Incremental hydrogen production from an existing steam/natural gas reformer

Abstract

In some aspects, a method for incremental hydrogen production includes separating in a first Pressure Swing Absorption (PSA) system an existing reformer synthesis gas product stream into a first hydrogen stream and a first waste stream. The first waste stream is compressed to at least 40 bar to produce a compressed waste stream. Water is removed from the compressed waste stream to produce a dried waste stream. Carbon dioxide is removed from the dried waste stream to produce a remaining waste stream, and the removed carbon dioxide is at least 85% of carbon dioxide in the existing reformer synthesis gas product stream. A second PSA system separates the remaining waste stream into a second hydrogen stream and a second waste stream, and the second hydrogen stream comprises at least 11% of hydrogen from the existing reformer synthesis gas product stream.

Claims

1. A method for incremental hydrogen production, comprising: separating in a first Pressure Swing Absorption (PSA) system an existing reformer synthesis gas product stream into a first hydrogen stream and a first waste stream; compressing the first waste stream to at least 40 bar to produce a compressed waste stream; removing water from the compressed waste stream to produce a dried waste stream; removing carbon dioxide from the dried waste stream to produce a remaining waste stream, wherein the removed carbon dioxide is at least 85% of carbon dioxide in the existing reformer synthesis gas product stream; separating in a second PSA system the remaining waste stream into a second hydrogen stream and a second waste stream, wherein the second hydrogen stream comprises at least 11% of hydrogen from the existing reformer synthesis gas product stream; and passing the second waste stream to a reformer furnace as fuel gas.

2. A system for incremental hydrogen production, comprising: a first Pressure Swing Absorption (PSA) system configured to separate an existing reformer synthesis gas product stream into a first hydrogen stream and a first waste stream; a compressor configured to compress the first waste stream to at least 40 bar to produce a compressed waste stream; a drier configured to remove water from the compressed waste stream to produce a dried waste stream; a low-temperature separator configured to remove carbon dioxide from the dried waste stream to produce a remaining waste stream, wherein the removed carbon dioxide is at least 85% of carbon dioxide in the existing reformer synthesis gas product stream; a second PSA system configured to separate the remaining waste stream into a second hydrogen stream and a second waste stream, wherein the second hydrogen stream comprises at least 11% of hydrogen from the existing reformer synthesis gas product stream; and a conduit configured to pass the second waste stream to a reformer furnace as fuel gas.

Description

DESCRIPTION OF DRAWINGS

(1) FIG. 1 is an example system for incremental hydrogen production.

(2) Like reference symbols in the various drawings indicate like elements.

DETAILED DESCRIPTION

(3) FIG. 1 illustrates an example system for incremental hydrogen production. For example, the process for incremental hydrogen production from an existing catalytic steam/natural gas reformer may use a low-temperature CO.sub.2 condensation process to separate the CO.sub.2 present in the waste gas from an existing reformer pressure swing adsorption (PSA) hydrogen separation unit so that the remaining hydrogen enriched waste gas may then be sent to a second PSA unit where more H.sub.2 can be separated. The waste gas stream 16 may initially be compressed from, for example, about 1.2 bar to 40 bar in the compressor 17 and then the compressed waste gas stream 4 is dried in, for example, an adsorbent bed drier 12, which is regenerated by a nitrogen gas stream 5 and 6. As illustrated, the compressed waste gas steam 7 enters the CO.sub.2 condensation system 3 where it is cooled to, for example, within 2 C. of its triple point temperature. The liquid CO.sub.2 is separated and evaporated to produce refrigeration for the process and the CO.sub.2 product leaves as two separate streams 10 and 11 at an average pressure of about 10 bar. The remaining compressed waste gas, stream 8, containing about 65% H.sub.2, is separated in the PSA 2 producing a substantially pure H.sub.2 stream 9 at 35 bar pressure and a waste gas stream 14 which is used as part of the fuel gas in the existing reformer furnace. In some implementations, the system described can produce an incremental 11% more H.sub.2 from the existing reformer synthesis gas product stream 1. The incremental H.sub.2 production may use additional natural gas to replace the H.sub.2 which would have been burned in the reformer furnace. The fuel consumption for the incremental H.sub.2 production is, in some implementations, 280 Btu/scf H.sub.2. In these instances, the produced CO.sub.2 in streams 10 plus 11 can be about 85% of the CO.sub.2 present in the reformer product stream 1.

(4) A number of embodiments of the invention have been described. Nevertheless, it will be understood that various modifications may be made without departing from the spirit and scope of the invention. Accordingly, other embodiments are within the scope of the following claims.