3rd International Conference and Expo on Oil and Gas in Berlin
Jordan, a non-oil producing country, faces energy challenges and explores oil shale combustion under oxyfuel conditions. Detailed analysis, experimental results, and discussions are presented from the study conducted at Al-Hussein Bin Talal University and Jordan University of Science and Technology.
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3rd International Conference and Expo on Oil and Gas July 13-14, 2017 Berlin, Germany LeemaAl-Makhadmeh Al-Hussein Bin Talal University, Jordan University of Science and Technology, Jordan l.al-makhadmeh@ahu.edu.jo lamakhadmeh@just.edu.jo
Presentation Outline Introduction Oxyfuel Combustion Experimental Part Results and Discussion Conclusions 2/20/2025 2
Introduction Jordan is a non-oil producing country and is largely affected by the world energy situation; it has a clear plan for oil-shale utilizations. Oil-shale resources in Jordan are estimated to be 40 billion tons, in which the oil is about 4 billion tons. Oil shale utilization in Jordan and elsewhere faces many obstacles that affect its utilization. Oil shale combustion under oxyfuel conditions was investigated in this study in a trial to solve some of the challenges that faces Jordanian oil shale combustion. 2/20/2025 3
Oxyfuel Combustion Oxyfuel combustion, a combination of oxygen, with a purity of more than 95%, and recycled flue gas is used for combustion of the fuel. Recirculated flue gas N2 O2 CO2 CO2 storage air ASU recovery Boiler Fuel CO2, H2O, H2O 2/20/2025 4
Experimental Part El-Lajjun oil-shale from south of Jordan was used in this study. The following table shows the detailed analysis of oil shale . Oil shale combustion was performed in a vertical 20- kW furnace (see the following Fig). Both unstaged and staged combustion experiments were performed in air and OF27 condition. The wall temperature during all the combustion experiments was 1200 C. 2/20/2025 5
El-Lajjun oil-shale analysis Proximate Analysis Water (ar, %) 1.08 Ash (wf, %)2 54.20 Volatile (waf, %)3 99.06 Fixed carbon (waf, %) 0.85 Ultimate Analysis 1: as received 2: water free 3: water ash free 4: by difference 5 Di: represent that i% by volume of the particles that have a diameter equal to or less than Di. C (waf, %) 55.68 H (waf, %) 4.27 N (waf, %) 0.87 S (waf, %) 8.30 O (diff, %)5 30.88 LHV (waf, kJ/kg) 19585.15 D90 ( m) 35.3 2/20/2025 6
A once-through vertical 20 kW furnace 2/20/2025 7
Results and Discussion Oil shale behavior during unstaged combustion NO air-firing SO2 air-firing NO OF27 SO2 OF27 O2 air-firing CO air-firing O2 OF27 CO OF27 800 9000 30 1.6 8000 700 1.4 25 7000 600 1.2 SO2, ppm 6000 CO, vol% 20 500 1 NO, ppm O2, vol% 5000 400 15 0.8 4000 0.6 300 10 3000 0.4 200 2000 5 0.2 100 1000 0 0 0 0 0 0.5 1 1.5 2 2.5 0 0.5 1 1.5 2 2.5 distance from burner, m distance from burner, m Axial concentration profiles of oxygen, carbon monoxide, nitrogen oxide and sulphur dioxide for air-firing and OF27 combustion (excess O2 = 3%, T = 1200 C). 2/20/2025 8
Oil shale emission during unstaged combustion NO emission Conversion, % SO2 emission Conversion, % 600 100 8000 100 6762 Oil shale-N conversion to NO, % Oil shale-S conversion to SO2, % 433 7000 500 80 NO emission, mg/MJ 80 SO2 emission, mg/MJ 6000 4933 400 5000 60 60 69 237 300 4000 40 49 40 27 3000 200 15 2000 20 20 100 1000 0 0 0 0 air-firing OF27 air-firing OF27 NO and SO2 emissions and their conversions during air-firing and OF27 combustion at the exit of the reactor for El-Lajjun oil shale combustion. 2/20/2025 9
Oil shale behavior during staged combustion NO O2 CO 400 25 350 25 350 300 20 20 300 250 O2 and CO, vol% O2 and CO, % 250 15 15 NO, ppm NO, ppm 200 200 150 10 10 150 100 100 5 5 50 50 0 0 0 0 0 0.5 1 1.5 2 2.5 0 0.5 1 1.5 2 2.5 distance from burner, m distance from burner, m Air-firing OF27 combustion Axial concentration profiles of O2, CO, and NO for staged air-firing and OF27 combustion ( =0.75, T = 1200 C, 2 m far from the burner). 2/20/2025 10
Reduction of NO emissions using staged combustion NO emission Oil shale-N conversion to NO 450 30 450 30 27.34% Air-firing Oil shale-N conversion to NO, % Oil shale-N conversion to NO, % OF27 combustion 400 400 25 25 350 350 NO emission mg/MJ NO emission mg/MJ 300 20 300 20 14.67% 250 250 15 15 200 7.46% 200 150 10 150 10 6.61% 3.90% 100 4.24% 100 2.86% 3.31% 5 5 50 50 0 0 0 0 0.75 0.85 0.95 1.19 0.75 0.85 0.95 1.15 burner oxygen ratio, burner oxygen ratio, NO emissions and Oilshale-N conversion over burner oxygen ratio under air-firing and OF27 combustion. 2/20/2025 11
Reduction of simulated recycled NO during undstaged and staged combustion NO-injected NO-measured Reduction of simulated recycled NO 1400 100 Reduction of simulated recycled NO, % 64% 1200 57% 1067 80 62% 65% 59% 1000 909 821 820 723 60 NO, ppm 800 711 649 622 601 600 40 432 451 400 20 200 0 0 Unstaged OF27-3% 800 99% 99% 99% Reduction of simulated recycled NO, % 99% 700 100 600 702 80 498 500 60 NO, ppm 400 311 300 40 136 200 147 145 139 138 134 20 100 0 0 Staged OF27- =0.75, t3s 2/20/2025 12
In-furnace limestone addition during unstaged combustion SO2 Desulphurization efficiency 7000 100 7000 100 6279 80.28% Desulphurization efficiency, % 99.68% 6000 6000 Desulphurization efficiency, % 95.28% 80 80 5136 SO2 emission, mg/MJ SO2 emission, mg/MJ 5000 88.35% 5000 43.85% 48.51% 60 60 4000 4000 3000 3000 40 40 3526 2000 2000 2645 1238 20 20 1000 598 1000 297 16 0 0 0 0 0 1 2 3 0 1 2 3 Ca/S molar ratio Ca/S molar ratio Air-firing OF27 combustion SO2 emissions and the efficiency of desulphurization during unstaged air-firing and OF27 combustion (Ca/S ratios=1, 2, and 3) 2/20/2025 13
In-furnace limestone addition during unstaged combustion 7000 6279 6000 5136 SO2 emission, mg/MJ 5000 4300 3859 3525 4000 3550 3103 air OF27 2643 3000 2000 1238 598 1000 0 0.75 0.85 0.95 unstaged 1 unstaged 2 Burner oxgen ratio, Fig. 3. SO2 emission during unstaged and staged air-firing and OF27 combustion, limestone molar ratio is Ca/S=2 for staged combustion and for unstaged1, unstaged2 without limestone addition. Position of staged probe is 2 m from the burner. 2/20/2025 14
Conclusions During OF27 combustion, the CO concentration in the burner section is much higher than air-firing due to the gasification reactions in a CO2-rich medium. Even though, there is almost no problem for CO controlling for OF27 combustion as well as air-firing. Oxidant staging was used efficiently for NO reduction from oil shale combustion in both modes. Oil-shale N conversion to NO at the exit of the furnace during unstaged mode and with oxygen burner ratio of 0.95 is lower for OF27 combustion compared to air-firing. 2/20/2025 15
During unstaged and staged air-firing and OF27 combustion, the simulated recycled NO is efficiently reduced. The simulated recycled NO reduction is more efficient during staged OF27 combustion than unstaged case. El-Lajjun oil shale- S conversion rates to SO2 is 69% and 49% for air-firing and OF27 combustion, respectively. By using direct in furnace limestone injection, SO2 emission was reduced significantly in both unstaged and staged OF27 and air-firing as well. 2/20/2025 16
The desulfurization efficiency was affected by the oxidant-stage level, Ca/S molar ratio and position of the secondary oxidant. The combustion in staged air-firing and in staged OF27 combustion ranged from 32 to 61% and from 25 to 60%, respectively. desulfurization efficiency for oil shale The desulfurization efficiency during unstaged combustion was much higher than that during staged combustion. 2/20/2025 17
3rd International Conference and Expo on Oil and Gas July 13-14, 2017 Berlin, Germany Thank you 2/20/2025 18
