. 2023 Jul 16;37(15):10775–10798. doi: 10.1021/acs.energyfuels.3c00760

Table 9. NH₃ Conversion and Corresponding Hydrogen Recovery Achieved in Membrane Reactors for Ammonia Decomposition Studies Available in Literature.

	Membrane			Reactor operating conditions						NH₃ conversion [%]
Author(s) [ref]	Membrane composition	Selective layer thickness [μm]	Length [mm]	Temperature [°C]	Reaction pressure [bar]	Permeate pressure [bar]	NH₃ feed flow rate [mL_N/min]	GHSV [mL/(g_cat h)]	Catalyst	Conventional reactor	Membrane reactor	Hydrogen recovery [%]
Zhang et al.¹⁷	Pd + Ru/YSZ	6.2	N/A	400	5	1	30^a	N/A	Ru (impregnated in the membrane support)	31^a	93	N/A
Zhang et al.¹⁷	Ru-Cs/YSZ + Pd	6.2	N/A	400	5	1	61.3	N/A	Ru (impregnated in the membrane support)	N/A	98	87.5
Zhang et al.²⁷	Pd + Al₂O₃	3	N/A	500	5	1	200^b	2000	Ni/La-Al₂O₃ (Ni/Al = 1.20, La/Ni = 0.22), 6 g	95^a	>99^a	92^a
Cechetto et al.⁴⁰	Al₂O_3-–YSZ + Pd-Ag + Al₂O₃	∼6–8	195	500	6	1	500	120^b	(2 wt %) Ru/Al₂O₃, 250 g	N/A	99.8	91.6
Cechetto et al.⁶⁵	Al₂O₃-YSZ + Pd-Ag + Al₂O₃	4.61	202	400	4	Vacuum	500	120^b	(2 wt %) Ru/Al₂O₃, 250 g	65.4	99.3	93.5
Cechetto et al.⁶⁵	Al₂O₃-YSZ + Pd-Ag + Al₂O₃	4.61	190	450	5	1	500	120^b	(2 wt %) Ru/Al₂O₃, 250 g	N/A	99.7	90.5
Cerrillo et al.⁶⁶	Pd-Au + ceramic support	8	186^a	485	5	1	200	1200^b	(0.5 wt %) Ba-CoCe, 10 g	N/A	>99^a	92^a
Liu et al.⁶⁷	Pd + stainless steel support + MnCO₃	6.5	N/A	400	3	1	47^b	1880	(5 wt %) Ru/MgO, 1.5 g	N/A	99.8	N/A
Li et al.⁷⁶	Ru/γ-Al₂O₃/α-Al₂O₃+ SiO₂	<0.3	N/A	400	1	Vacuum	10	N/A	(0.45 wt %) Ru/γ-Al₂O₃/α-Al₂O₃, Ru impregnated in the membrane support	55	84	77
Jiang et al.⁷⁷	Pd-Ag + Al₂O₃	1.8	100^a	450	7	1	250^b	5000	(3 wt %) Ru/(1 wt %)Y/(12 wt %) K/Al₂O₃, 3 g	N/A	99.11	90.6
Itoh et al.⁷⁹	Pd	200	65	450	1	Vacuum	9.7	1164^b	(5 wt %) Ru/SiO₂, 0.5 g	73^a	87^a	59^a
Itoh et al.⁸⁰	Pd + Al₂O₃ + Ru	2	90	375	1	Vacuum	20	N/A	(2 wt %) Ru/Al₂O₃, 0.88 g	35^a	>99^a	N/A
Kim et al.⁸²	Pd + Inconel 600	∼5	450	430	5	Vacuum	950	N/A	(2 wt %) Ru/Al₂O₃, N/A	N/A	99.4	97.5
Omata et al.⁸³	Pd-Ag + V-Fe	∼0.2 μm Pd-Ag	N/A	350	3	1	10	3000^b	(5 wt %) Ru/Cs₂O/Pr₆O₁₁, 0.2 g	52.6%^a	89^a	89^a
Omata et al.⁸³	Pd-Ag + V-Fe	∼100 μm V-Fe	N/A	350	3	1	10	3000^b	(5 wt %) Ru/Cs₂O/Pr₆O₁₁, 0.2 g	52.6%^a	89^a	89^a
Jo et al.⁸⁴	Pd/Ta	∼0.4 μm Pd	N/A	450	6.5	1	3000^b	30000	(1.6 wt %) Ru/La-Al₂O₃, 6 g	N/A	>99.5	N/A
Jo et al.⁸⁴	Pd/Ta	∼250 μm Ta	N/A	450	6.5	1	3000^b	30000	(1.6 wt %) Ru/La-Al₂O₃, 6 g	N/A	>99.5	N/A
Park et al.⁸⁵	Pd/Ta/Pd	∼1–2 μm Pd	N/A	500	5	1	100^b	6000	(0.65 wt %)Ru/(10 mol %)La-Al₂O₃, 1 g	N/A	95^a	86^a
Park et al.⁸⁵	Pd/Ta/Pd	∼250 μm Ta	N/A	500	5	1	100^b	6000	(0.65 wt %)Ru/(10 mol %)La-Al₂O₃, 1 g	N/A	95^a	86^a
Israni et al.⁸⁶	Pd/γ-Al₂O₃/α-Al₂O₃	∼13	156	500	3	1	65^a	135^b	(70 wt %) Ni/γ-Al₂O₃, 29 g	N/A	99^a	80^a
Sitar et al.⁸⁷	Pd + Ru/YSZ	4.23	73	450	5	1	100	1200^b	(0.5 wt %) Ru/Al₂O₃, 5 g in the catalyst bed	N/A	>99^a	>90^a
Sitar et al.⁸⁷	Pd + Ru/YSZ	4.23	73	450	5	1	100	1200^b	(1.9 wt %) Ru/YSZ, Ru impregnated in the membrane support	N/A	>99^a	>90^a
Rizzuto et al.⁸⁹	Pd + metallic support	N/A	N/A	450	5	1	245	N/A	(N/A) Ru/Al₂O₃, N/A	N/A	>99^a	91^a

Data not directly reported in the publication and retrieved from graphic representation of experimental results.

Data not directly reported in the publication. Calculated based on provided information about catalyst and flow rates used.

Table 9. NH3 Conversion and Corresponding Hydrogen Recovery Achieved in Membrane Reactors for Ammonia Decomposition Studies Available in Literature.

Table 9. NH₃ Conversion and Corresponding Hydrogen Recovery Achieved in Membrane Reactors for Ammonia Decomposition Studies Available in Literature.