An Energy Production System Powered by Solar Heat with Biogas Dry Reforming Reactor and Solid Oxide Fuel Cell

Akira Nishimura¹, Ryotaro Sato¹, Eric Hu²

¹Division of Mechanical Engineering, Graduate School of Engineering, Mie University, Tsu, Japan.
²School of Electrical Mechanical Engineering, The University of Adelaide, Adelaide, Australia.

DOI: 10.4236/sgre.2023.145006                

Abstract

In this paper, an energy system consisting of solar collector, biogas dry reforming reactor and solid oxide fuel cell (SOFC) has been proposed. The heat produced from the concentrating solar collector is used to drive a biogas dry reforming reactor in order to produce H₂ as a fuel for SOFC, in such as system. The aim of this study is to clarify the impact of climate data on the performance of solar collector with various sizes/designs. The temperature of heat transfer fluid produced by the solar collector is calculated by adopting the climate data for Nagoya city in Japan in 2021. The amount of H₂ produced from the biogas dry reforming reactor and the power generated by SOFC were simulated. The results show the temperature of heat transfer fluid (T_fb) and T_fb ratio (a) based on the length of absorber (dx) = 1 m have a peak near the noon following the trend of solar intensity (I). Results also revealed that a increases with increase in dx. It is found that the differences of T_fb and a between dx = 2 m and dx = 3 m are larger than those between dx = 1 m and dx = 2 m. It is revealed that T_fb and a are higher in spring and summer. dx = 4 m is the optimum length of solar absorber. The amount of H₂ produced from the biogas dry reforming reactor as well as the power generated by SOFC is the highest in August, resulting that it is prefer to produce H₂ and to generate SOFC in summer.

Keywords

Solar Collector, Fluid Temperature, Climate Data, Biogas Dry Reforming, H₂ Production, SOFC

1. Introduction

Global warming has been a serious problem in the world. Renewable energy is one of promising procedure to solve the global warming problem. According to Energy White Paper 2022 in Japan [1] , the ratio of renewable energy to the whole energy consumption in the world is 5.7% in 2020. To realize a net zero emission society, it is suggested that the supply of renewable energy should be 7919 million oil equivalent tons in 2050, while the whole energy supply is 12,967 million oil equivalent ton [1] . As the other procedure to solve the global warming problem, a renewable H₂ is a candidate. H₂O is emitted only after utilization of H₂O as a fuel for fuel cell. There are several techniques to produce H₂ from fossil fuels such as natural gas, coal and oil. However, they are needed to combine the carbon capture storage (CCS) or usage (CCU) technology for realization of a net zero emission society.

This study focuses on a biogas dry reforming to produce H₂. Biogas is a gaseous fuel consisting of CH₄ (55 - 75 vol%) and CO₂ (25 - 45 vol%) [2] , mainly produced from fermentation by the action of anaerobic microorganisms on raw materials such as, garbage, livestock excretion, and sewage sludge. Additionally, the conversion of biogas to H₂ can be said as a carbon neutral since the CO₂, which is a by-product in the biogas production process, can be absorbed by plants. It is reported from the International Energy Agency (IEA) [3] that the biogas has been produced 62.3 billion·m³ globally with an equivalent energy of 1.43 EJ in 2019. The amount of produced biogas in 2019 has been five times as large as that in 2000. Consequently, it is thought that the biogas is a promising energy source. Generally speaking, the biogas is used as a fuel for gas engine or micro gas turbine [4] . Since a biogas contains CO₂ of approximately 40 vol%, the efficiency of power generation decreases due to smaller heating value compared to natural gas. This study proposes the H₂ production from biogas dry reforming to utilize as a fuel for solid oxide fuel cell (SOFC) system. SOFC can also use CO which is a by-product from biogas dry reforming as a fuel, resulting in the effective energy production system.

Since the biogas dry reforming is an endothermic reaction, this study proposes the combination system with a solar collector. In the previous studies by the authors [5] [6] , the biogas dry reforming has been conducted by the heat input using the electric heater. Then, CO₂ is emitted due to usage of the electricity generated by Japanese electric power company which uses a fossil fuel actually now. Therefore, the authors hit on the new system consisting of solar collector, biogas dry reforming reactor and SOFC. There is no previous report on the concept of this type.

According to the literature survey by the authors, a parabolic trough collector is the most established solar concentration technology worldwide [7] . The temperature of heat transfer fluid can be attained approximately 723 K by a parabolic trough collector [7] [8] [9] . The impact of concentration ratio on the relationship between the temperature of heat transfer fluid and energy efficiency was investigated [8] . The concentration ratio was changed from 10 to 30. There is the optimum concentration ratio to obtain the higher temperature of heat transfer fluid, which is the concentration ratio of 20. The effect of configuration of parabolic trough collector, e.g. solar incidence angle [9] on the collector efficiency and the optimal loss was investigated. When the mass flow rate of heat transfer fluid increases, the heat loss decreases due to promotion of convective heat transfer between the tube wall and the heat transfer fluid. There are several reports on the heat transfer model for investigation of parabolic trough collector [8] [9] [10] [11] . The heat transfer model considers a conduction, a convection and a radiation heat transfer. The double pipes structure model considering heat loss to the atmosphere can estimate the temperature of heat transfer fluid changing the solar intensity, the mass flow rate of fluid, the diameter and length of glass tube [10] . Though the previous studies developed the heat transfer model, there is no study investigating the impact of climate data on the performance of solar collector changing the shape of solar collector. In addition, there is no study to estimate the amount of H₂ produced from the biogas dry reforming reactor when assuming to use the heat obtained from the solar collector for the biogas dry reforming. Moreover, there is no study to estimate the power generated by SOFC consisting of solar collector and biogas dry reforming reactor.

The aim of this study is to clarify the impact of climate data on the performance of solar collector changing the shape of solar collector. This study refers the developed heat transfer model investigating the parabolic trough collector [10] . The temperature of heat transfer fluid is calculated by adopting the climate data for Nagoya city in Japan in 2021 [12] . The diameter and the length of heat absorber are changed for this analysis. In addition, this study also aims to estimate the amount of H₂ produced from the biogas dry reforming reactor when assuming to use the heat obtained from the solar collector for the conduction of biogas dry reforming. In this study, the specific characteristics of biogas dry reforming reactor developed by the authors [5] [6] are adopted to estimate the amount of produced H₂. Moreover, this study also aims to estimate the power generated by SOFC consisting of solar collector and biogas dry reforming reactor. The power generation efficiency of commercial SOFC is adopted to estimate the power generated by SOFC in this study.

2. Analysis Procedure

2.1. Heat Transfer Model for Solar Collector

Figure 1 illustrates the schematic diagram for heat transfer model of parabolic trough collector. The heat transfer mechanism in this model is explained in the caption of Figure 1. Figure 2 shows the thermal resistance distance diagram for the heat transfer process in this model. Each thermal resistance is explained in the caption of Figure 2.

This study assumes that the surrounding surface temperature is equal to the ambient air temperature. The model equation for a single glass cover can be explained as follow [10] :

$I\alpha \tau D\pi dx=\frac{T_{\text{to}}-T_{\text{fb}}}{R_1}+\frac{T_{\text{to}}-T_{\text{s}}}{{\left(R_5^{-1}+R_6^{-1}\right)}^{-1}}$ (1)

Figure 1. Schematic diagram for heat transfer model of parabolic trough solar collector (A solar radiation is mainly absorbed at the outlet surface of the absorber tube as a heat [10] . Some parts of the absorbed heat transports to the working/heat transfer fluid by conduction through tube wall and convection from the inner surface of the tube to the fluid. Other parts of the heat transfers as a loss by radiation to the inner surface of the glass through the vacuum space and then by conduction from the inner surface of the glass to the outer surface of the glass. The heat transferred to ambient from the outlet surface of the glass by two mechanisms, i.e. the convection to the surrounding air and the radiation to the surrounding surfaces, e.g. buildings and sky).

Figure 2. Thermal resistances diagram of the heat transfer model in this study (R₁: thermal resistance by thermal convection from the heat transfer fluid to the absorber [K/W], R₂: thermal resistance by thermal conduction through the absorber [K/W], R₃: thermal resistance by radiation through vacuum [K/W], R₄: thermal resistance by thermal conduction through the glass tube [K/W], R₅: thermal resistance by thermal convection to the ambient air [K/W] and R₆: thermal resistance by radiation to the surrounding surfaces (buildings and sky)).

$mc\frac{d{T}_{\text{fb}}}{dx}=mc\frac{T_{\text{fb},\text{out}}-T_{\text{fb},\text{in}}}{dx}=\frac{T_{\text{to}}-T_{\text{fb}}}{R_1}$ (2)

$\frac{T_{\text{to}}-T_{\text{gi}}}{R_3}=\frac{T_{\text{to}}-T_{\text{s}}}{R_3+{\left(R_5^{-1}+R_6^{-1}\right)}^{-1}}$ (3)

where, I means a solar intensity [W/m²], α means an absorptivity of absorber tube [-], τ means a transmissivity of glass tube [-], D means a diameter of absorber [m], dx means a length of absorber [m], m means a mass flow rate of heat transfer fluid which is assumed to be a biogas [kg/s], c is a specific heat of heat transfer fluid [J/(kg·K)], T_fb means a temperature of heat transfer fluid [K], T_fb,out means a temperature of heat transfer fluid at outlet [K] and T_fb,in means a temperature of heat transfer fluid at inlet [K]. Each thermal resistance can be defined as follows:

$R_1=\frac{1}{2\pi r_{\text{ti}}h}$ (4)

$R_2=\frac{1}{2\pi k_{\text{t}}}\ln \frac{r_{\text{to}}}{r_{\text{ti}}}$ (5)

$R_3=\frac{1}{2\pi \sigma r_{\text{to}}}\left[\frac{1}{{\epsilon }_{\text{t}}}+\frac{1-{\epsilon }_{\text{g}}}{{\epsilon }_{\text{g}}}\left(\frac{r_{\text{to}}}{t_{\text{gi}}}\right)\right]{\left[\left(T_{\text{to}}^2+T_{\text{gi}}^2\right)\left(T_{\text{to}}+T_{\text{gi}}\right)\right]}^{-1}$ (6)

$R_4=\frac{1}{2\pi k_{\text{g}}}\ln \frac{r_{\text{go}}}{r_{\text{gi}}}$ (7)

$R_5=\frac{1}{2\pi r_{\text{go}}{h}_{\text{o}}}$ (8)

$R_6=\frac{1}{{\epsilon }_{\text{g}}\sigma 2\pi r_{\text{go}}\left(T_{\text{go}}+T_{\text{s}}\right)\left(T_{\text{go}}^2+T_{\text{s}}^2\right)}$ (9)

where, r_ti means an inside radius of absorber [m], r_to means an outside radius of absorber [m], r_gi means an inside radius of glass tube [m], r_go means an outside radius of glass tube [m], σ means Stefan-Boltzmann constant [W/(m²·K⁴)], h means the heat transfer coefficient between heat transfer fluid and inside surface of absorber [W/(m²·K], h_o means the heat transfer coefficient from outside surface of glass tube to atmosphere [W/(m²·K)], k_t means a thermal conductivity of absorber [W/(m·K)], k_g means a thermal conductivity of glass tube [W/(m·K)], ε_t means an emissivity of absorber [-], ε_g means an emissivity of glass tube [-], T_to means a temperature of outside surface of absorber [K], T_gi means a temperature of inside surface of glass tube [K], T_go means a temperature of outside surface of glass tube [K], T_s means a temperature of surroundings surface [K], and T_a means a temperature of surrounding air [K].

2.2. Estimation of Heat Transfer Coefficient

In this study, the heat transfer coefficient for the turbulent flow in a tube is followed by Dittus-Boelter correlations [13] :

$\text{Nu}=0.023{\mathrm{Re}}^{0.8}{\mathrm{Pr}}^{1/3}$ (10)

$\text{Nu}=\frac{hD}{k_{\text{a}}}$ (11)

$\mathrm{Re}=\frac{{\rho }_{\text{a}}{u}_{\text{a}}D}{{\mu }_{\text{a}}}$ (12)

$\mathrm{Pr}=\frac{C_{\text{p},\text{a}}{\mu }_{\text{a}}}{k_{\text{a}}}$ (13)

$h_{\text{o}}=0.0191+0.006608u_{\text{a}}$ (14)

where, C_p,a means a specific heat of surrounding air [J/(kg·K)], μ_a means a viscosity [Pa·s], k_a means a thermal conductivity of surrounding air [W/(m∙K)], u_a means a velocity of surrounding air [m/s] and ρ_a means a density of surrounding air [m/s].

2.3. Calculation Procedure

According to Equations (1) and (2), the following equation can be obtained:

$T_{\text{fb},\text{out}}=\frac{dx}{mc}\left\{I\alpha \tau D\pi dx-\frac{\left(T_{\text{to}}-T_{\text{s}}\right)\left(R_5+R_6\right)}{R_3\left(R_5+R_6\right)+R_5{R}_6}\right\}+T_{\text{fb},\text{in}}$ (15)

Moreover, R₃ is obtained according to Equation (3) as follows:

$R_3=\frac{\left(T_{\text{to}}-T_{\text{gi}}\right)R_5{R}_6}{\left(R_5+R_6\right)\left(-T_{\text{s}}+T_{\text{gi}}\right)}$ (16)

From Equations (6) and (16), T_to can be calculated as follows:

$T_{\text{to}}={\left[\frac{\left(R_5+R_6\right)\left(-T_{\text{s}}+T_{\text{g}}\right)}{2\pi \sigma r_{\text{to}}{R}_5{R}_6}\times \frac{\left\{r_{\text{gi}}+r_{\text{to}}\left(1-{\epsilon }_{\text{g}}\right)\right\}}{{\epsilon }_{\text{t}}{r}_{\text{gi}}}+T_{\text{gi}}^4\right]}^{\frac{1}{4}}$ (17)

In this study, T_fb is estimated by averaging T_{fb, in} and T_{fb, out} as follows:

$T_{\text{fb}}=\frac{T_{\text{fb},\text{out}}+T_{\text{fb},\text{in}}}{2}$ (18)

This study calculates T_fb changing D and dx according to the above equations when inputting the climate data, i.e. I, u_a and T_a in Nagoya city in Japan in 2021 [12] . The heat transfer fluid used in this study is CH₄ and CO₂ mixture with the molar ratio of CH₄:CO₂ is 1.5:1. The molar ratio of CH₄:CO₂ is 1.5:1 which simulates the biogas. In this study, the following assumptions were made as follows:

1) The mass flow rate of the heat transfer fluid (m) is 0.05 kg/s.

2) The distance between absorber and glass tube is 1/10 D.

3) T_{fb, in} is 283 K.

4) T_s equals to T_a.

5) The thickness of absorber and glass tube is 0.005 m and 0.010 m, respectively.

6) R₂ and R₄ are ignored since they are very small compared to the other thermal resistances [10] .

7) T_ti equals to T_to.

8) T_gi equals to T_go, which is 373 K.

The values of physical properties used in this study are listed in Table 1.

Figure 3 illustrates the system consisting of solar collector, biogas dry reforming reactor and SOFC proposed by this study. The flow is explained in the caption of Figure 3.

To estimate the amount of H₂ produced from the biogas dry reforming reactor, this study follows the reaction scheme of biogas dry reforming as follows:

Table 1. The physical properties used in this study [10] [14] .

Figure 3. System consisting of solar collector, biogas dry reforming reactor and SOFC proposed by this study (Heat transfer fluid consisting of CH₄ and CO₂ flows into solar collector. After heated by solar collector, the heat transfer fluid flows into biogas fry reforming reactor. After the reaction by biogas dry reforming, H₂ is produced. The produced H₂ is supplied into SOFC as a fuel, resulting that the electricity is generated).

${\text{CH}}_{\text{4}}+{\text{CO}}_{\text{2}}\to {\text{2H}}_{\text{2}}+\text{2CO}$ (19)

In this study, the molar flow rate of CO₂ and CH₄ is 1.67 × 10⁻² mol/s and 2.51 × 10⁻² mol/s, respectively, which presents the molar ratio of CH₄:CO₂ of 1.5:1 and m of 0.05 kg/s. According to Equation (19) and these molar flow rates, the molar flow rate of produced H₂ can be calculated to be 3.34 × 10⁻² mol/s. According to the authors’ previous experimental studies changing the reaction temperature, which corresponds to T_fb in this study, from 673 K to 873 K [5] [6] , the performance of biogas dry reforming is the best at 873 K. Consequently, this study assumes H₂ can be produced by biogas dry reforming at T_fb over 873 K. The conversion ratio of H₂ is changed by 1%, 10% and 100%. According to the authors’ previous experimental studies [5] [6] , the highest conversion ratio of H₂ was approximately 10%. This study adopts the conversion ratio of H₂ of 10% following the experimental result and also adopts that of 1% and 100% as the assumed minimum and maximum performance case, respectively.

To estimate the power generated by SOFC, this study considers the lower heating value of H₂ (=10.79 MJ/m³N) and the power generation efficiency of commercial SOFC of 55% [15] . When the conversion ratio of H₂ is 100%, the power generated by SOFC can be calculated as follows:

$\begin{array}{l}\left(3.34\times {10}^{-2}\left[\text{mol}/\text{s}\right]\right)\times \left(\text{2}2.4\left[\text{L}/\text{mol}\right]\right)÷\left(1000\left[\text{L}/{\text{m}}^{\text{3}}\right]\right)\\ \times 0.55\times \left(10.79\left[\text{MJ}/{\text{m}}^{\text{3}}\cdot \text{N}\right]\right)=4.44\left[\text{kW}\right]\end{array}$ (20)

The amount of produced H₂ and the power generated by SOFC which are estimated by this study under several conditions are shown and discussed in the next section.

3. Results and Discussion

3.1. Calculation on Temperature of Heat Transfer Fluid

At first, the climate data, i.e. I, u_a and T_a in Nagoya city in Japan in 2021 [12] which are used for the calculation of T_fb are shown. In Tables 2-5, the data in January, April, July and October are listed as a representative data for Winter, Spring, Summer and Autumn, respectively. The monthly mean values are listed in these tables.

Figures 4-7 show T_fb with time changing D and dx among different months. In Figures 4-7, the data in January, April, July and October are listed as a representative data for Winter, Spring, Summer and Autumn, respectively. The monthly mean value is shown in these figures. In addition, Figures 8-11 show the T_fb ratio (a) based on dx = 1 m with time changing D and dx among different months. a is defined as follows:

$a=\frac{T_{\text{fb}}\left(dx=2\text{m}~5\text{m}\right)}{T_{\text{fb}}\left(dx=1\text{m}\right)}$ (21)

Table 2. Climate data of I, u_a and T_a in Nagoya city in January.

Table 3. Climate data of I, u_a and T_a in Nagoya city in April.

Table 4. Climate data of I, u_a and T_a in Nagoya city in July.

In Figures 8-11, the data in January, April, July and October are listed as a representative data for Winter, Spring, Summer and Autumn, respectively. Additionally, in Figures 8-11, the gray area indicates that there is no shining.

Table 5. Climate data of I, u_a and T_a in Nagoya city in October.

It is seen from Figures 4-11 that T_fb and a have a peak near the noon. This is followed by the trend of Ias shown in Tables 2-5. In addition, it is found from Figures 4-7 that T_fb for dx = 1 m keeps low value irrespective of D. According to Equation (19), it is known that dx has more impact compared to D from the view point of digit. It is seen from Figures 8-11 that a increases with increase in dx. Since the surface area for absorbing solar heat increases, the amount of absorbed heat increases. Moreover, it is known from Figures 4-11 that the differences of T_fb and a between dx = 2 m and dx = 3 m are larger than those between dx = 1 m and dx = 2 m. This is because Equation (15) has the term of dx².

Investigating the effect of the season on T_fb and a, the highest T_fb is obtained for April, which is 2400 K. The 2nd highest T_fb is obtained for July. Comparing four seasons, T_fb and a are higher in spring and summer, while they are lower in autumn and winter. These results follow the data of I. In addition, it is revealed from Figures 4-7 that T_fb is over 873 K for D = 1.0, 1.5 m and dx = 4, 5 m except for winter. However, it is known that T_fb is too high for D = 1.5 m and dx = 5 m, e.g. T_fb = 2199 K as shown in Figure 6. Since it is the excess heated temperature for the material of solar absorber, it can claim that dx = 4 m is the optimum length of solar absorber.

3.2. Estimation of the Amount of H₂ Produced from Biogas Dry Reforming Reactor

To estimate the amount of H₂ produced from the biogas dry reforming reactor, Table 6 lists the time when T_fb is over 873 K. The time when T_fb is over 873 K is

Figure 4. T_fb with time changing D in January ((a): D = 0.5 [m], (b): D = 1.0 [m], (c): D = 1.5 [m]).

Figure 5. T_fb with time changing D in April ((a): D = 0.5 [m], (b): D = 1.0 [m], (c): D = 1.5 [m]).

Figure 6. T_fb with time changing D in July ((a): D = 0.5 [m], (b): D = 1.0 [m], (c): D = 1.5 [m]).

Figure 7. T_fb with time changing D in October ((a): D = 0.5 [m], (b): D = 1.0 [m], (c): D = 1.5 [m]).

Figure 8. a with time changing D in January ((a): D = 0.5 [m], (b): D = 1.0 [m], (c): D = 1.5 [m]).

Figure 9. a with time changing D in April ((a): D = 0.5 [m], (b): D = 1.0 [m], (c): D = 1.5 [m]).

Figure 10. a with time changing D in July ((a): D = 0.5 [m], (b): D = 1.0 [m], (c): D = 1.5 [m]).

Figure 11. a with time changing D in October ((a): D = 0.5 [m], (b): D = 1.0 [m], (c): D = 1.5 [m]).

Table 6. The time when T_fb is over 873 K.

marked in this table. When T_fb is over 873 K, this study assumes that H₂ can be produced.

The amount of H₂ produced from the biogas dry reforming reactor, when assuming to use the heat obtained from the solar collector for the conduction of biogas dry reforming, is calculated changing the conversion ratio of H₂ by 1%, 10% and 100%. Table 7 lists the amount of H₂ produced from the biogas dry reforming reactor.

According to Table 7, it is known that the amount of H₂ produced from the biogas dry reforming reactor is the highest in August, which is 74.55 kg in the case of conversion ratio of H₂ = 100%. The time when T_fb is over 873 K is the longest in August as shown in Table 6, resulting that the amount of H₂ produced from the biogas dry reforming reactor is the largest in August. In addition, it is seen from Table 7 that the amount of H₂ produced from the biogas dry reforming reactor is larger in June and July, while it is lower in January and December. Consequently, it can be claimed that it is prefer to produce H₂ in summer.

3.3. Estimation of the Power Generated by SOFC

This study assumes that the power is generated by SOFC over T_fb = 873 K changing the conversion ratio of H₂ by 1%, 10% and 100%. Table 8 lists the power generated by SOFC.

According to Table 8, it is known that the power generated by SOFC is the highest in August, which is 1380 kWh in the case of the conversion ratio of H₂ = 100%. The time when T_fb is over 873 K is the longest in August as shown in Table 6, resulting that the amount of H₂ produced from the biogas dry reforming reactor is the largest in August. In addition, it is seen from Table 8 that the power generated by SOFC is higher in June and July, while it is lower in January

Table 7. The amount of H₂ produced from the biogas dry reforming reactor under several conditions.

Table 8. The power generated by SOFC under several conditions.

and December. If the power generated by SOFC is supplied for the electricity demand of a couple household [16] , 5.2 households can be supplied in August as the maximum, while 1.7 households can be supplied in January as the minimum. Consequently, it can be claimed that it is prefer to generate SOFC in summer, which follows the production of H₂ from the biogas dry reforming reactor.

According to the previous experimental studies by the authors [5] [6] , the conversion ratio of H₂ is approximately 10%. Since the scale of biogas dry reforming reactor is a laboratory level, it is necessary to scale up the biogas dry reforming reactor or promote the thermal storage to prolong the time over T_fb = 873 K. Otherwise, the development of catalyst used for biogas dry reforming is needed. They are the future work in the experimental study.

4. Conclusion

This study has investigated the impact of climate data on the performance of solar collectors with various designs. In addition, this study has estimated the amount of H₂ produced from the biogas dry reforming reactor powered by the solar collectors. Moreover, this study has also estimated the power generated by SOFC with the produced H₂. It is revealed that T_fb and a are higher in spring and summer, resulting from the data of I. It can be claimed that dx = 4 m is the optimum length of solar absorber. The amount of H₂ produced from the biogas dry reforming reactor and the monthly power that could be generated by SOFC is the highest in August, which is 74.55 kg and 1380 kW respectively in the case of conversion ratio of H₂ = 100%. It is revealed that 5.2 households can be supplied by the power generated by SOFC in August as the maximum. It can be claimed that it is prefer to produce H₂ as well as to generate SOFC in summer.

Conflicts of Interest

The authors declare no conflicts of interest regarding the publication of this paper.

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