Generation of ammonia/hydrogen mixtures and/or hydrogen-enriched fuel mixtures
Methods for the operation of membrane reactors (MRs) are disclosed for the efficient production of hydrogen-enriched fuel blends with tunable composition and high hydrogen recovery at both elevated and isobaric pressure operation. These methods enable use of greatly reduced operating temperatures relative to packed bed reactors (PBRs) and elimination of the need for a secondary separation unit operation. These methods provide greater productivity and hydrogen recovery while relaxing membrane selectivity constraints relative to conventional MR operation.
1 . A method for producing a hydrogen-enriched fuel stream, comprising:
introducing a feed stream comprising ammonia into a feed region of a catalytic membrane reactor, wherein the catalytic membrane reactor comprises:
a feed vessel, comprising a feed-facing surface and a permeate-facing surface, wherein the permeate-facing surface is impregnated with a first metal catalyst and coated with a hydrogen-selective membrane;
a permeate vessel;
the feed region, in contact with the feed-facing surface of the feed vessel and containing particles of a second metal catalyst; and
a permeate region, in contact with the permeate-facing surface of the feed vessel;
causing at least a portion of the ammonia in the feed stream to undergo a decomposition reaction to form a product gas stream comprising hydrogen gas within the feed region, wherein the decomposition reaction is catalyzed by the first and second metal catalysts;
passing at least a portion of the hydrogen gas in the product gas stream through the hydrogen-selective membrane to form a separated hydrogen gas stream in the permeate region, thereby leaving a remainder of the product gas stream in the feed region as a retentate gas stream;
flowing the retentate gas stream out of an exit of the feed region;
passing a sweep gas comprising a fuel into the permeate region to form the hydrogen-enriched fuel stream; and
flowing the hydrogen-enriched fuel stream out of an exit of the permeate region,
wherein at least one of the following is true:
(i) a pressure of the feed stream and a pressure of the sweep gas are approximately equal; and
(ii) a pressure of the retentate gas stream and a pressure of the hydrogen-enriched fuel stream are approximately equal.
2 . The method of claim 1 , wherein the at least a portion of the hydrogen gas comprises at least about 98% of the hydrogen gas in the product gas stream.
3 . The method of claim 1 , wherein an ideal H 2 /N 2 selectivity of the hydrogen-selective membrane is between about 10 and about 10,000.
4 . The method of claim 1 , wherein the fuel of the sweep gas is selected from the group consisting of ammonia, natural gas, methane, propane, butane, vaporized hydrocarbons, and combinations thereof.
5 . The method of claim 1 , wherein a hydrogen content of the hydrogen-enriched fuel stream is from about 1 vol % to about 99 vol %.
6 . The method of claim 1 , wherein the decomposition reaction is carried out at a temperature of no more than about 450° C.
7 . The method of claim 6 , wherein the temperature is no more than about 400° C.
8 . The method of claim 7 , wherein the temperature is no more than about 350° C.
9 . The method of claim 1 , wherein the temperature is at least about 300° C.
10 . The method of claim 1 , wherein the decomposition reaction is carried out at atmospheric or superatmospheric pressure.
11 . The method of claim 10 , wherein the decomposition reaction is carried out at a pressure from about 0 barg to about 50 barg.
12 . The method of claim 10 , wherein the decomposition reaction is carried out at a pressure of at least about 5 barg.
13 . The method of claim 1 , wherein at least one of the first and second metal catalysts comprises ruthenium.
14 . The method of claim 1 , wherein the feed vessel comprises a ceramic support material.
15 . The method of claim 14 , wherein the ceramic support material comprises yttria-stabilized zirconia.
16 . The method of claim 1 , wherein the second metal catalyst comprises aluminum (III) oxide (Al 2 O 3 ).
17 . The method of claim 1 , wherein the hydrogen-selective membrane comprises palladium.
18 . The method of claim 17 , wherein the hydrogen-selective membrane has a thickness of no more than about 5.0 μm.
19 . The method of claim 1 , wherein the feed-facing surface of the feed vessel is impregnated with the first metal catalyst.