAdams equation [19, 29]:
$\mathrm{h}_1=0.023\left(\frac{\lambda_{\mathrm{l}}}{\mathrm{d}_{\mathrm{e}}}\right)\left(\operatorname{Re}_1\right)^{0.8}\left(\operatorname{Pr}_1\right)^{0.4}$ (11)
The Prandtl number (Pr) is the ratio of the molecular diffusivity of momentum to the molecular diffusivity of heat, which can be expressed as:
$P r_l=\frac{C p_l \mu_l}{\lambda_l}$ (12)
Re_{l }is the Reynolds number in shell side, calculated as in Eq. (13).
$\operatorname{Re}_1=\frac{\mathrm{G}_{\mathrm{s}}(1\mathrm{y}) \mathrm{D}_{\mathrm{e}}}{\mu_{\mathrm{l}}}$ (13)
G_{s }is shell side mass velocity, defined by:
$\mathrm{G}_{\mathrm{s}}=\frac{\mathrm{m}_{\mathrm{s}}}{\mathrm{a}_{\mathrm{s}}}$ (14)
D_{e} is referred as the shell side equivalent diameter. For triangular pitch arrangement it is determined as Eq. (15).
$\mathrm{D}_{\mathrm{e}}=4\left(\frac{\frac{\sqrt{3}}{4} P^2\frac{\pi}{8} d_o}{\frac{\pi d_o}{2}}\right)=\frac{3,46 p^2}{\pi d_o}d_0$ (15)
a_{s} is shell side ﬂow cross, defined by:
$\mathrm{a}_{\mathrm{s}}=\frac{\mathrm{D}_{\mathrm{s}}}{\mathrm{p}}\left(\mathrm{p}\mathrm{d}_0\right) \mathrm{b}$ (16)
5.4 Overall heat transfer area
The surface area (A) of a shell and tube heat exchanger can be expressed as [25, 30]:
$A=\frac{Q}{U L M T D}$ (17)
The LMTD method of heat exchanger analysis is based on using the Eq. (18). LMTD is the log mean temperature difference and described as:
$L M T D=\frac{\Delta \mathrm{T}_1\Delta \mathrm{T}_2}{\operatorname{Ln} \frac{\Delta T_1}{\Delta T_2}}$ (18)
For a counter flow arrangement the ∆T’s are therefore ∆T_{1} = (T_{h,in}T_{c,out}) and ∆T_{2} = (T_{h,out}T_{c,in}).
Figure 5 depicts the heat transfer diagram along the heat exchangers. It was assumed that the heat transfer areas in the heat exchanger are divided into two zones (preheating zone and superheating zone) [25]. The heat transfer area of each region is a portion of the total heat transfer area of the heat exchanger, and defined as:
$\mathrm{A}=A_p+A_S$ (19 )
Figure 5. Variations of the temperature of the heat exchanger in terms of the heat transfer rate
Preheating zone
The heat transfer area in preheating zone (A_{p}) is calculated as [22]:
$A_p=\frac{Q_p}{U_p \text { LMTD }_p}$ (20)
The overall heat transfer coefficient (U_{p}) in preheating zone can be expressed by the following Eq. (21):
$\frac{1}{\mathrm{U}_{\mathrm{p}}}=\frac{1}{\mathrm{~h}_{\mathrm{i} 0}}+\frac{1}{\mathrm{~h}_{\mathrm{tp}}}+\sum \mathrm{R}_{\mathrm{f}}$ (21)
where, $\frac{1}{h_{t p}}, \frac{1}{h i o}$ and R_{f} are tubeand shellside heat transfer coefﬁcients (h.m^{2}°C/kcal), and tubeand shellside fouling resistances (h.m^{2}°C/kcal), respectively.
$\mathrm{h}_{\mathrm{i} 0}=\mathrm{h}_{\mathrm{i}} \frac{\mathrm{d}_{\mathrm{i}}}{\mathrm{d}_0}$ (22)
Superheating zone
The heat transfer area in superheating zone (A_{s}) is calculated as [22]:
$\mathrm{A}_{\mathrm{s}}=\frac{\mathrm{Q}_{\mathrm{s}}}{\mathrm{U}_{\mathrm{s}} \mathrm{LMTD}_{\mathrm{s}}}$ (23)
The overall heat transfer coefficient (U_{s}) in superheating zone can be expressed by the following Eq. (24):
$\frac{1}{\mathrm{U}_{\mathrm{s}}}=\frac{1}{\mathrm{~h}_{\mathrm{i} 0}}+\frac{1}{\mathrm{~h}_0}+\sum \mathrm{R}_{\mathrm{f}}$ (24)
Aspen HYSYS software was used to simulate the heat exchanger. The components chosen in Aspen HYSYS were naphtha, recycle gas, and effluent compositions (See Appendix Table A1A3). The thermodynamic model is Peng Robinson as a fluid package for the simulation basis. On the other hand, for component labelled ‘inlet hot’ was filled with effluent in component selection, and in the component that was labelled ‘Inlet cold’ was filled with Naphtha and recycle gas in component selection. The working conditions include input temperatures, mass ﬂowrate, pressure, and compositions provided from real project executed by RA1K. The design suggested to pumped naphtha and recycle gas in shell side and hot effluent in tube side. The naphtha mass flow is 7.28×10^{4} kg/h (100%), according to the configuration of the design. The heat exchanger was simulated and analyzed under the conditions of 100, 90, 80, 70 and 60 % of naphtha mass flow rate (the corresponding mass flow of naphtha is 7.28×10^{4}, 6.55×10^{4}, 5.83×10^{4}, 5.09×10^{4} and 4.36×10^{4} kg/h, respectively). The other values were left blank and Aspen HYSYS was used to simulate it.
A study is done on the shell and tube (H_{2}, HC/effluent) heat exchanger and various parameters are calculated for different mass flow rates and at varying inlet and outlet temperatures. Calculations shown in Tables 2 and 3 are made using Kern method for the two cases design and experimental (the corresponding mass flow of naphtha is 7.28×10^{4} and 4.36×10^{4} kg/h, respectively). And further readings are shown for different flow rates and comparison graphs are drawn. The Kern method is used for tube side heat transfer coefficient evaluation; for shell side heat transfer coefficient calculations, the LockhartMartinelli correlation is utilized in turbulent flow, the singlephase heat transfer coefficient for liquid alone was obtained using the DittusBoelter/McAdams equation.
According to the design, the parameters of the exchanger calculated by the Kern method are as follows: The temperature at the outlet of the shell side exchanger is 456°C, so this temperature is very close to the temperature according to the design (454℃), i.e. the exchanger is able to reach the desired temperature at the outlet of the shell side exchanger. In the experimental case, the Kern method was used to determine the value of the feed temperature at the outlet of the exchanger on the shell side, which is about 430°C. It can be seen that this temperature is low compared to the one expected according to the design (454℃); however, the value of the temperature currently measured in the unit is about 427°C, this temperature (427℃) is very close to the determined temperature (430℃), and although the feed entering the heat exchanger with a temperature of 95℃ instead of 92℃ in the design case (there is therefore a temperature gain of 3℃) it remains that the outlet temperature (427℃) is lower than that of the design 454℃. And this loss of 27℃ in temperature influences the quality of the gasoline since 2℃ increases a RON number.
The computed overall thermal conductance (UA), the total heat transfer rates, the outlet temperature of shellside heat exchanger, the logmean temperature difference (LMTD) and H_{2}/HC ratio for two cases (design and experimental) are shown in Table 4. From the results given in Table 4, for the design case, the computed overall thermal conductance by using the Kern method and the HYSYS simulation software were calculated to be 2.09×10^{5} and 2.13×10^{5} kcal/°C.h, respectively, but this computed value was about 1.08×10^{5} and 1.14×10^{5} kcal/℃.h for the experimental case.
Table 2. The results for the shell side are shown below
Description 
Design 
Experimental 
T_{c, in }(℃) 
92 
95 
T_{c, out} (℃) 
457 
430 
m_{H2 }(kg/h) 
2.47×10^{4} 
1.76×10^{4} 
m_{naphtha }(kg/h) 
7.28×10^{4} 
4.36×10^{4} 
C_{P, H2 }(Kcal/kg.℃) 
0.7599 
0.7690 
C_{p, ,naohtha }(Kcal/kg.℃) 
0.5908 
0.5889 
C_{pt }(Kcal/kg.℃) 
0.8172 
0.8650 
L_{v }(Kcal/kg) 
79.2 
79.0 
a_{s }(m^{2}) 
0.1847 
0.1847 
D_{e }(m) 
0.0247 
0.0247 
G_{s }(kg/h.m^{2}) 
52.83×10^{4} 
33.21 ×10^{4} 
X_{tt} 
0.1465 
0.1199 
Re_{l} 
7.15×10^{3} 
4.016×10^{3} 
Pr_{l} 
5.3737 
5.37 
h_{l }(Kcal/h.m^{2}.℃) 
235.03 
147.36 
h_{tp }(Kcal/h.m^{2}.℃) 
21.48×10^{2} 
14.89×10^{2} 
j_{h} 
138 
135 
h_{0 }(Kcal/h.m^{2}.℃) 
747.54 
712.87 
Table 3. The results for the tube side are shown below
Description 
Design 
Experimental 
m_{effluents }(kg/h) 
16.94×10^{4} 
10.44×10^{4} 
T_{h, out} (℃) 
360 
363 
T_{h, in} (℃) 
516 
514 
a_{t }(m^{2}) 
0.366 
0.366 
G_{t }(kg/h.m^{2}) 
46.30 ×10^{4} 
28.54 ×10^{4} 
Re 
65.34×10^{3} 
40.27×10^{3} 
j_{h} 
165 
128 
C_{pi }(Kcal/kg.℃) 
1.188 
1.189 
μ_{i }(kg/m.h) 
0.1501 
0.1501 
h_{i }(Kcal/h.m^{2}.℃) 
14.52×10^{2} 
11.27×10^{2} 
h_{i0 }(Kcal/h.m^{2}.℃) 
12.11×10^{2} 
9.40×10^{2} 
The comparisons presented by Table 4, show that the agreement between the results obtained by the Kern method and the simulated results is quite good. As the results obtained by the simulation gives temperatures at the outlet of the shellside heat exchanger close to the Kern method. For this we will carry out a technical study to find a solution. Then, with the HYSYS simulation software, variations of the shell side heat transfer coefficient and overall thermal conductance vs naphtha mass flow are investigated. Finally, the effects of H_{2}/HC ratio and different mass flow of the feed on outlet temperature of shellside heat exchanger are investigated.
Table 4. Results of analytical and numerical calculations for the design and experimental cases

Kern 
HYSYS Simulation 

Description 
Design 
Experimental 
Design 
Experimental 
U.A (Kcal/℃. h) 
2.09×10^{5} 
1.08×10^{5 } 
2.13×10^{5} 
1.14×10^{5} 
Q (Kcal/h) 
31419086 
18757030 
31470085 
18783507 
T_{c, out }(℃) 
457 
430 
453 
431 
LMTD (℃) 
146.2 
162.5 
147.8 
164.6 
H_{2}/HC 
4.68 
5.56 
4.68 
5.56 
7.1 Eﬀect of naphtha mass flow on heat transfer coeﬃcient
Figure 6 show the variation of the two phase heat transfer coefficient versus mass flow rate ratio. Also, the mass flow rate ratio (γ) is determined as follows:
$\gamma=\frac{\mathrm{m}_{\mathrm{H} 2}}{\mathrm{~m}_{\mathrm{H} 2}+\mathrm{m}_{\text {naphtha }}}$ (25)
Figure 6. Variations of heat transfer coefficient of hydrogennaphtha the two phase flow vs (γ)
From Figure 6, it is observed that raising the naphtha mass flow rate induces an increase in the two phase heat transfer coefficient. Also, it could be seen that the mass flow rate ratio is an important parameter influencing on the trend of the heat transfer coefficient. By increasing the mass flow rate ratio value, heat transfer coefficient decreases, this phenomenon could be interpreted in a way that as the mass flow rate ratio increases at the constant naphtha mass flow (increment in the hydrogen mass flow rate or decrement in the naphtha mass flow rate), actually, larger amounts of superficial are associated with higher hydrogen flow rates, which would cause bigger slugs. These bigger slugs are less frequent and prevent disruption of the naphtha flow. Bigger slugs could lead in the heat transfer coefficient decreases [31].
Figure 7. Variations of heat transfer coefficient of hydrogennaphtha twophase flow per single phase (naphtha) vs (γ)
Figure 7 depicts the relationship between heat transfer ratio (two phase per single phase) and mass flow rate ratio. As shown in Figure 7, the heat transfer coefficient of two phase flow is higher than that of single phase flow. It is believed that at least one of the following mechanisms is responsible for the increase in heat transfer coefficient of two phase flow than that of single phase flow. The mechanisms are as follows:
 The Reynolds number is increasing: according to the continuity equation, injecting of the H_{2} into the shell reduces the volume fraction of naphtha and as a result the local velocity of naphtha elements increases, as the liquid phase moves quicker, the Re number of the liquid phase also increases. Increment in Reynolds number leads to increment of heat transfer coefficient.
 Interaction between hydrogen bubbles and Naphtha elements: another important mechanism which could responsible for the increase in heat transfer coefficient between the hydrogen bubbles and Naphtha elements. The hydrogen bubbles move along the shell with higher velocity amount than the naphtha elements. However, when hydrogen bubbles move with higher velocity than naphtha elements, the hydrogen bubbles crash with naphtha elements, transmitting the kinetic energy of hydrogen bubbles to naphtha elements making them to have more velocity fluctuations. Subsequently, the turbulence intensity of flow increases, this leads to increment of heat transfer coefficient.
7.2 Eﬀect of naphtha mass flow on overall thermal conductance (UA)
In this paper, overall thermal conductance (UA) is determined by multiplying the overall heat transfer coefficient (U) and the effective surface area (A) of the heat exchanger.
Figure 8. Variations of UA in the heat exchanger with the naphtha mass flow rate
Figure 9. Variations of LMTD in the heat exchanger with the naphtha mass flow rate
In the heat exchanger system, the amount of adsorbent mass in the heat exchanger is one of the most influential parameters. Therefore, the influence of naphtha mass flow rate on the system performance varying mass flow rate in shellside is discussed: Figure 8 shows the effect of mass flow rate in shellside on overall thermal conductance, where the abscissa represents the mass flow rate of naphtha. In Figure 8, naphtha mass flow rate in shellside varies from 4.36× 10^{4} to 7.28 ×10^{4} Kg/h. It can be seen from Figure 8 that UA increases with the increase in naphtha mass flow on the shell side. For example, UA is 1.14 × 10^{5} kcal/℃.h at mass flow rate of naphtha of 4.36 × 10^{4} kg/h. With the increase in mass flow rate of naphtha to 5.82 × 10^{4} kg/h, UA increases by 23% to 1.14 × 10^{5} kcal/°C.h. From Figure 8, we can also see that maximum overall thermal conductance (UA) can be obtained at mass flow rate of naphtha about 7.28 × 10^{4} kg/h. Therefore, the change in UA values is mainly due to the change in mass flow rate of naphtha. This is because large UA value means large heat transfer area or high heat transfer coefficient or both, which results in high performance.
Based on Figure 9, it can be seen that with increasing the mass flow rate ratio value the logarithmic temperature difference (LMTD) of the heat exchanger has decreases, this leads to increment of overall heat transfer coefficient of the heat exchanger. The lowest logarithmic temperature difference (LMTD) occurred for mass flow rate of 7.28 ×10^{4} Kg/h. The amount of LMTD was about 143℃.
Figure 10 shows the variations of the overall heat transfer coefficient of the heat exchanger vs of the heat transfer rate. As shown in Figure 10, the total heat transfer coefficient has also increased with increasing fluid heat transfer rate. The highest heat transfer rate occurred for a mass flow of 7.28×10^{4} Kg/h. The amount of heat transfer was about 31470085 kcal/h.
Figure 10. Variations of U in the heat exchanger with the heat transfer rate
7.3 Eﬀect of H_{2}/HC ratio on outlet temperature of shellside heat exchanger
The hydrogen/hydrocarbon (H_{2}/HC) ratio is defined as the number of moles of hydrogen recycled per mole of naphtha charged to the unit. For studying the influence of the H_{2}/HC ratio on outlet temperature of shellside heat exchanger, using the HYSYS simulation software, the following procedure can be used: The mass flow rate of the naphtha in the experimental case and the inlet temperatures are fixed and the hydrogen flow rate sent by the compressor is varied. The summary of the results so obtained have been presented in Table 5.
Table 5. Influence of H_{2}/HC ratio on outlet temperature of shellside heat exchanger
Mass flow rate of naphtha (kg/h) 
Mass flow rate of H_{2} (kg/h) 
H_{2} /HC ratio 
Temperature (T_{c, out}) (℃) 
43687 
17656 
5.56 
428.4 
43687 
16500 
5.19 
438.0 
43687 
16000 
5.04 
442.3 
43687 
15500 
4.88 
446.7 
43687 
15000 
4.72 
451.2 
43687 
14868 
4.68 
454.0 
Figure 11 shows the variations of the outlet temperature of shellside heat exchanger vs of the H_{2}/HC ratio. As shown in Figure 11, it can be seen that the gradual decrease in the H_{2}/HC ratio makes it possible to increase the outlet temperature of shellside heat exchanger. The highest outlet temperature of shellside heat exchanger occurred for H_{2}/HC ratio of 4.68. The value of outlet temperature of shellside heat exchanger was about 454℃. We notice that with hydrogen mass flow rate of 14868 kg/h, the value of H_{2}/HC ratio was about 4.68. This value is very close to the value of the H_{2}/HC ratio in the design case (Table 4). Furthermore, outlet temperature of shellside heat exchanger was about 454℃. This value is very close to the desired value in the design case (454℃).
In the design, case the H_{2}/HC ratio used is about 4.68 (Table 4). But, in the experimental case this ratio is about 5.56 (table 4). Note that the H_{2}/HC ratio in the experimental case is higher than the H_{2}/HC ratio in the design case. That is to say that the quantity of hydrogen put in circulation by the compressor in the experimental case does not correspond to the quantity of hydrocarbon used with a mass flow of 60% of the naphtha where 43687 kg/h.
In the primary reforming reactor, the dehydrogenation of naphthenes is rapid and highly endothermic, a significant temperature decrease happens. This effect is minimized by lowering the hydrogen supply to the first reactor, which also lowers the amount of gas produced as a result of hydrocracking. Under project conditions, in order to protect the catalyst, the H_{2}/HC ratio must be held at or above the minimum value of 3 on the 1st reactor of the magnaforming section, so this value (4.68) is valid for the project conditions.
7.4 Effect of different mass flow of the feed on outlet temperature of the shellside heat exchanger
In practice, the catalytic reforming unit is currently operating at a naphtha flow rate of 60% of the design flow rate. The hydrogen flow rate used in this case has caused major problems, especially in the outlet temperature of the shellside heat exchanger. For confirm the results given by the previous study, influence of the H_{2}/HC ratio on the outlet temperature of the shellside heat exchanger, it was considered to vary this ratio with different mass flow rates of naphtha, according to the following cases: 100%, 90%, 80%, 70% and 60%. Thus, the quantity of naphtha is fixed and the quantity of H_{2} is varied. The simulation results are shown in Figure 12. As shown in Figure 12, it can be seen that the decrease of the naphtha flow rate does not influence the temperature at the exchanger outlet, but with a hydrogen flow rate corresponding to the naphtha flow rate.
By examining these values, we deduce that it is indeed the H_{2}/HC ratio close to 4.6 that gives the temperature expected according to the design (Table 6).
Figure 11. Variations of outlet temperature of the shellside heat exchanger with the H_{2}/HC ratio
Figure 12. Variations of outlet temperature of the shellside heat exchanger with the H_{2} mass flow rate
Table 6. Influence of different mass flow of the naphtha on outlet temperature of the shellside heat exchanger
Mass flow rate (%) 
Mass flow rate of naphtha (kg/h) 
Mass flow rate of H_{2} (kg/h) 
H_{2} /HC ratio 
Temperature (T_{c, out}) (℃) 
100% 
72812 
24781 
4.68 
454 
90% 
65531 
22303 
4.68 
454 
80% 
58249 
19825 
4.68 
454 
70% 
50968 
17346 
4.68 
454 
60% 
43687 
14868 
4.68 
454 
In this work the existing heat exchanger of the catalytic naphtha reforming unit was analysed by applying Kern method and Aspen HYSYS simulation software. Experiments were performed to characterize the thermal performances of the heat exchangers. The thermal performance indicators such as the heat transfer coefficient (h_{i}), overall heat transfer coefficient (U), overall thermal conductance (UA), logarithmic temperature difference (LMTD), and mass flow rates for fluids circulating inside the heat exchanger were determined. The results reveal that the ratio two fluids are supplied to the heat exchanger significantly matters in this issue: the flow maldistribution has an important impact on the thermal performances of shell and tube heat exchangers if two fluids are supplied from the same side. Moreover, the flow maldistribution due to due to the decrease in the temperature of the fluids at the outlet of the heat exchanger. It is observed that the degradation in performance is severe for low mass flow rates application. In the present case of shell and tube heat exchanger, it was found that the studied heat exchanger is competent for the duty of heat transfer. It means the feed (naphtha and recycle gas) at 92℃ can be heated to 454℃ by this heat exchanger with hot effluent at 530℃. So, the temperature of feed also can be achieved for low naphtha mass flows rates, but with a H_{2}/HC ratio in the scope of demand (4.68). These results demonstrated the potential of using Aspen HYSYS software to simulate industrialscale heat exchangers with enhanced heat transfer performances. As a result of this, it is recommended that the refinery modifies the H_{2}/HC ratio currently used.
The authors gratefully acknowledge RA1K for the data provided, the industrial members of the catalytic naphtha reforming unit for useful discussions, feedback and encouragement.
A 
Heat transfer area, m^{2} 
a_{s} 
Shellside ﬂow cross sectional area, m^{2} 
a_{t} 
Tubeside ﬂow cross sectional area, m^{2} 
b 
Distance between baffles, mm 
C_{p} 
Specific heat, kcal /kg ℃ 
d_{0 } 
Tube outside diameter, mm 
d_{i } 
Tube inside diameter, mm 
D_{s } 
Shell diameter, mm 
D_{e} 
Diameter equivalent, mm 
G_{s} 
Shell side mass velocity, kg/m^{2} h 
G_{t} 
Tube side mass velocity, kg/m^{2} h 
h 
heat transfer coefficient, kcal/hm^{2} ℃ 
j_{h} 
thermal factor according to Kern method 
U 
Overall heat transfer coefficient, kcal/hm^{2} ℃ 
L_{T} 
Length of tube, mm 
LMTD 
Logmean temperature difference, ℃ 
L_{v} 
Latent heat of vaporization, kcal/kg 
m 
Mass flow rate of the fluid, kg/h 
N_{T} 
Number of tubes 
N_{P} 
Number of shell passes 
n_{p} 
Number of tube passes 
P 
Pitch, mm 
Pr 
Prandtl number 
Q 
Heat transfer rate, kcal/h 
Re 
Reynolds number 
R_{f} 
Fouling resistance, hm^{2}℃/kcal 
∆T_{1} 
Temperature difference at the hot fluid side, ℃ 
∆T_{2} 
Temperature difference at the cold fluid side, ℃ 
T_{m} 
Mean fluid temperature, ℃ 
Greek symbols 

λ 
thermal conductivity, kcal/hm℃ 
γ 
mass flow rate ratio 
ρ 
density, kg/m^{3} 
µ 
dynamic viscosity, kg/m.h 
Subscripts 

c 
Cold 
e 
Equivalent 
h 
hot 
in 
Inlet 
l 
Liquid 
out 
Outlet 
s 
Shell 
t 
Tube 
tp 
two phase 
v 
Vapor 
Table A1. Composition (mol %): effluent
Component 
mol % 
Hydrogen 
82.614 
Methane 
5.4355 
Ethane 
2.9396 
Propane 
2.1284 
iButane 
0.7390 
nButane 
1.0967 
iPentane 
0.2034 
nPentane 
1.4631 
nHexane 
0.3809 
nHeptane 
0.2968 
nOctane 
0.0185 
nNonane 
0.0086 
Cyclohexane 
0.0185 
1,1 methylcyclopentane 
0.0.007 
Benzene 
0.4273 
Toluene 
0.7885 
Ethylbenzene 
0.2649 
pXylene 
0.2112 
mXylene 
0.4027 
oXylene 
0.2312 
1 methyl 3 ethylbenzene 
0.3260 
Table A2. Composition (mol %): recycle gas
Component 
mol % 
Hydrogen 
83.9 
Methane 
4.8 
Ethane 
4.3 
Propane 
3.7 
iButane 
1.1 
nButane 
1.4 
iPentane 
0.1 
nPentane 
0.4 
nHeptane 
0.3 
Table A3. Composition (mol %): Naphtha
Component 
mol % 
iPentane 
1.09 
nPentane 
1.00 
nHexane 
9.73 
nHeptane 
21.27 
nOctane 
18.48 
nNonane 
7.49 
nDecane 
2.28 
Cyclopentane 
0.19 
Cyclohexane 
2.6 
Methylcyclopenta 
2.12 
1,1 methylcyclopentane 
13.00 
1, 1, 2 methylCyclopentane 
8.66 
1, 1, 3 methylCycC6 
3.01 
1, 2, 3, 4 titra methyl cyclo C6 
0.25 
Benzene 
1.20 
Toluene 
2.8 
Ethylbenzene 
0.61 
pXylene 
0.55 
mXylene 
1.47 
oXylene 
0.78 
1, 2, 3 methylbenzene 
1.42 
Figure A1. Tube side heat transfer factor [20]
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