Process analysis of solar steam reforming of methane for producing low-carbon hydrogen

Regarding the trend of hydrogen-powered fuel cell engine development, hydrogen fuel is undisputedly the next generation renewable and sustainable energy carrier. The steam reforming of methane (SRM) is a field-proven technology for efficient hydrogen production. However, producing low-carbon hydrogen is the most technical challenge related to available hydrogen production technologies. This paper investigated the process analysis of SRM for low-carbon hydrogen production using concentrated solar energy as a heat source. Analysis of the solar SRM is carried out considering the reformate gas and their influencing factors. The operating temperature of 200–1000 °C and the pressure of 1.02–30 bar were considered when the mass ratio of steam-to-methane in feed gas was varied from 1.0 to 4.0. It was found that the composition of reformate gas, hydrogen yield, methane and steam conversion rate, the thermal efficiency of reforming reactor, and volume flow of reformate gas are significantly affected by the operating parameters including temperature, pressure, and the mass ratio of feed gas. Carbon content in the yield of hydrogen produced can be limited by considering the water–gas shift reaction in the SRM process. Besides, the centralized tower type solar concentrating system is selected as the heat source of the SRM process. The effect of solar radiation on the operation performance of the solar SRM process was analyzed. Direct normal irradiation is a key factor affecting the operating performance of the solar SRM process.


Introduction
Developing clean fuel production technology is a promising way to meet the worldwide increasing energy demands with a great contribution to mitigating the raising effect of greenhouse gases and environmental pollution hazards. Apart from increasing environmental pollution effects, the prices of fossil fuels such as natural gas and oil are increasing unceasingly while its reserves are decreasing. According to the statistical review of world energy 2018, the reserves of natural gas (NG) and oil are limited to a range of 40-60 years while the reserves of coal can last for more than 150 years. 1 The increasing interest in the issues related to environmental pollution and economic growth have recently led to the development of next-generation sustainable and renewable clean fossil fuel production as energy carriers. Regarding a range of products that are compatible with our energy infrastructure today, hydrogen can be considered as the next-generation energy carrier since hydrogen is one of the important feedstock materials in chemical, petroleum, metallurgical, and electronic industries. In the transportation sector, hydrogen is commonly used in a fuel cell system based on electrochemical conversion and an internal combustion engine system via direct combustion. The transportation sector accounts for approximately 60% of the total air pollution. 2 For that reason, all vehicles with conventional internal combustion engine systems are needed to be replaced by the hydrogen and electric engine systems. Sufficient technologies have been developed for hydrogen production. However, steam reforming of methane process is considered as state-of-the-art technology for efficient production of hydrogen regarding the current scientic research and development (R&D). In the SRM process, pure methane and natural gas are not only used for producing hydrogen. Moreover, other types of gases with higher methane content (marsh gas, biogas, raw syngas from gasication, coal mine methane, and coal bed methane) are possible to be used for increasing the quality of syngas and producing hydrogen. Integrating solar thermal energy into conventional SRM technology is a promising approach for ecological hydrogen production based on fossil fuel in the near and midterm. In the long term, the solar-based full green and clean technologies, including thermochemical, 3 photochemical, 4 electrochemical 5 and water electrolysis will be dominated for producing hydrogen.
In recent years, intensive researches have been developed on different methods and technology under various conditions for methane reforming technology development. Pure hydrogen production technology based on the reforming process consists of converting methane into a hydrogen-rich gas, which is further upgraded and puried to hydrogen. Different types of reforming processes such as steam reforming (SRM), dry reforming (DRM), partial oxidation (POX), auto-thermal reforming (ATR), combined reforming (bi and tri), and plasma reforming have been investigated for efficient hydrogen production. [6][7][8] Regarding the steam reforming process, methane (natural gas) reacts with steam to produce hydrogen-rich gas using appropriate catalysts at a temperature ranging from 200-1000 C and operating pressure ranging from 1-30 bar. The steam reforming process is always associated with the watergas shi (WGS) reaction, which generates a high amount of CO 2 . Steam methane reforming and WGS reactions are the global reactions for leading to a signicant amount of hydrogen production. Considering steam methane reforming reaction, WGS reaction can reduce the concentration of CO in the amount of gaseous product. Aer the WGS reaction, the concentration of CO in the reformate gas is lower than 1.0%. Water-gas shi reaction is an exothermic type reaction. However, this might lead to excessive CO 2 generation in hydrogen-rich gas produced. 6,7 Steam methane reforming reaction can be typically described by the following equations.
Water-gas shi reaction (CO-shi reaction): Steam methane reforming reaction (SRM#1): Overall reaction (SRM#2): Since the past decades, the R&D on SRM technology aims to produce a high concentration hydrogen-rich gas which can be commonly used as an important feedstock in the chemical industry, energy, and transportation sector for various purposes. In the SRM process, the composition of the reformate gas, especially hydrogen yield depends on the reaction temperature and the operating pressure, process time, the quality of the feedstock, the catalyst activity, the mass ratio of steam-to-methane (H 2 O/CH 4 ) in the feed gas, and the type of reactor design. Finding appropriate candidate catalysts for the SRM process is a big technical challenge since the use of a potential catalyst can signicantly improve the performance of thermal chemical reactivity thereby resulting in an important amount of reformate gas production. In recent years, researchers have signicantly advanced the structure of the reactor and the catalyst materials. Among common-based catalyst materials including Ni, Fe, Co, and Al, other types of catalysts including Ru, Rh, Pd, Ir, and Pt have been investigated for higher hydrogen production and greater durability. [9][10][11] Fig. 1 describe the solar SRM process and different application elds for H 2 production. As indicated in Fig. 1, the steam reforming process is mainly a composite of feedstock pretreatment (desulfurization) process, reforming and shi reactor and purication process of reformate gas.
Hydrogen production via SRM is a high endothermic process which requires a high potential heat source for preheating feedstock, producing high potential steam, and controlling steam reforming process. However, developing medium and high-temperature scales concentrated solar energy system is another challenge that can overcome this issue by contributing to CO 2 emission reduction. Solar steam reforming methane is one of the energy effective technologies for producing low carbon hydrogen from methane. 12 The use of concentrated solar energy for a high-temperature heat source to the SRM process has the potential of avoiding up to 35-40% of the CO 2 emissions derived from the conventional SRM process based on fossil fuel. 13,14 Last decade, many studies have been developed on effective and reliable technology of the solar SRM under different methods. Wang et al. have performed thermodynamic analysis and numerical investigation of concentrated solarpowered membrane reactor concept for hydrogen production at lower and medium operating temperatures based on SRM. 15 Moreover, Giaconia et al. have investigated the solar steam reforming of natural gas for hydrogen production using molten salt heat carriers. 16 Besides, a dynamic simulation model is developed on a 400 kW solar reforming reactor to predict the temperature variation, heat transfer rates, outlet mass ow rates, and product composition during purging, thermal testing, experimental run, and cycling operation. 17 A numerical model combining Monte-Carlo ray-tracing method with a niteelement method is developed for the thermodynamic and kinetic analysis of solar methane reforming reactor using a reticulated porous ceramics structure of Ni/CeO 2 -ZrO 2 as a potential catalyst. Analysis of the system is performed under different reaction conditions with wide ranges of temperature, solar power input, and the ratio of steam to methane. 18 Moreover, Brown et al. 19 have developed the studies on the potential cost, performance, and economic characteristics of steam reforming of methane with parabolic dish concentrator for syngas production. The evaluation and performance analysis of membrane reactor with natural gas and steam for hydrogen production was investigated using concentrated solar energy as an energy source, molten salt thermal storage process, and Nibased catalyst. 20 The thermodynamic 21 and economic analysis 22 of solar steam reforming of NG integrated with a gas turbine power plant has been investigated. Regarding carbon capture and utilization technology, DRM process can signicantly contribute to CO 2 emission reduction. Performance analysis of solar thermochemical reactor was investigated based on the solar-driven methane reforming process using CO 2 . 23,24 The solar-thermal uid-wall aerosol ow reactor powered by high-ux concentrated solar energy was designed for the investigation of carbon black and hydrogen production based on the DRM process. 25 Intensive studies have been conducted on the numerical investigation of the thermochemical analysis 26 and thermochemical storage performance analysis 27 of DRM in a volumetric foam reactor powered by concentrated solar radiation.
In this section, some examples of process analysis of simulation models for SRM available in the literature are introduced. The simulation models based on equilibrium constant, and kinetic method using some process simulation soware have been performed for the thermodynamic analysis of the SRM process. The effect of different factors including temperature, pressure, and the mass ratio of steam-to-methane on the steam reforming of NG for hydrogen production was studied. Two equilibrium reactions, such as steam methane reforming reaction and WGS reaction for the conversion of steam and carbon monoxide to hydrogen and carbon dioxide were examined. 28 The steady-state simulation model was developed for hydrogen production via steam reforming of NG using Aspen Hysys soware. The optimization and sensitivity analysis of hydrogen production based on steam reforming process has been studied. 29 Moreover, the process simulation soware Aspen Plus was used to perform sensitivity analysis and optimization of hydrogen production based on SRM. 30 Furthermore, Gibbs free energy minimization methods via Aspen Hysys was developed to numerically investigate the thermodynamic analysis and optimization of dry and partial oxidation and auto-thermal (combined DR and POX) reforming processes at temperatures range of 200-1000 C and pressure range of 1-3 bar. 31 The effect of several parameters including the process temperature, operating pressure, catalyst weight loading, and mass ratio of feed gas on the process of steam reforming of NG has been studied to perform hydrogen production. The kinetic-based simulation model of steam methane reforming and WGS reaction for hydrogen production was performed in Aspen Plus. 32 The simulation model of DRM and SRM for syngas production using solar or hybrid heat sources was developed and investigated. 33 Solar cracking and solar SRM processes have been compared with the conventional SRM based on hydrogen production material and energy source. 34 The process analysis and simulation model of SRM, POX and ATR processes via the solar thermochemical hydrogen production was developed and studied by Aspen Plus soware. 35 As resulted from literature reviews, solar energy is possible to use for driving endothermic steam reforming reactions in which methane is reacted to form hydrogen-rich gas. In recent years, many studies have been conducted on the solar SRM process using different methods and technologies. The most of previous studies of solar SRM are investigated using numerical simulation of the CFD model and laboratory-scale experimental setup. However, the previous studies on the process analysis for solar SRM are not comprehensive. Therefore, it is practically important to study the process analysis of solar SRM. Moreover, the study of a large scale commercial solar SRM plant with a concentrated solar system is signicantly important.
In this study, the simulation study of solar SRM for hydrogen production is investigated using Pyrolysis and Gasication Process Library and Concentrating Solar Power Library in IPSEpro process simulation soware. This study aims to nd the thermodynamically favorable operating conditions on the solar SRM process. Therefore, the effect of operating parameters on the SRM process is considered. The effect of several operating parameters, including temperature, pressure, and mass ow ratio of the feed gas is analyzed. Moreover, the solar SRM plant for processing 5.0 tons of methane per hour is investigated based on the estimated optimum operating conditions. The centralized tower type solar concentrating system is selected as the heat source of solar SRM. The effect of solar radiation on the operation performance of solar SRM process is considered.

Model of steam reforming and water-gas shi reactor
The thermodynamic equilibrium in steam reforming methane reactor can be calculated in two methods. One is to minimize the Gibbs free energy, the other is to use equilibrium constants. According to the previous studies, the steam methane reforming and water-gas shi reactions were modeled based on the method of equilibrium constants. In this study, the simulation model of solar SRM for hydrogen production is investigated using IPSEpro process simulation soware based on the method of equilibrium constants. The simulation model of SRM reactor was performed using the equilibrium type reactor, thus there is no catalyst effect on the nal equilibrium composition of the reformate gas from the reactor. The simulation model of SRM is one-dimensional model, which is not considered any dimensions, reactor design, velocity, reaction rate, and catalyst effect. Pyrolysis and Gasication Process library (PGP library) of IPSEpro process simulation soware 36 is used to investigate the process analysis of steam reforming of methane for hydrogen production. The unit model of steam reformer is a model for various applications. The model equations are accessible for the steam reforming methane process. In this unit model, both the steam methane reforming and the water-gas shi reaction can take place simultaneously and allow us to calculate equilibrium as well as non-equilibrium gas compositions at the given temperature and ratio of H 2 O/CH 4 . The process ow diagram of SRM and component models used in the simulation model are basically described in Fig. 2.
CH 4 and H 2 O considered as feeding streams were rstly mixed by a mixer standard model before entering into the chemical reactor. The inlet and outlet streams are analyzed and monitored by the gas analyzer installed at the inlet and outlet of the gas reactor. The component model of the gas-phase chemical reactor has one feed stream and one drain stream. Once entered into the reactor, the feeding stream is transformed into a drain stream involving different chemical composition due to the effect of concentrating solar energy. Besides, the energy balance is formulated using the total thermodynamic enthalpies of all streams including their possible loadings. 37 The working uids used in the simulation model of SRM could be seen in Table 1.
IPSEpro soware is used to perform the numerical investigation of the SRM process. The simulation is carried out by considering different operating parameters including temperature, pressure, chemical composition, and mass ow rates of the inlet streams. Moreover, the heat input necessary to conduct steam reforming process including side reactions such as water-gas shi reaction and the conversion of hydrocarbons is considered in this study. Besides, important factors such as pressure drop, temperature decrease and heat loss of reactor that can signicantly affect the system efficiency have been investigated to improve the thermochemical reaction performance. The chemical compositions, operating parameters, and material and energy balances of all outlet material streams are calculated based on the mentioned above assumptions. Chemical equilibrium in a chemical reforming reactor could be calculated in the equilibrium constant. If the composition and mass ow rate of feed gas are specied, the composition and mass ow rate of drain gas are calculated by prescription of conversion rates or setting the concentrations in the drain. 36,37 The conversion rate of a component i in dynamic equilibrium can be calculated as follows.
X i ¼ 1 À m gas;out Â w i;gas;out m gas;in Â w i;gas;in ¼ m gas;in Â w i;gas;in À m gas;out Â w i;gas;out m gas;in Â w i;gas;in ;  where X i is a conversion rate of component i, m gas,out and m gas,in are the mass ow of outlet and inlet gases, while w i,gas,out and w i,gas,in are the mass fraction of outlet and inlet gases. The conversion rate is not calculated if w i,gas,in ¼ 0. The model attributes from 0 to X i as an ideal value. The conversion rate of hydrocarbon species C x H y (C 2 H 4 , C 2 H 6 , C 3 H 8 , and CH 4 ) and conversion rate of steam are typically formulated in the case of steam reforming and WGS reactions. The chemical equilibrium formulation is introduced in this section. 37 In the chemical reactor model, the minimization of Gibbs free enthalpy as the necessary condition for the progress of chemical reactions is not considered. In general, the chemical reaction can be calculated by the following formulae.
where A i are all species taking part in the reaction and v i are their stoichiometric coefficients. The equilibrium constant for the partial pressures is calculated by the following formulae.
In the case of ideal gases, the equilibrium constant is only a function of temperature, which is calculated by the reaction of Gibbs free enthalpy minimization.
where DG 0 R is the Gibbs free enthalpy at standard pressure, as calculated from the thermodynamic enthalpies and entropies of the participating species: The actual partial pressure product is related to the equilibrium constant and the logarithm of the ratio, which is expressed as a model parameter: If pd eq < 0, then the actual state of the drain gas is still on the side of the reactants, i.e. further reaction is thermodynamically in direction of the products possible. If pd eq > 0, the actual state of the drain gas is on the side of the products. In this case, the reaction can only proceed towards the reactants, i.e. from right to le. If pd eq ¼ 0 is prescribed, equilibrium must be fullled by the gas composition. In general, the equilibrium calculation requires p i > 0 for in all gas species. The operation performance of the SRM reactor is characterized by methane conversion rate, steam conversion rate, hydrogen yield, thermal efficiency of reactor and energetic upgrade factor. 38 Methane conversion rate, steam conversion rate and hydrogen yield can be dened as follows.
Methane conversion rate: Steam conversion rate: Fig. 3 Process flow diagram of a central receiver system for solar SRM process.
Hydrogen yield: where m in CH4 ; m out CH4 are the mass ow of methane at the inlet and outlet of the reformer; m in H2O ; m out H2O are the mass ow of steam at the inlet and outlet of the reformer; m H 2 is mass ow of hydrogen.
The thermal efficiency of the SRM reactor can be determined by the following equation.
where LHV H 2 , LHV CO and LHV CH 4 are the lower heating value of hydrogen, carbon monoxide and methane, respectively while m H 2 , m CO and m CH 4 are the mass ow rate of hydrogen, carbon monoxide and methane, respectively. The conversion efficiency of solar energy into chemical energy by the solar SMR is characterized by the energetic upgrade factor (U). 39 The energetic upgrade factor can be determined as the ratio of the LHV of reformate gas produced to that of the feedstock processed.
where m ref is the mass ow rate of reformate gas; LHV ref is the lower heating value of reformate gas.

Model of a solar eld with a central receiver system
SMR process is an endothermic process and requires a heat source with high potential. The solar SRM process is similar to that of conventional except for the energy source in which the solar SRM process is powered by high-temperature concentrated solar energy. According to the numerical and experimental studies, the dish and centralized tower type solar concentrating systems are convenient for solar SRM process. 40,41 Previously, a few studies on the thermochemical hydrogen production using a CSP plant with a central receiver system have been reported in the literature. 42,43 CSP library of IPSEpro soware 44 was used to perform the simulation model of the solar eld (SF) with a central receiver system of SRM reactor concerning the data reported in the literature. The process ow diagram of the solar eld with a central receiver system for solar SRM process and component models used in the simulation model are basically described in Fig. 3. The solar eld with a central receiver system consists of a receiver unit, solar tower, and heliostat. Heliostat eld has 14 subelds, which are located on three annular rings with their respective center given coordinates. Direct normal irradiation (DNI) is the most important parameter for performance assessment of a solar eld with a centralized tower, which is prescribed as the input value for any process model of concentrated solar energy utilization. 2.2.1 Heliostat. Heliostat solar eld consists of a number of individual heliostats, which surround the solar tower and reect sunlight to the central receiver system set on the top of a solar tower. Solar thermal power reected towards a central receiver system (q re ) can be determined by the following equation.
where q inc is solar power incident on the total area of heliostat mirror; h hel is the heliostat efficiency, which is composed of reectivity and spilling. Solar power incident on the total area of a mirror (q inc ) can be determined by the following equation.
where DII is direct incident irradiance; A hel is aperture area of the heliostat. Direct incident irradiance (DII) can be determined by the following equation.
where DNI is direct normal irradiance; q is incident angle. 2.2.2 Central receiver system. Central receiver at the top of the solar tower is used to transfer the sunlight reected by heliostats to the HTF. Received summary of reected solar power from heliostats (q rec ) can be calculated as: This journal is © The Royal Society of Chemistry 2020 RSC Adv., 2020, 10, 12582-12597 | 12587 q rec ¼ q refl À q rec.loss ; (18) where q rec.loss is the solar thermal power loss in the receiver, which is composed of the power loss reected from receiver, radiation and convection losses of the receiver. Solar thermal power loss in the receiver (heat loss from receiver aperture area to ambient air) can be calculated as: q rec.loss ¼ q ref.loss + q rad.loss + q conv.loss ; where q re.loss is the power loss reected from the receiver; q rad.loss is the radiation loss of receiver; q con.loss is the convection losses of the receiver. q re.loss , q rad.loss and q con.loss can be obtained by ref. 45.
where d is concerning solar absorptance of the tube panels, (0.95); 3 is the hemispherical emittance, (0.88); s 0 is the Stefan-Boltzmann constant; A r is the lateral surface of the tube; f mix,i is the mixed convection coefficient; T wall,i is the wall temperature; T amb is the ambient air temperature. Thermal efficiency of receiver system can be calculated as: Sunlight reected by mirrors of heliostat is focused onto the central receiver system and the temperature of HTF increases by transferring heat (absorbing energy) from the receiver. Transferred heat (q trans ) to HTF can be calculated as: where m HTF is the mass ow rate of heat transfer uid; h out HTF and h in HTF are specic enthalpy of HTF at outlet and inlet of receiver. The receiver model is validated with experimental data from the Solar Two power plant. The actual efficiency of the receiver system is around 85.2%, which agrees well with the experimental data of Solar Two demonstrated as 86-88%. 46 Moreover, other studies reported the efficiency of the receiver as 83-90% by Jianfeng et al. 47 and 78-88% by Lata et al. 48 Therefore, the precision and simulation result of the receiver system could satisfy the project modeling requirements.
The simplied owchart for calculating the simulation model of solar SRM using IPSEpro soware can be seen in Fig. 4. The simulation models contain a mass balance, energy balances and specic equations describing chemical conversion rates, splitting conditions, basic functional and empiric correlations. 49 However, it is rst necessary to build the component models of the SRM plant for analyzing the process ow diagram of SRM. In general, the process modeling is based on the component models provided by IPSEpro which describes the basic physical and chemical processes, builds the total SRM plant according to the sequence of components including the component models, subsystems, and complete systems. 50 2.2.3 Model validation. The accuracy of IPSEpro models and the validation of our simulation results were carried out and discussed under the same simulation conditions used by Wang et al. 51 Wang et al. have investigated the effect of process temperature on the methane conversion rate under the operation conditions of 200-900 C of process temperature, 1.02 bar of operating pressure, and 1.0-4.0 of mass ow ratio of feed gas. Fig. 5 clearly describes the comparison for the effect of process temperature on the methane conversion rate under various ratios of feed gas between the results calculated in Wang's model and in this paper. As can be seen from Fig. 5, the calculated results agreed well with those reported in Wang's model. Increasing the mass ratio of feed gas leads to an increase in the methane conversion rate at the given reaction temperature. Moreover, the methane conversion rate is increased by growing process temperature under the different mass ratios of feed gas. The simulation results of IPSEpro model from this study are accurate compared to the previous study. Moreover, the simulation results have similar behavior and pattern under the same operating conditions. According to the results, IPSEpro model can be considered for the simulation model of SRM since it satises the project modeling requirements.

Material balance analysis of feed and reformate gas
According to the literature, the process modeling of the SRM can be simulated by different soware with diverse mathematical models. Steady-state simulation of H 2 production from SRM process is performed using IPSEpro process simulation soware. Important factors including mass ow ratio of H 2 O/ CH 4 in the feed gas, reaction temperature, and operating pressure of the feed gas that can inuence the compositions of reformate gas in the reformer are considered during the numerical analysis. A pressure range of 1.02-30 bar, temperature range of 200-1000 C, and mass ratio of steam-to-methane (H 2 O/CH 4 ) of 1.0-4.0 are the limited conditions calculating the composition of reformate gas (CH 4 , CO, CO 2 , H 2 and H 2 O), methane conversion rate, steam conversion rate, volume ow of reformate gas, and volume ow of hydrogen gas. The material balance of feed gas into the reforming reactor can be seen in Table 2. In this study, the feeding gas is essentially a composite of CH 4 and H 2 O. The numerical calculation is carried out by varying the ratio of H 2 O/CH 4 from 1.0 to 4.0 while maintaining constant the process temperature at 800 C and the pressure at 1.02 bar.
Moreover, the input value of the concentration of CH 4 and H 2 O is clearly described in Table 3 by considering different mass ratios of H 2 O/CH 4 . The volume ow rate of reformate gas at normal condition changes with the variation in the operating conditions. Increasing H 2 O/CH 4 ratio from the feed gas and the reacting medium resulted in an increase in the volume ow rate of reformate gas at normal conditions. Thus, the concentration of H 2 O is responsible for the density of reformate gas in the reactor. As for H 2 yield, both mass ow rate and volume ow rate are affected by the change in the operating conditions at normal conditions. It was found that the increase in the ratio of H 2 O/CH 4 leads to a slight increase in hydrogen production at the given reaction temperature. By considering the operating  the ratio of H 2 O/CH 4 ¼ 4.5. 34 As can be seen in Table 3, the mass ratio of feed gas and the WGS reaction is slightly inuenced by hydrogen production. H 2 O and CH 4 are the most abundant source of H 2 . Besides, the WGS reaction results in higher H 2 production at certain operating conditions. Combining these processes could evidently result in higher H 2 production with a slightly increasing mass ratio of H 2 O/CH 4 . Therefore, the ratio of H 2 O/CH 4 , operating temperature are important key parameters that should be carefully investigated to optimize the process of hydrogen production via SRM.

Parameters study
3.2.1 Effect of mass ow ratio on feed gas. The effect of the mass ow ratio of feed gas (steam-to-methane) on the SRM process was investigated under the temperature of 800 C and 1.02 bar of operating pressure. Composition of reformate gas is considered in wet and dry mass. Aer the reactor, the composition of reformate gas contains water vapor, which is called wet mass. The mass of reformate gas aer the purication process is called the dry mass. The quality of the reformate gas is signicantly improved aer the purication process. Fig. 6(a) indicates the effect of the mass ratio of H 2 O/CH 4 on the composition of reformate gas from the reformer in wet mass. By considering the wet mass, the concentration of CH 4 , CO, and H 2 in the reformate gas decrease while the concentration of CO 2 and H 2 O increase as the ratio of H 2 O/CH 4 increases. Analysis of the composition of reformate gas results in the decrease in CH 4 concentration from 4.523-0.023%, CO from 23.126-9.028%, H 2 from 70.897-51.866%, and the increase in CO 2 from 0.379-6.196% and H 2 O from 1.075-32.888% when the ratios of H 2 O/ CH 4 was increased from 1.0-4.0. Besides, it was observed that the decrease in the concentration of CH 4 form 4.572-0.034%, CO from 23.377-13.452%, and the increase in CO 2 and H 2 concentration from 0.383-9.232% and 71.667-77.283%, respectively when the ratios of H 2 O/CH 4 was increased from 1.0-4.0 in dry mass. Thus, CH 4 and CO concentrations in the reformate gas decrease while CO 2 and H 2 concentrations increase as the ratio of H 2 O/CH 4 increases by considering dry mass. The increase in the concentration of CO 2 along with that of H 2 could be attributed to the reverse water-gas shi reaction leading to signicant H 2 O and CO conversion into CO 2 and H 2 .
Regarding the effect of the ratio of H 2 O/CH 4 on the conversion rate of methane and steam as depicted in Fig. 6(b), methane conversion rate increases compared to steam conversion rate which decreases when the ratio of H 2 O/CH 4 was increased at a given temperature and pressure. The increase in the methane conversion rate from 83.86% up to 99.85% and the decrease in steam conversion rate from 95.69% to 39.44% is obtained at 800 C and 1.02 bar of operating temperature and pressure, respectively. Consequently, higher volume ows of reformate gas and hydrogen was obtained at higher ratios of steam-to-methane as shown in Fig. 6(c). By considering the operating temperature of 800 C and pressure of 1.02 bar, the volume ow of reformate gas and that of hydrogen increase to 4.98-9.16 N m 3 h À1 and 3.53-4.75 N m 3 h À1 , respectively. Thus, reformate gas, as well as hydrogen gas were thermodynamically favored by the higher ratio of H 2 O/CH 4 . It could be observed that the mass ratio of feed gas has a big effect on steam reforming and WGS process. Besides, the effect of the ratio of H 2 O/CH 4 on the thermal efficiency of reforming reactor was investigated under the operating conditions of 800 C of the reaction temperature and at 1.02 bar of pressure as shown in Fig. 6(d). It was found that the thermal efficiency of the reforming reactor increases from 55.79% to 85.64% as the ratio of H 2 O/CH 4 increases as well. It can be reported that the thermal efficiency of the reforming reactor is thermodynamically favored at a higher ratio of steam-to-methane.
3.2.2 Effect of process temperature. The effect of temperature on the SRM process was investigated for the pressure of 1.02 bar and temperature ranging from 200 C to 1000 C under the ratio of steam-to-methane of 3.0. In theoretical, two moles of steam can fully transform one mole of methane. However, the SMR process is usually carried out under an excess ratio of H 2 O/ CH 4 (more than 3.0) in practice. Considering the reformer in wet mass as indicated in Fig. 7(a), the concentration of H 2 and CO 2 , in the reformate gas increases while the contents of CH 4 , H 2 O and CO decrease with the increase in the process temperature at H 2 O/CH 4 ¼ 3.0. However, when process temperature increases, H 2 content rst increases, reaching a maximum value, and then slowly decreases. Higher conversion of CH 4  Thus, the process temperature is an important key factor that signicantly inuences the conversion rates of methane and steam. As shown in Fig. 7(b), methane and steam conversion rates could be thermodynamically favored between 200-1000 C since higher conversion rates of methane and steam reported to 1.32-100.0% and 0.99-45.47%, respectively were obtained at H 2 O/CH 4 ¼ 3.0. Moreover, the volume ow of reformate gas and hydrogen gas reported to 5.17-7.92 N m 3 h À1 and 0.074-4.492 N m 3 h À1 , respectively was observed in Fig. 7(c) when the process temperature was increased. Therefore, increasing the process temperature results in the increase in the thermal efficiency of the reforming reactor from 1.58% up to 80.68% as depicted in Fig. 7(d). Operating temperature ranging in 700-800 C could thermodynamically favor the SMR process at H 2 O/CH 4 ¼ 3.0. Results show that the process temperature has a big effect on steam reforming and WGS process. Fig. 7(e) shows the hydrogen content in reformate gas under the various mass ratio of feed gas and process temperature. The hydrogen content can increase by reducing the mass ratio of feed gas. It's depending on the mass ow of reformate gas. Moreover, the hydrogen content is increased by increasing process temperature under the different ratios of feed gas. Besides, it is pertinent to mention that the volume ow of hydrogen is increased when the mass ratio of the feed gas is increased.

3.2.3
Effect of process pressure. The effect of process pressure on the SRM process was investigated for the temperatures of 800 C and operating pressure ranging from 1.02 bar to 30 bar under a mass ow ratio of steam-to-methane of 3.0. By considering the ratio of H 2 O/CH 4 ¼ 3.0, the composition of the reformate gas includes 0.059-7.921% of CH 4 , 12.148-6.580% of CO, 5.446-5.925% of CO 2 , 58.228-43.437% of H 2 , and 24.119-36.137% of water vapor at wet mass as shown in Fig. 8(a). However, the change in the composition of the reformate gases of 0.078-12.403% of CH 4 , 16.009-10.303% of CO, 7.177-9.278% of CO 2 , and 76.736-68.016% of H 2 was obtained at the same ratio of H 2 O/CH 4 ¼ 3.0 at dry mass. Regarding the composition of the reformate gases, increasing the process pressure signicantly affects the global yield of reformate gases. The concentrations of CH 4 , CO 2 and H 2 O increase while those of CO and H 2 decrease in reformate gases when the process pressure was increased by considering the wet mass at the ratio of H 2 O/CH 4 ¼ 3.0. Besides, the conversion rate of methane and steam decrease as the process pressure increases as shown in Fig. 8(b). At H 2 O/CH 4 ¼ 3.0, the conversion rates of methane and steam decreased from 99.67-61.22% and 48.86-33.77%, respectively when the operating pressure was increased from 1.02-30 bar. Thus, CH 4 and steam conversion rates are thermodynamically favored at low operating pressure. At the same time, as can be seen in Fig. 8(c), the volume ow of reformate gas and hydrogen gas gradually decrease from 7.91-6.84 N m 3 h À1 and 4.61-2.97 N m 3 h À1 , respectively due to the decrease in the thermal efficiency of reforming reactor associated with the increase in the process pressure. Moreover, the thermal efficiency of the reforming reactor could slightly decrease from 80.13-56.54% with the increase in the operating pressure as depicted in Fig. 8(d). Pressure has a low effect on steam reforming and WGS process. However, the process pressure has operational advantages.

Assessment of solar heat input for steam reforming methane process
The assessment of solar heat input on the SRM process was investigated via a concentrated solar power library (CSP lib) of IPSEpro soware. The numerical calculation is carried out by varying the temperature from 600 C to 900 C while maintaining constant the ratio of H 2 O/CH 4 at 4.0 and the pressure at 1.02 bar. The combined steam methane reforming and watergas shi stoichiometric reaction for a 4 : 1 steam to methane ratio at 800 C is given by the mass fraction (kg kg À1 ) in eqn (25).  The input values of material balance of feed gas, estimated values of material balance of reformate gas, the composition of reformate gas, and operation performance of reforming reactor are clearly described in Table 4 at 800 C. The SRM process is carried out at 30.1 MW of heat input for processing 5.0 tons of methane and 20.0 tons of steam under 800 C of temperature and 1.02 bar of pressure. The results show that 2.14 tons of hydrogen can be produced from 5.0 tons of methane using 30.1 MW of solar power can be achieved. Fig. 9 shows the inuence of temperature on the solar heat input of the SRM process. The process temperature is directly dependent on the solar heat input of the SRM process. Increasing the process temperature until to desired thermochemical conversion temperature leading to good operating performance can be obtained by increasing the solar heat input of the SRM process. However, the process temperature should be limited to 900 C to ensure the long-term durability and stability of catalysts. Noted that in practice, most cases of steam reforming reactors operate around 800 C.
In this study, the climate data of Dalanzadgad city in Omnogobi province (43.35 S, 104.41 E) was offered by NREL's standard system advisor model library (SAM). To create the results closer to real operation conditions, the simulation model of the solar SRM system is performed based on climate data in a typical year of Dalanzadgad city given in Table 5. 50 Variation of annual DNI in a typical year of Dalanzadgad city is shown in Fig. 10. The annual DNI distribution of Dalanzadgad city was around 2187 kW h m 2 . The design-point value of DNI is taken as 0.60 kW m À2 based on climate data of Dalanzadgad city in 2017. The main parameters and operation performance of the solar eld were estimated based on this design-point value of DNI.  Fig. 9 Effect of temperature on the solar heat input of the SRM process. This journal is © The Royal Society of Chemistry 2020 RSC Adv., 2020, 10, 12582-12597 | 12593 Fig. 11 describes the effect of DNI on the aperture area of the solar eld. The aperture area of the solar eld was calculated considering the required solar heat (30.1 MW) of the SRM process. DNI is an important key factor that signicantly inuences the aperture area of the solar eld. The DNI condition was varied between 0.40 to 1.00 kW m À2 . As shown in Fig. 11, the aperture area of the solar eld decreases when DNI increases.
The main parameters and operating performance of the solar eld with a central receiver system are summarized in Table 6. Numerical simulation of the solar eld was performed in the off-design regime (variation of DNI). As can be seen in Table 6, the DNI is a key parameter affecting the operation performance of the solar eld with a central receiver system. Fig. 12 shows the operation performance of the solar eld in the off-design regime. The operation performance of the solar eld has been calculated considering the design-point aperture area (A SF ¼ 93 000 m 2 ), and the DNI changes from 0.20 to 1.00 kW m À2 . Operation performance of the solar eld mainly depends on DNI value. The solar eld has good performance under higher DNI condition, but the optical and thermal losses are increased. Fig. 13 describes the effect of DNI on the thermal efficiency of the receiver and solar eld under the variation of DNI. The thermal efficiency of the receiver and solar eld have been obtained considering the design-point aperture area, and the DNI changes from 0.20 to 1.00 kW m À2 . The thermal efficiency of the receiver and solar eld are not linear correlation on the DNI. The thermal efficiency of the receiver and solar eld slightly decrease by 9.8% and 6.7% respectively from 1.00 to 0.50 kW m À2 . Besides, the thermal efficiency of the receiver and solar eld were drastically decreased between 0.40 to 0.20 kW m À2 .   . 12 Effect of DNI on the operation performance of solar field: q DNI -DNI on effective aperture area; q DII -DII hitting the mirror on heliostat; q rec -reflected solar radiation from heliostat; q trans -transferred heat to SRM process; q loss -heat loss of receiver. Fig. 13 Effect of DNI on the thermal efficiency of the receiver system and solar field.