Dataset for Sustainable biofuel production through anaerobic digestion, SOEC and carbon-capture-and-utilization (CCU): techno‑economic, exergy and Life‑cycle analysis

Dataset for: Sustainable biofuel production through anaerobic digestion, SOEC and carbon-capture-and-utilization (CCU): techno-economic, exergy and Life-cycle analysis Towhid Gholizadeh a*, Nastaran Abbaspourb, Hamed Ghiasirada, Anna SkorekOsikowskaa a Department of Power Engineering and Turbomachinery, Silesian University of Technology, Gliwice, Poland b Institute of Chemical, Environmental and Bioscience Engineering, TU Wien, Vienna, Austria * Corresponding author’s email address: [email protected], [email protected] Table 2. Input data used to model the proposed system. Parameter Value Ref. Ambient temperature 25 ℃ Ambient pressure 1 bar Anaerobic digestion unit (ADU) Biomass type Sewage sludge [1] Digestion type Thermophilic [1] The outlet temperature of the digester 55 ℃ [1] Outlet temperature of the thermal pretreatment tank 90 ℃ [1] Temperature of sewage sludge 18 ℃ [1] Mass flow rate of biomass 8.608 kg/s [1] Biogas production of anaerobic digestate 0.167933 kg/s [1] Output pressure of pump1 2 bar [1] Output pressure of pump2 3.5 bar [1] Biogas split fraction into oxy-fuel gas turbine unit 20% Biogas split fraction into biogas upgrading unit 80% LHV of biogas 20198 kJ/kg [1] LHV of hydrogen 119950 kJ/kg [2] LHV of methanol 19920 kJ/kg [2] LHV of methane 50020 kJ/kg [2] Biogas upgrading unit (BUU) Pressure of absorber and stripper 1.05 and 1.5 bar [3] Number of stages in absorber and stripper 10 and 10 [3] Diameter of absorber and stripper 0.37 and 0.725 m [3] Height of absorber and stripper 3.5 and 4.8 m [3] Packing dimension of absorber and stripper 38 and 50 mm [3] Solid Oxide Electrolysis Cell (SOEC) Split fractions of stream 10% and 90% [4] Outlet temperature of H2, O2 100 ℃ [5] Faraday’s constant, F 96487 ℃/mol [6] Stack temperature 750 ℃ [5] Cathode effective diffusion, 𝐷c eff 5.11∙10-5 m2/s [7] Anode effective diffusion, 𝐷a eff 2∙10-5 m2/s [7] Cathode activation energy, 𝐸c act 100 000 J/mol [7] Anode activation energy, 𝐸a act 120 000 J/mol [7] Cathode pre-exponential factor, 𝛾c 1.34 A/m2 [8] Anode pre-exponential factor, 𝛾a 2.05 A/m2 [8] Cathode thickness, 𝛿c 3.13∙10-4 m [7] Anode thickness, 𝛿a 1.75∙10-5 m [7] The ideal gases constant, R 8.314 J/mol/K [7] Electrolyte thickness, 𝛿e 1.25∙10-5 m [7] Cell active area, 𝐴cell 0.324 m2 [5] Current density, J 10 000 A/m2 [9] Methanol Synthesis Unit (MSU) Pressure of gases entering the MSU 51 bar [10] Pressure drops in heat exchangers in the MSU 1 bar [11] Outlet temperature of the coolers between 4SCP of CO2 125.6℃ [11] Outlet temperature of the coolers between 4SCP of H2 and FG 157℃ [11] Inlet temperature of the distillation column 80℃ [11] Inlet and outlet temperature of methanol reactor 210 and 278℃ [10] Outlet temperature and pressure of the valve 32℃ and 1.2 bar [11] Inlet temperature of drum 35℃ [11] Pressure of the partial condenser and reboiler 1 bar [11] Number of stages in the distillation column 20 [10] Temperature of methanol and water leaving their coolers 40 ℃ [11] Isentropic efficiency of the methanol and gas compressors 0.85 [12] Separate fraction of exhaust gases from stream 324 1.01% [11] Outlet pressure of methanol compressor 1.2 bar [11] Oxy-fuel gas turbine unit (OFGTU) Pressure of combustion chamber 6 bar [13] Split fraction of exhausted gas into recycled flue gas 85% [13] Temperature of recycled flue gas into combustion chamber 300℃ [11] Pressure of condenser 1 bar [11] Temperature of condenser 35℃ [11] Table 3 shows the elemental analysis of the organic component in sewage sludge. Based on the analysis, the lower heating value of dry biomass and dry digestate were calculated as 17,221 kJ/kg and 11,527 kJ/kg, respectively [14]. Table 3. Elemental analysis of the organic component in sewage sludge [1] Element C H O N S Ash Mass fractions 0.3565 0.0489 0.2172 0.0516 0.0297 0.2961 The parameters used in the techno-economic analysis for calculating the net present value (NPV) are summarized in Table 4. Table 4. Details of the techno-economic analysis to calculate the net present value (NPV). Item Value Ref. Biomethane selling price 0.85 $/kg [15] Biomethanol selling price 1.1 $/kg [16] Inflation rate, R 5% [17,18] Discount rate, DR 8% [17,18] 1.1 Methodology of environmental analysis 1.1.1 Definition of goals and scope 1.1.2 Life Cycle Inventory (LCI) and Marginal technologies and products The identified marginal technologies and products used for system expansion are summarized in Table 7. Table 7. Details of life cycle assessment in SimaPro software Item Selected option Solar energy 570 kW photovoltaic panels, low voltage, Poland, open ground installation, multi-Si, consequential, system Wind turbine energy 1-3 MW onshore wind turbines, high voltage, Poland, consequential, system Hard coal energy Electricity production, high voltage, Rest of world, hard coal, consequential, system Natural gas enery Electricity production, high voltage, Poland, natural gas, combined cycle power plant, consequential, system Input water Natural origin Input heat Central or small-scale, Poland, co-generation, biogas, consequential, system Utilized CO2 Market for liquid CO2, consequential, system Avoided product of natural gas High pressure, Poland, market for natural gas, consequential, system Avoided product of biomethanol Market for methanol, global, consequential, system 4. RESULTS AND DISCUSSION 4.2 Main results Table 14 presents the operational benchmarks of the biofuel generation system. Fig .4 shows the amount of power supplied and consumed by all the subsystems. Table 14. Overall results of the proposed system for biofuels generation Parameter Unit Value Overall energy efficiency % 58.09 Biomethane capacity of overall system kg/h 188.68 Biomethanol capacity of overall system kg/h 269.54 Heat consumption of overall system kW 839.38 Power consumption of overall system kW 949.7 Heat consumption of anaerobic digestion unit kW -500.77 Number of SOEC cells - 3 × 80 Hydrogen yield of SOEC kg/h 23.2 Oxygen yield of SOEC kg/h 184.1 Heat consumption of biogas upgrading unit kW -930 Heat consumption of thermal pretreatment tank kW -500.77 Heat generation of oxyfuel unit into biogas upgrading unit (HX3) kW 90.612 CO2 capacity in biogas upgrading unit kg/h 298.3 CO2 capacity in Oxy-fuel gas turbine unit kg/h 201.64 CO2 utilization in MSU kg/h 499.95 CO2 emission from whole system (stream 315,324 of MSU) kg/h 7.98 Emitted CO2 per Biofuel production, 𝐸co2 - 0.01742 Fig. 4. The power suppliers and consumption of the proposed system. 4.3 Performance comparison 4.4 Results of a techno-economic analysis Table 16. Main results for economic analysis of the proposed system. Optimistic scenario Main scenario Pessimistic scenario Cost of sources 𝐶elec = 0.04 (€/kWh), Cheat = 7.712 (€/GJ), C𝑆𝑆 = 0.0(€/ton) Celec = 0.05 (€/𝑘𝑊ℎ), Cheat = 9.64 (€/𝐺𝐽), CSS = 0.0(€/𝑡𝑜𝑛) Celec = 0.06 (€/𝑘𝑊ℎ), Cheat =11.57 (€/𝐺𝐽), CSS = 1 (€/𝑡𝑜𝑛) Fixed capital investment costs (FCI, €) 2 744 227 2 744 227 2 744 227 Ratio factor (RF) 3.28 3.28 3.28 Total capital investment costs (TCI, €) 11 745 291 11 745 291 11 745 291 Annual income (AI, €) 3 654 976 3 654 976 3 654 976 Total product costs (TPC, €) 1 601 026 1 733 334 2 157 302 Annual net savings (ANS, €) 2 053 950 1 921 642 1 497 674 Payback period (PP) 5.72 6.11 7.84 Levelized cost of biomethanol (LCOM, €/ton) 233.02 294.37 490.99 Table 17. Economic analysis of proposed system based on biogas split fraction into oxy-fuel gas turbine unit (BSOF). BSOF 10 % 15 % 20% 25 % 30 % Fixed capital investment costs (FCI, €) 2 127 422 2 371 156 2 744 227 3 105 967 3 462 953 Total capital investment costs (TCI, €) 9 105 365 10 148 548 11 745 291 13 293 541 14 821 437 Annual income (AI, €) 3 486 000 3 568 800 3 654 976 3 742 000 3 850 000 949,7 10,1 -0,127 -5,38 -129,43 -824,89 -1000 -800 -600 -400 -200 0 200 400 600 800 1000 1200 Power generation of RES for overall system, kW Power generation of oxy-fuel gas turbine unit, kW Power consumption of biogas upgrading unit, kW Power consumption of anaerobic digestion unit, kW Power consumption of MSU, kW Power consumption of SOEC system, kW Total product costs (TPC, €) 1 527 362 1 633 738 1 733 334 1 877 298 2 015 964 Annual net savings (ANS, €) 1 958 638 1 935 062 1 921 642 1 864 702 1 834 036 Payback period (PP) 4.65 5.24 6.11 7.13 8.08 Levelized cost of biomethanol (LCOM, €/t) 113.24 215.70 294.37 386.24 454.33 Celec = 0.05 (€/𝑘𝑊ℎ), Cheat = 9.64 (€/𝐺𝐽),CSS = 0.0(€/𝑡𝑜𝑛) Fig. 9. The effect of biogas split fraction into oxy-fuel gas turbine unit (BSOF) on subsystems' fixed capital investment costs (FCI). 4.5 Results of life cycle assessment 0 0,5 1 1,5 2 2,5 3 3,5 4 10% 15% 20% 25% 30% FCI ( M€ ) BSOF BUU Oxy AD SOEC MSU -0,02 -0,015 -0,01 -0,005 0 0,005 0,01 0,015 0,02 0,025 0,03 0,035 Poland's electricity mix Renewable-baseline Climate change ( kg CO2eq / kg biomass) Total MSU Digestion Biogas upgrading SOEC Methan production methanol production Fig. 13. Potential environmental impact analysis results for climate change. Fig. 14. Comparison of the values of climate change for different power sources 4.6 Results of the transient study The climatic drivers exhibit marked seasonal and diurnal variability (Fig. 16). Ambient temperature ranges (Fig. 17), while mean wind speeds climb (Fig. 18). -0,02 -0,01 0 0,01 0,02 0,03 0,04 0,05 Poland's electricity mix Renewable-baseline Climate change ( kg CO2eq / kg biomass) methanol production Methan production SOEC Biogas upgrading Digestion MSU Fig. 16. Seasonal hourly global horizontal irradiance (GHI) profiles for Warsaw Fig. 17. Daily minimum, mean and maximum ambient temperatures recorded in Warsaw -20 -10 0 10 20 30 40 Jan Feb Mar Apr May Jun Jul Agu Sep Oct Nev Dec Daily temperature [°C] Daily temperatures min [°C] Daily temperatures avg [°C] Daily temperatures max [°C]