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Integrated biomass gasification combined cycles can be advantageous for providing multiple products simultaneously. A new electricity and freshwater generation system is proposed based on the integrated gasification and gas turbine cycle as the main system, and a steam Rankine cycle and multi-effect desalination system as the waste heat recovery un...
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... schematic of the proposed integrated gasification combined cycle for electricity and freshwater production is provided in Figure 1. The new hybrid system is based on a downdraft gasification system, a gas turbine cycle, steam Rankine cycle, and a multi-effect desalination system. ...
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... parallel-cross heat exchanger arrangement, because it performs better in terms of energy consumption and gain output ratio (GOR) [25], was used in this study. Figure 1 shows a magnified schematic of a MED unit with six effects. ...
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... the effect of the increasing of the combustion chamber temperature on the sum unit cost of the product exhibits a different trend, with SUCP decreasing to a minimum value and then increasing. Figure 10 demonstrates the variation of net output power, exergy efficiency, freshwater production capacity, and SUCP with the air preheater efficiency. It is observed that the freshwater and power production capacity increase as air preheater efficiency rises. ...
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... variations in water production rate and power generation capacity lead to an increase in exergy efficiency, and ultimately, sum unit cost of the product as air preheater efficiency rises. Figure 11 shows the variation of net output power, exergy efficiency, freshwater production rate, and SUCP as superheating temperature difference (í µí»¥í µí± ) varies for the proposed system. The net power generation rate increases as the superheating temperature difference raises since the inlet temperature to the steam turbine increases, leading to a higher power production rate by the steam turbine. ...
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... Effect of Feedwater Temperature (í µí± ) on Water Production Capacity Figure 12 illustrates the variation of freshwater production rate with feedwater temperature (í µí± ) for the proposed system. The relation parallels that observed for the water production rate as feedwater temperature rises. ...
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... effect of gasification temperature for selected biomass was studied to observe the gas yield potential at different operating temperatures. The produced components molar ratio in the temperature range 800 K to 1100 K is presented in Figure 13. It is observed from the plot that hydrogen yield percentage increases with an increase in temperature up to 1000 K. ...
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... is observed that a lower payback period and higher total NPV are attained as the electricity price increases. Figure 14 shows the variation of NPV for í µí± = 2 $/GJ, í µí± = 1.8 $/m , and various electricity selling prices. It can be seen that, for an electricity selling price of 0.05 $/kWh and lower, the total value of NPV at the end of the plant life is negative, so such a plant is not feasible from an economic viewpoint. ...
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... based on this figure, the payback period ( í µí±í µí± ) drops from 6.75 years for í µí± = 0.07 $/kWh to 4.13 years for í µí± = 0.09 $/kWh. The effect of varying fuel purchase price is shown in Figure 15, for í µí± = 0.07 $/kWh and í µí± = 1.8 $/m . It is seen that, for a fuel price higher than 5 $/GJ, the total NPV is negative at the end of the plant lifetime. ...
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... schematic of the proposed integrated gasification combined cycle for electricity and freshwater production is provided in Figure 1. The new hybrid system is based on a downdraft gasification system, a gas turbine cycle, steam Rankine cycle, and a multi-effect desalination system. ...
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... parallel-cross heat exchanger arrangement, because it performs better in terms of energy consumption and gain output ratio (GOR) [25], was used in this study. Figure 1 shows a magnified schematic of a MED unit with six effects. ...
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... the effect of the increasing of the combustion chamber temperature on the sum unit cost of the product exhibits a different trend, with SUCP decreasing to a minimum value and then increasing. Figure 10 demonstrates the variation of net output power, exergy efficiency, freshwater production capacity, and SUCP with the air preheater efficiency. It is observed that the freshwater and power production capacity increase as air preheater efficiency rises. ...
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... variations in water production rate and power generation capacity lead to an increase in exergy efficiency, and ultimately, sum unit cost of the product as air preheater efficiency rises. Figure 11 shows the variation of net output power, exergy efficiency, freshwater production rate, and SUCP as superheating temperature difference (í µí»¥í µí± ) varies for the proposed system. The net power generation rate increases as the superheating temperature difference raises since the inlet temperature to the steam turbine increases, leading to a higher power production rate by the steam turbine. ...
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... Effect of Feedwater Temperature (í µí± ) on Water Production Capacity Figure 12 illustrates the variation of freshwater production rate with feedwater temperature (í µí± ) for the proposed system. The relation parallels that observed for the water production rate as feedwater temperature rises. ...
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... effect of gasification temperature for selected biomass was studied to observe the gas yield potential at different operating temperatures. The produced components molar ratio in the temperature range 800 K to 1100 K is presented in Figure 13. It is observed from the plot that hydrogen yield percentage increases with an increase in temperature up to 1000 K. ...
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... is observed that a lower payback period and higher total NPV are attained as the electricity price increases. Figure 14 shows the variation of NPV for í µí± = 2 $/GJ, í µí± = 1.8 $/m , and various electricity selling prices. It can be seen that, for an electricity selling price of 0.05 $/kWh and lower, the total value of NPV at the end of the plant life is negative, so such a plant is not feasible from an economic viewpoint. ...
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... based on this figure, the payback period ( í µí±í µí± ) drops from 6.75 years for í µí± = 0.07 $/kWh to 4.13 years for í µí± = 0.09 $/kWh. The effect of varying fuel purchase price is shown in Figure 15, for í µí± = 0.07 $/kWh and í µí± = 1.8 $/m . It is seen that, for a fuel price higher than 5 $/GJ, the total NPV is negative at the end of the plant lifetime. ...
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Citations
... The marine engine's thermal efficiency typically ranges from 30% to 50% [6]. Hence, there exists significant potential in the adoption of waste heat recovery systems (WHRS) for the ship's engine [7], as they enable the recovery of waste heat from ships, thereby enhancing energy efficiency [8] and reducing fuel consumption [9] of ships. ...
... Biomass, as a type of low-emission renewable energy resource, is an emerging alternative to fossil fuels and can play a significant role in energy systems. [1][2][3][4] A solid oxide fuel cell (SOFC), as a modern and efficient energy conversion technology with respect to the conventional power generation systems, can utilize the syngas produced from the biomass gasification process as the input fuel for power generation. The integration of the biomass gasification-based SOFC with a microgas turbine (mGT) makes it one of the most promising candidates for future energy conversion devices. ...
In this paper, a small scale biomass gasification based solid oxide fuel cell/gas turbine (SOFC/GT) combined heat and power (CHP) plant is investigated by means of both conventional and advanced exergy and exergoeconomic analysis. A one-dimensional model of an internal reforming planner SOFC is employed to account for the temperature gradient within the fuel cell solid structure, which is maintained at the maximum allowable temperature gradient (150 K) under different operating conditions. Two main parameters of the gasification process, namely, air-to-steam ratio and modified equivalence ratio, are investigated, and the key parameters of the cycle exergy and exergoeconomic study are analyzed. Moreover, a multi-objective optimization procedure is applied to determine the unavoidable gasifier conditions required for the advanced exergy analysis of the system. The results of the conventional exergy and exergoeconomic analysis reveal that the highest rate of exergy destruction occurs in the gasifier, followed by the afterburner (AB) with 41.87% and 21.98%, respectively. Also, the lowest exergoeconomic factor is related to AB by 5.34%, followed by heat recovery steam generator (HRSG), gasifier, air compressor, and SOFC, which implies that the priority is to improve these components to reduce the exergy destruction cost rate. The results obtained from the advanced exergy and exergoeconomic analysis indicate that the most of the total exergy destruction rate is unavoidably in the CHP plant. The AB shows the least improvement potential in terms of reduction of the exergy destruction by almost 2% avoidable part, followed by Heat Exchanger 3 (H.X.3), gasifier, and SOFC duo to their lowest avoidable exergy destruction parts of almost 5%, 10% and 13%f respectively. Furthermore, the unavoidable part of the investment cost rate for all the components of the cogeneration plant is larger than the avoidable part, which means that it is difficult to reduce the investment cost rate of the system components. Meanwhile, the endogenous/exogenous analysis shows that the exergy destruction is completely endogenous for all components of the integrated plant, except for HRSG, GT, and HX1. Compressors and turbines have the highest potential to reduce endogenous exergy destruction. This is due to their higher avoidable endogenous exergy destruction. Reducing the investment cost rate seems difficult, as the main investment cost rate was found to be an unavoidable endogenous part for all system components. Finally, some results obtained from the advanced analysis approach are the opposite to those of the conventional method. This fact emphasizes that the results of conventional exergy analysis alone are insufficient and unreliable. For example, based on the advanced analysis perspective, the gas turbine and H.X.2 by 8.9% and 8.46% modified exergoeconomic factor, respectively, should be considered for reducing investment cost rate, while the conventional method gives opposite results.
... Furthermore, the gasifier system can be tested for other promising applications such as powder coating, foundry sand drying and lowcapacity boiler systems. The biomass gasification technique has recently been employed for water desalination [50]. ...
Gasification of waste biomass can offer a cleaner and renewable alternative to wood and fossil fuel-based cooking systems. However, field evaluations of biomass gasifiers for institutional cooking are rarely reported in the scientific literature. This study was aimed to develop a fuel-efficient gasifier system for institutional cooking in the Indian context. We conducted field experiments in both rural and urban settings using collaborative approaches. The results demonstrated significant improvements in gasifier-based cooking including up to a 25% reduction in cooking time, about 28% lower fuel consumption, and 82% less fine particulate matter emissions, within the permissible limits, when compared to cooking via traditional chulha (clay stove). Through collaborative design with users, the gasifier system underwent further modifications to achieve a substantial reduction in cooking time (around 25–30%) across various testing scenarios. Furthermore, the gasifier system was successfully demonstrated to supplement a liquefied petroleum gas (LPG)-based cooking system, and the latter showed around 25% faster cooking performance and a 12.5% lower energy input. Practical problems encountered during biomass gasifier field trials were documented and analyzed, along with a project SWOT (Strengths, Weaknesses, Opportunities, and Threats) analysis. The results of gasifier field trials imply significant potential when compared to the traditional cooking in a rural setting. Overall, the proposed gasifier system could serve as a sustainable technology alternative for bioenergy applications in the developing world.
... With the integration of the first two equations, Equation (6) is obtained [31]: ...
... ̇ is total cost of system product, ̇ is the total cost of production, ̇ is the fixed-cost associated with fixed investment and ̇ represent the operation and maintenance cost. In order to evaluate the unit cost of input and output exergy flows (̇ ‚̇), the power (̇) and heat transfer (̇), the following equations are utilized [24]: ...
... The total cost of each unit can be evaluated as [24]: ...
... which is the purchasing fixed cost of system components, is the annual runtime of each component and assumed 7000 hours, is the maintenance factor and is 1.06 and is the capital recovery factor, which can be calculated from following equation [24]: ...
Highlights ➢ A flash-binary geothermal-based system is proposed for power generation. ➢ Zeotropic mixtures as the working fluid are used for performance improvement. ➢ Thermodynamic, exergoeconomic, and optimization assessments were performed. ➢ The system led to generating 3841 kW net power with 61.09% exergetic efficiency. ➢ The optimum payback and exergetic efficiency were obtained to be 3.26 years and 62.15%, respectively. Article Info Abstract In this paper, a geothermal system is combined with an organic Rankine cycle to generate power. The zeotropic mixture is utilized to improve the organic Rankine cycle performance. The mass, energy, exergy, and exergoeconomic analysis is applied to evaluate the proposed system performance, in which the system led generated 3841 kW net power with 61.09% exergetic efficiency and 3.55 years of payback period. Then, a parametric study is performed to obtain the effect of vapor generator temperature and zeotropic mixture's mass fraction on the proposed system's main performance criteria. Based on the parametric study results, the mass fraction variation influences the net power generation, energy and exergetic efficiencies, and the payback period is higher than the evaporation temperature in the vapor generator unit while, the exergy destruction is influenced by the evaporation temperature higher than the zeotropic mixture mass fraction. Also, the net present value is estimated for three different geofluid and electricity sale prices. Increasing the electricity price about 22% with the same geofluid price decreases the payback period by about 23% and improves the system profit by about 54.7%. Finally, applying a multi-objective optimization refers to obtaining the payback and exergetic efficiency by about 3.26 years and 62.15%, respectively.
... As the most dominant contributor to current energy sources, fossil fuels, although cheap, versatile, and easy to store and transport, have resulted in climate change, environmental pollution, and even global warming as a result of their overuse [1][2][3]. Terefore, clean, green, and efcient renewable energy sources are urgently needed to curb the use of fossil energy. Te renewable nature of solar, wind, geothermal, and biomass energy is self-explanatory. ...
Establishing an accurate equivalent model is a critical foundation to describe the energy conversion characteristics of a photovoltaic system, which can support the research of fault analysis, output power prediction, and performance analysis of the photovoltaic system. However, the widely used equivalent models are highly nonlinear and have many unknown parameters, making it difficult to identify these parameters accurately. Our previous work found that the gaining-sharing knowledge-based algorithm (GSK) shows promising performance in solving this problem. But its efficacy is not enough to achieve accurate parameters within a relatively limited computing resource. In this context, a dual-population GSK algorithm (DPGSK), which introduces a dual-population evolution strategy for more excellent searchability, is proposed to address this issue. In each iteration, the population splits equally and randomly into two subpopulations, one of which performs the junior gaining-sharing phase while the other performs the senior gaining-sharing phase. Then two updated subpopulations merge to form a new population. This allows for a grand reconciliation of convergence speed and population diversity, giving DPGSK powerful optimization performance. Afterward, DPGSK is applied to five photovoltaic models and validated for performance against other advanced metaheuristics. Besides, the impact of different components on DPGSK is also investigated. Results and comparisons show that either component is indispensable to DPGSK, and DPGSK strengthens the convergence and achieves accurate and reliable results, demonstrating its superiority over other algorithms in solving this studied problem.
... They showed that by feeding 14 kg/s steam flow to the MED unit, the best result by considering the economic and exergy approaches was achievable and provided 12294 m 3 /day of freshwater. Hamrang et al. [31,32] presented a gas turbine-based system to produce electricity and freshwater. Freshwater in this system is provided by the MED unit. ...
Problems of sustainable development and environmental protection pose a challenge to humanity unprecedented in scope and complexity. Whether and how the problems are resolved have significant implications for human and ecological well-being. Accordingly, this work proposes an electricity and freshwater cogeneration system using solar energy and natural gas dual sources. The proposed system is a combination of a heliostat field with a gas turbine cycle as the top systems and thermal vapor compression-multi effect desalination, steam Rankine cycle, organic Rankine cycle, and thermoelectric generator as subsystems. For performance analysis, energy, exergy, exergoeconomic, economic, and environmental analyses were performed. To optimize the system, a coupled model of the support vector regression, multi-objective grey wolf optimization algorithm, multi-objective Grasshopper optimization algorithm, and two different decision-making methods were suggested. According to obtained results, the best swirling number and pressure ratio were 0.95 and 7, respectively. Moreover, the exergy efficiency, total product cost rate, and CO2 emission were chosen as the best optimization scenario, which led to 45.6% of exergy efficiency, 2.716 $/GJ of total product cost rate, and 30.26 kg/s of freshwater. Moreover, the total exergy destruction rate decreased from 15153 kW to 14820 kW after the optimization of the system.
... According to Fig. 2, the modeling process starts with the consideration of some simplifications and assumptions, which are presented as follows [30]: ...
In light of the movement toward sustainable development and environmental protection, this work proposes a novel cogeneration system using geothermal and natural gas dual-sources. The proposed plant is a combination of the gas turbine cycle with thermophysical recuperation, double-flash geothermal cycle, parallel dual-pressure Kalina cycle, and single-effect absorption cooling cycle for simultaneous power and cooling production. For performance investigation, energy, exergy, exergoeconomic, and economic analyses were performed. To have the optimum operating conditions of the system, a coupled model of the response surface methodology, multi-objective grey wolf optimization algorithm, and four different decision-making methods were suggested. The findings revealed that the combustion chamber has the highest contribution to total exergy destruction by 3885 kW. Based on the economic analysis, considering cooling selling cost of 0.07 $/kWh and fuel purchase cost of 3 $/GJ, increasing electricity cost to 0.15 $/kWh results in total revenue of 76.6 $M with a payback period of 0.66 years. This means that the system with mentioned prices is attractive for investment since it's profitable after some years of operation. Also, according to the optimization results, in the first optimization scenario, the optimum exergy efficiency and sum unit cost of products are determined to be 45.2 % and 3.82 $/GJ.
... It is worth noting the potential of the hybrid system from an eco- Table 6 Power block efficiency and desalination efficiency for points A, B, and C on the Pareto curve. [49][50][51]. The levelized cost is a function of the annualized capital cost (CC), operation and maintenance cost (OMC), and the total annual production (power and water): ...
... The cost functions and data of the components are valid for the reference year. The CEPCI is used to update the costs to the year 2020 [49][50][51]. ...
By integrating a membrane distillation (MD) block with a nuclear driven supercritical CO2 (sCO2) power block, a novel water and electricity cogeneration system is proposed, aiming at the water and energy supply for remote islands and coastal households. MD uses the waste heat from the sCO2 power block through an intermediate heat exchanger (IHX), while the exhaust low-pressure sCO2 flow leaving from the low temperature recuperator (LTR) is cooled by the seawater introduced into MD, without influencing the efficiency of power block. Steady state thermodynamic and economic analysis for the subsystems and the hybrid system are carried out by considering the effects of operation conditions and membrane properties. As the optimal performance of each single subsystem does not always correspond to the optimal performance of the cogeneration system, optimization genetic algorithm is employed to obtain the solutions to optimal block performance and optimal cogeneration system performance, respectively. The results predict that the maximum energy efficiency of the power block and the desalination block is 48.18% and 37.10%, respectively. The minimum levelized cost of electricity (LCOE) and levelized cost of water (LCOW) are 0.0527 $/kWh and 0.445 $/m³, respectively. The maximum exergy efficiency of the hybrid system is 67.82%. The nuclear driven sCO2-MD system is proved to be an effective layout to enhance the nuclear energy conversion efficiency and reduce water and electricity generation costs.
... Results show that the increase in the temperature reference point and the mass flow rate of biomass increase system efficiency. Hamrang et al. (2020) presented a biomass gasification-based system, a schematic of which is shown in Fig. 11. This plant is integrated to produce electricity and freshwater. ...
... Yilmaz et al. (2019) showed in another article that if the temperature of the gasifier from 688 reaches 1088 • C, the power generation rate of the system increases from 11,000 kW to 13,500 kW. The results reported in (Cao et al., 2021a;Sotoodeh et al., 2022;Yuksel et al., 2019;Hamrang et al., 2020;Xu et al., 2022;Zhang et al., 2019) also confirm this effect. But among the articles of recent years in this field, four studies reported different results; in the references (Safari and Dincer, 2022;Roy et al., 2020aRoy et al., , 2019Khanmohammadi and Atashkari, 2018), the exergy efficiency has decreased with an increase in the gasification temperature. ...
... A biomass gasification-based system for electricity and freshwater production (adapted fromHamrang et al. (2020)). ...
Biomass is the most widely used renewable energy source which is highly appreciated due to its high availability and non-intermittent nature. Considering problems such as reduction of fossil fuels, global warming, and emission of greenhouse gases, lack of attention to the existing situation may cause irreversible damage to the future of the planet. In addition to using renewable energy sources, improving the efficiency of systems will also be helpful. Polygeneration systems play an important role in increasing efficiency and reducing pollution. So, the use of biomass in polygeneration systems seems to be a great approach for sustainable development. Recent studies on biomass-based polygeneration systems have focused on how to use biomass and integrate diverse subsystems to achieve the best performance from energy and exergy viewpoints. The present paper reviews biomass-based systems, and the parameters affecting the performance of these systems. The literature review shows that the high exergy destruction rate in the gasifiers is the most frequent problem among recent articles. In addition, despite the advantages of anaerobic digestion process, the number of studies conducted on the use of this method for biomass conversion is small. In the end, results, limitations, and future outlooks of these systems are discussed.
