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the various state points in the system. The initial CO2 from state 2 is preheated in the low temperature recuperator and reaches state 2a where the two CO2 streams combine. The complete stream is then further preheated in the high temperature recuperator and reaches state 3. Further heat addition from external sources like Energies 2020, 13, 5043 7 of 20 combustion of a fuel or a concentrating solar thermal heat transfer fluid via a heat exchanger brings the CO2 to state 4. For the purposes of the analysis here, we use combustion of methane to generate here is that the heat rejected from the pre-cooler can drive the sorption/desorption based air separation the heat in order to provide the most direct comparison with the FFCTH system. A turbine extracts unit, thus making this system self-sustained and powered by one fuel source and one injection point. mechanical energy from the sCO2 stream between state 4 to state 5. The turbine exit stream preheats The efficiency of the sorption/desorption based air separation unit is assumed to be in the acceptable the incoming CO2 streams in the high temperature recuperator, reaching state 5a, and in the low range. This assumption applies due to the various tunable state points in the cycle and parameters in temperature recuperator, reaching state 6. Heat rejection to the environment or for external thesystemdeppernodciensgsiunpgohnetahteinmgaoteccriuarlsuinsetdhfeorpareir-csoeoplaera,ttionr.eTtuhrensttaotesptaotient1s.oCfothoelinsCgOthecyecxlehaust from the 2 remainthesamceoamsbshuostwonr iannFdigsurpep1lywiinthgttwhoeramdadlitieonnearlgcyomtopothnenstsC:O(12)thuerabtirneecocvyecrlyeffraocmilithaeteFsFCmaximizing the subsystem ande(l2e)ctariircaselpefafriactieionncyfr.om a sorption unit. To identify theThaedvelaenctarigceasl eafnfidciednrcaywobfacthkes sotfanreddaerdsigsnCiOng2 csyoclteh(aηtSStGhTe) gsiyvsetnemincFaingubre C1Ois2represented in sequestration-rEeaqduya,tiwone t(h1)e,owrehteicraelly analiysztehde thoitsalsCysOte2mawsisthfloawndrawteitihnotuhteacirycslep. aTrhaetisopne. cWifictheonutht alpies of states separation, the FFC subsystem uses air, whereas with separation it produces and utilizes pure oxygen. 1, 2, 2a, 4, 5, and 6, are h1, h2, h2a, h4, h5, and h6, respectively. The coefficients 0.53 and 0.47 are the mass We compare the system efficiencies, the fuel requirement, and the P/H for cases with and without the fraction of CO2 entering the main compressor and secondary compressor, respectively. The mass flow rate of methane required to provide the necessary thermal energy is , and HHVf is the higher FFC integrated and with and without sorption-based air separation. Equation (17) shows the electrical efficiencyoftheFFCintegratedsCO turbineFFCTH(η ),whereP andP isthepower heating value of meth2ane. PCC is the totaFFlCeGlTectrical powFFeCr requirCeOdGfTor CO2 compression during 2 generatedbyFFCandbythesCO turbinecycle,respectively.Theheatrequiredfortheairseparation sequestration. Prev2ious literature has shown that the specific power required for compression and unitistakenfromtheheatrejectedinthesCO cyclepre-cooler(states6to1).Theelectricalefficiency refrigeration of CO2 for seques2tration at 15 Bar is 107 kW/kg CO2 [41], which is used in this work. of the FFCTH is given by Equation (17). 3. Experimental This power is kept zero when sequestration is not assessed. ɳ = FFC CO2 GT CC = (17) (1) (h −h )−0.47(h −h )−0.53(h −h )− P +P −P FFCGT m.HHV An experimental assessment and analysis of the FFC performance operating in methane and oxygen fuel-rich combustion exhaust provided data to calibrate and enable simulation of the FFCTH system. Figure 4 shows the schematic of the experimental setup. Use of mass flow controllers regulated the flow of the gases. Connecting the fuel lines for CO and H2 to flame arrestors mitigates and avoids flashback risk. Figure 4. Schematic of the experimental setup with gases mixture used for model exhaust. The flow rates of the gases used in the experiment (CO, H2, CO2) were calculated using chemical equilibrium, from NASA Chemical Equilibrium and Applications (CEA) [43], for the combustion exhaust composition at a constant inlet fuel flow rate of 0.066 mg·s−1. Methane was used as an approximation for natural gas since natural gas is up to 90% methane by molar content [44] and thus, using methane instead of natural gas would not lead to significant departure from the natural gas case. Sulfur impurities will need to be removed from the natural gas before its use in the fuel cell due to ffPDF Image | Hybrid Fuel Cell Supercritical CO2 Brayton Cycle CO2 Storage
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