Monnerie, Nathalie

Roeb, Martin

Rosenstiel, Andreas

Sattler, Christian

Institute of Transport Research:Publications

Solar hydrogen and fuels production with concentrated solar energyEuropean Hydrogen Energy Conference EHEC 2022 – 18-20 May 2022 Madrid, SpainA. Rosenstiel, N. Monnerie, M. Roeb and C. SattlerGerman Aerospace Center (DLR), Institute of Future Fuels> Lecture > Author  •  Document > DateDLR.de  •  Chart 1Outline• Introduction• Overview of concepts for solar fuel production• Simulation and results• Concept 1• Concept 2• Summary and Outlook> Lecture > Author  •  Document > DateDLR.de  •  Chart 2Introduction> Lecture > Author  •  Document > DateDLR.de  •  Chart 3Future Fuels…Carbon dioxide (CO2)Water (H2O)Synthesis gas (H2 + CO)e.g. Fischer-Tropsch-Plant-> high energy density makes liquid fuels vital for the energy and transportation sectors in the near future, especially for long transport with truck or by aviation sectorMotivation> Lecture > Author  •  Document > DateDLR.de  •  Chart 4Identify promising production pathways for solar hydrogen and other solar fuelsOverview of concepts for solar synthesis gas production> Lecture > Author  •  Document > DateDLR.de  •  Chart 5-> Process simulation modeling have been developed-> Entire process chain of solar-produced fuels has been evaluatedDAC: potential to beuseful long termsolution to achievenet0 emissionSolar thermal liquid salts storageSimulations and resultsConcept 1 - PV/CSP hybrid power plant and low-temperature electrolysis > Lecture > Author  •  Document > DateDLR.de  •  Chart 6• By coupling: combination of advantages of bothtechnologies:• Low PV electricity generation costs• Low costs for thermal liquid salt storage• High full load hours with low electricity generation costs• Direct synthesis of methanol from CO2 and hydrogen• H2/CO2 in a molar ratio of 3:1 • Electricity demand for CO2 supply also covered by PV/CSP hybrid power plantCombination of CSP with thermal liquid salt storage with PV power plant-> Achievment of a relatively continuous power supply for AEL and other process unitsSimulations and resultsConcept 1 - Flow diagram PV/CSP hybrid power plants> Lecture > Author  •  Document > DateDLR.de  •  Chart 7• PV plant: electricity production depending on the instantaneous solar irradiance• CSP electricity production can be adapted to the demand• Aim: combination of PV and CSP electricity production in the best way for cost-optimal operation of the alkaline electrolyser systemSimulations and resultsConcept 1 - Flow diagram PV/CSP hybrid power plants> Lecture > Author  •  Document > DateDLR.de  •  Chart 8Coupling solar H2 production to MtG plantContinuous gasoline production processSimulations and resultsConcept 1 - Process simulation: Hierarchy MTG process material> Lecture > Author  •  Document > DateDLR.de  •  Chart 9Prozesskomponente Methanolsynthese(Lurgi Prozess)Anzahl Reaktoren 2Kohlenstoffumsatzper Pass41,4 %DruckMethanolreaktorR1/R280 barBetriebstemperaturR1/2max. 255 °CProzesskomponente MTG-Prozess(Syngas-To-FuelVerfahren) [2]Temperatur MTG-Reaktor340 °CMethanol-To-FuelWirkungsgrad88,2 %• Simulation with Aspen Plus• Hierarchy Block• different combinations of the PV and CSP technologies are investigated• For comparison, systems with only PV or CSP electricity production are simulatedSimulations and resultsConcept 1 - Energy flow diagram of the overall process> Lecture > Author  •  Document > DateDLR.de  •  Chart 10Werte für 2030 OuarzazatePtL Wirkungsgrad 47,5%H2tL Wirkungsgrad (LHV) 68,4%Overall efficiency from solar to gasoline: 7,3% Simulations and resultsConcept 1 - Techno-economic model> Lecture > Author  •  Document > DateDLR.de  •  Chart 11➢ dynamic annual simulations (temporal resolution of 1 h)Overall plant design optimization approach:Minimisation of product costs:൯min(𝐿𝐶𝑂𝐻) = 𝑓(𝑃 𝐶𝑆𝑃,𝑅𝑒𝑐, 𝑃𝑃𝑉,𝑃𝑒𝑎𝑘, 𝑃𝐴𝐸𝐿, 𝑃𝑇𝑢𝑟𝑏, C𝑇𝐸𝑆, P𝐻𝑒𝑎𝑡𝑒𝑟,𝑒𝑙Simulations and resultsConcept 1 - Results Minimisation of hydrogen production costs> Lecture > Author  •  Document > DateDLR.de  •  Chart 12• influence of different solar resources• Local price index for installation ofsolar equipment• Freiburg: only PV • CSP: for a DNI in the range of 2000 kWh/m2a and above• 2 cost scenarios: today and scenario which considers the possible cost reductions until 2030• -> today: lowest hydrogen costs :4.04 USD/kgH2 with AEL powered by a hybrid PV/CSP plant• -> 2030: 3.09 USD/kg • Selling of surplus electricity and of O2 as a by-product is not considered Simulations and resultsConcept 2 - Solar thermochemical hydrogen and synthesis gas production> Lecture > Author  •  Document > DateDLR.de  •  Chart 13Source: sun-to-liquid.eu• Direct synthesis gas generation with solar high-temperature heat• High potential in the mid-long term• Synthesis gas then converted into a syncrude in a low-temperature Fischer-Tropsch process, from which the Fischer-Tropsch fuel is obtained through subsequent processingCO2/H2OstorageThermochemicaltransformationFuel DesignPerformanceSyngas solarH2O CO2Solar energyH2O/CO2synthesisEmission controlDrop-In fuelReduktion (endotherm)OTemperaturTredH2O/CO2 Spaltung (exothermal)Toxthermochemischer KreisprozessOO OCfuel (syngas)OCKonzentrierte SolarstrahlungSpeicherungvon SolarenergieH HHHOOO22red2ox O/COHMO    /COHMO ++oxMO redMO2redox OMOMO +→Simulations and resultsConcept 2 - Solar thermochemical hydrogen and synthesis gas production> Lecture > Author  •  Document > DateDLR.de  •  Chart 14• Based on an innovative thermochemical cycle and on a thermochemistry model with 3 receivers • CeO2 operating at 1773 K and 1300 K for reduction and oxidation step• Faster kinetics and better stability and selectivity• Particle form• Carrying out of the reduction of cerium oxide in series-connected reactors• Reduce the required vacuum pump work and to achieve thus higher efficiency in hydrogen or synthesis gas production• Production of synthesis gas as continuously as possible• 2 storage units provided in the process:• 1 for reduced particles to achieve a relatively continuous particle flow for the synthesis gas supply, which also enables continuous heat extraction• 1 for oxidised particles to adapt the particle flow to the reduction reactors to the currently available solar supplySimulations and resultsConcept 2 - Modelling Fischer-Tropsch process> Lecture > Author  •  Document > DateDLR.de  •  Chart 15• Modelling: approach Chain growth probability α as a function of reactor temperature and H2/CO ratio• Assumption: Only alkanes in the productProzesskomponente Fischer-Tropsch Prozess (Cobalt-Festbett Reaktor)Kettenwachstumsgeschwindigkeit α 83,9 %CO-Umsatz [6] 40 %Druck FT-Reaktor [6]. 25 barReaktortemperatur [6]. 220 °CProzesskomponente RWGS Reforming ReaktorTemperatur RWGS-ReformingReaktor900 °CDruck RWGS-Reforming Reaktor 1,5 barProzesskomponente HydrocrackerTemperatur Hydrocracker [7] 370 °CDruck Hydrocracker [7] 35 bar(*) Vervoloet et al (2012), DOI: 10.1039/c2cy20060k(**) Adelung et al (2020)´, https://doi.org/10.1016/j.seta.2020.100897 Simulations and resultsConcept 2 – Coupling to solar thermochemical synthesis gas production with Fischer-Tropsch process> Lecture > Author  •  Document > DateDLR.de  •  Chart 16FTRB3RWGSH2OKNOCKB14 B15B16B17B19H2STORSYNCOM PB9DESIGN-SPECB26B4B7B20B1B2 B6B11CO2H2STEAMS6S1SYNCRUDEGASPRODS4S5H2ORECS10S18S21H2PROD2425S28S17S34S19ST EAMOXS24H2OADDS8S12S14 S20S2S13Array of thermochemical reactorsS23RGIB BSTC1RGIB BSTC2RGIB BSTC3RGIB BSTC4S25S26S27ST EAMINHIER ARCHYTC5OXYGENHIER ARCHYEVAPORB30S31B31S32S33S35Fischer-Tropsch Process• Recirculation of gaseous FT products into RWGS reforming reactor (endothermic)• Utilisation of thermal energy of the reduced particles (exit storage RPS)• Target product C5-C12𝐻2 + 𝐶𝑂2 ↔ 𝐶𝑂 + 𝐻2𝑂𝐶𝐻4 + 𝐶𝑂2 ↔ 2𝐶𝑂 + 2𝐻2𝐶𝐻4 +𝐻2𝑂 ↔ 𝐶𝑂 + 3𝐻2Reverse water-gas shift reactionDampf- und CO2 ReformierungSimulations and resultsConcept 2 – Energy flow diagram solar thermochemical Fischer-Tropsch process> Lecture > Author  •  Document > DateDLR.de  •  Chart 17Location: Ouarzazate (Morroco)Overall efficiency from solar to gasoline: 8,2% Summary and Outlook> Lecture > Author  •  Document > DateDLR.de  •  Chart 18➢Two solar concepts have been investigated:➢Concept 1: PV/CSP + alkaline electrolysis + Methanol-to-Gasoline: overall h:7.3%➢Concept 2: solar thermochemical cycle + Fisher-Tropsch plant: overall h:8.2%➢Techno-economic model was developed:➢H2 Production cost (Concept 1): 3.09 USD/kg ➢Final techno-economic / ecologic assessment➢Consideration for three locations: Spain (Almeria), Morocco (Ouarzazate), United Arab Emirates.➢Optimised plant configuration for each site➢Minimisation of the CO2 footprint➢Minimisation of product costs taking into account all positive boundary conditions in the economic efficiency➢Sensitivity analysis: influence of the use of carbon point sourceThank you for your attention!The authors of this paper gratefully acknowledge the funding of the project SolareKraftstoffe (Grant agreement Nr. 03EIV221) by the Federal Ministry for Economic Affairs and Energy, on the basis of a decision by the German Bundestag.nathalie.monnerie@dlr.de> Lecture > Author  •  Document > DateDLR.de  •  Chart 19

Solar hydrogen and fuels production with concentrated solar energy

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Solar hydrogen and fuels production with concentrated solar energy

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