TWO-MODE PROCESS FOR HYDROGEN PRODUCTION

• US 20110064648A1
• Filed: 09/15/2010
• Published: 03/17/2011
• Est. Priority Date: 09/16/2009
• Status: Abandoned Application

• Current Assignee: Sure Champion Investments Limited
• Original Assignee: GreatPoint Energy, Inc.
• Inventors: Sirdeshpande, Avinash, Preston, William E.
• Application Number:
  US12/882,417
• Publication Number:
  US 20110064648A1
• Time in Patent Office: Days
• US Class Current: 423/648.1
• CPC Class Codes: C01B 2203/0244 the reforming step being an autothermal reforming step, e.g. secondary reforming processes
• CPC Class Codes: C01B 2203/0255 containing a non-catalytic partial oxidation step
• CPC Class Codes: C01B 2203/0261 containing a catalytic partial oxidation step [CPO]
• CPC Class Codes: C01B 2203/0288 containing two CO-shift steps
• CPC Class Codes: C01B 2203/0405 Purification by membrane separation
• CPC Class Codes: C01B 2203/0415 Purification by absorption in liquids
• CPC Class Codes: C01B 2203/043 Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
• CPC Class Codes: C01B 2203/0445 Selective methanation
• CPC Class Codes: C01B 2203/046 Purification by cryogenic separation
• CPC Class Codes: C01B 2203/047 the impurity being carbon monoxide
• CPC Class Codes: C01B 2203/0475 the impurity being carbon dioxide
• CPC Class Codes: C01B 2203/0485 the impurity being a sulfur compound
• CPC Class Codes: C01B 2203/0888 by evaporation of a fluid
• CPC Class Codes: C01B 2203/0894 Generation of steam
• CPC Class Codes: C01B 2203/147 Three or more purification steps in series
• CPC Class Codes: C01B 2203/148 involving a recycle stream to the feed of the process for making hydrogen or synthesis gas
• CPC Class Codes: C01B 2203/84 Energy production
• CPC Class Codes: C01B 2203/86 Carbon dioxide sequestration
• CPC Class Codes: C01B 3/16 using catalysts
• CPC Class Codes: C01B 3/36 using oxygen or mixtures containing oxygen as gasifying agents
• CPC Class Codes: C01B 3/382 : Multi-step processes
• CPC Class Codes: C01B 3/386 : Catalytic partial combustion
• CPC Class Codes: C10J 2300/093 : Coal
• CPC Class Codes: C10J 2300/0973 : Water
• CPC Class Codes: C10J 2300/0986 : Catalysts
• CPC Class Codes: C10J 2300/1662 : to methane
• CPC Class Codes: C10J 2300/1807 : Recycle loops, e.g. gas, solids, heating medium, water
• CPC Class Codes: C10J 2300/1884 : with one stream being synthesis gas
• CPC Class Codes: C10J 2300/1892 : with one stream being water/steam
• CPC Class Codes: C10J 3/00 : Production of combustible gases containing carbon monoxide from solid carbonaceous fuels destructive distillation processes C10B
• CPC Class Codes: C10K 1/004 : Sulfur containing contaminants, e.g. hydrogen sulfide
• CPC Class Codes: C10K 1/005 : Carbon dioxide
• CPC Class Codes: C10L 3/08 : Production of synthetic natural gas
• CPC Class Codes: Y02P 30/00 : Technologies relating to oil refining and petrochemical industry

Abstract

The present invention relates to a 2-mode processes for preparing gaseous products, and in particular a hydrogen product stream, via the hydromethanation of carbonaceous feedstocks in the presence of steam, carbon monoxide, hydrogen and a hydromethanation catalyst in a first mode, and a partial oxidation of methane in a second mode.

Claims

1. A process for generating a hydrogen product stream, the process comprising a first hydrogen production mode and a second hydrogen production mode, wherein the second hydrogen production mode is utilized when the first hydrogen production mode is not operating, wherein the first hydrogen production mode comprises the steps of:

(a) supplying to a hydromethanation reactor (1) a carbonaceous feedstock, (2) a hydromethanation catalyst, (3) a steam stream, (4) a feed gas stream and (5) optionally a first oxygen-rich gas stream;

(b) reacting the carbonaceous feedstock in the hydromethanation reactor in the presence of carbon monoxide, hydrogen, steam, hydromethanation catalyst and optionally oxygen, to produce a methane-enriched raw product stream comprising methane, carbon monoxide, hydrogen, carbon dioxide, hydrogen sulfide and heat energy;

(c) withdrawing the methane-enriched raw product stream from the hydromethanation reactor;

(d) introducing the methane-enriched raw product stream into a first heat exchanger unit to remove heat energy from the methane-enriched raw product stream;

(e) sour shifting at least a predominant portion of the carbon monoxide in the methane-enriched raw product stream in a sour shift unit to produce a hydrogen-enriched raw product stream comprising hydrogen, methane, carbon dioxide, hydrogen sulfide and optionally carbon monoxide;

(f) removing a substantial portion of the carbon dioxide and a substantial portion of the hydrogen sulfide from the hydrogen-enriched raw product stream in an acid gas removal unit to produce a sweetened gas stream comprising a substantial portion of the hydrogen, methane and carbon monoxide (if present) from the hydrogen-enriched raw product stream;

(g) separating at least a predominant portion of the hydrogen from the sweetened gas stream in a hydrogen separation unit to produce (1) the hydrogen product stream and (2) a hydrogen-depleted sweetened gas stream comprising methane, carbon monoxide (if present in the sweetened gas stream) and optionally hydrogen;

(h) optionally splitting the hydrogen-depleted sweetened gas stream into a recycle gas stream and a methane-rich product gas stream;

(i) supplying at least a portion of the hydrogen-depleted sweetened gas stream (or the recycle gas stream if present), a second oxygen-rich gas stream and an optional supplemental methane gas stream to a partial oxidation reactor; and

(j) reacting the supplied hydrogen-depleted sweetened gas stream (or the supplied recycle gas stream if present) and the supplied supplemental methane gas stream (if present) with oxygen in the partial oxidation reactor to generate heat energy and the feed gas stream, wherein the feed gas steam comprises carbon monoxide, hydrogen and steam,

wherein the reaction in step (b) has a syngas demand, and the amount of the hydrogen-depleted sweetened gas stream (or the recycle gas stream if present) supplied to the partial oxidation reactor is at least sufficient to generate enough carbon monoxide and hydrogen in the feed gas stream to at least meet the syngas demand of the reaction in step (b); and

wherein the second hydrogen production mode comprises the steps of;

(1) supplying the supplemental methane gas stream and the second oxygen-rich gas stream to the partial oxidation reactor;

(2) reacting the supplied supplemental methane gas stream with oxygen in the partial oxidation reactor to generate heat energy and a supplemental gas stream comprising carbon monoxide, hydrogen and steam;

(3) introducing the supplemental gas stream into a heat exchanger unit to remove heat energy from the supplemental gas stream;

(4) sour shifting at least a substantial portion of the carbon monoxide in the supplemental gas stream in a sour shift unit to produce a hydrogen-enriched supplemental gas stream comprising hydrogen and carbon dioxide;

(5) removing a substantial portion of the carbon dioxide from the hydrogen-enriched supplemental gas stream in an acid gas removal unit to produce a hydrogen gas stream comprising a substantial portion of the hydrogen from the hydrogen-enriched supplemental gas stream; and

(6) purifying the hydrogen gas stream in a hydrogen separation unit to produce the hydrogen product stream.

2. The process of claim 1, wherein the partial oxidation reactor is a non-catalytic partial oxidation reactor.

3. The process of claim 1, wherein the partial oxidation reactor is a catalytic partial oxidation reactor.

4. The process of claim 1, wherein in the first hydrogen production mode step (h) is present.

5. The process of claim 1, wherein in the first hydrogen production mode step (h) is not pre-sent.

6. The process of claim 1, wherein in the first hydrogen production mode the reaction in step (b) has a steam demand;

the carbonaceous feedstock optionally comprises a moisture con-tent;

the first oxygen-rich gas stream, if present, optionally comprises steam;

the steam demand is substantially satisfied by the steam stream, steam contained in the feed gas stream, the moisture content (if present) of the carbonaceous feedstock, and (if present) steam in the first oxygen-rich gas stream;

in the first hydrogen production mode the reaction in step (b) has a heat demand; and

the steam stream and the feed gas stream as fed into the hydromethanation reactor comprise heat energy that, in combination, is sufficient to at least meet the heat demand of the reaction in step (b).

7. The process of claim 1, wherein in the first hydrogen production mode the first oxygen-rich gas stream is supplied periodically or continuously to the hydromethanation reactor.

8. The process of claim 1, wherein in the first hydrogen production mode a char by-product is generated in step (b), the char by-product is periodically or continuously withdrawn from the hydromethanation reactor, and at least a portion of the withdrawn by-product char is provided to a catalyst recovery operation.

9. The process of claim 1, wherein in the first hydrogen production mode the heat energy removed in step (d) is used at least in part to generate process steam.

10. The process of claim 9, wherein in the first hydrogen production mode the feed gas stream is passed through a second heat exchanger unit to remove heat energy prior to introduction into the hydromethanation reactor.

11. The process of claim 10, wherein in the first hydrogen production mode the heat energy removed from the feed gas stream is used at least in part to generate process steam.

12. The process claim 11, wherein in the first hydrogen production mode the steam stream is substantially made up from process steam.

13. The process of claim 1, wherein in the first hydrogen production mode the recycle gas stream comprises from about 34 wt % up to about 60 wt % of the sweetened gas stream (or the hydrogen-depleted sweetened gas stream if present, or the methane-enriched sweetened gas stream if present, or the methane-enriched split gas feed stream if present).

14. The process of claim 1, wherein in the first hydrogen production mode the hydro-methanation catalyst comprises an alkali metal hydromethanation catalyst, the carbonaceous feedstock is loaded with a hydromethanation catalyst prior to introduction into the hydro-methanation reactor, and the carbonaceous feedstock is loaded with an amount of an alkali metal hydromethanation catalyst sufficient to provide a ratio of alkali metal atoms to carbon atoms ranging from about 0.01 to about 0.10.

15. The process of claim 1, wherein the heat exchanger unit used in the second hydrogen production mode is also used in the first hydrogen production mode.

16. The process of claim 1, wherein the sour shift unit used in the second hydrogen production mode is also used in the first hydrogen production mode.

17. The process of claim 1, wherein the acid gas removal unit used in the second hydrogen production mode is also used in the first hydrogen production mode.

18. The process of claim 1, wherein the hydrogen separation unit used in the second hydrogen production mode is also used in the first hydrogen production mode.

19. The process of claim 1, wherein the heat exchanger unit, sour shift unit, acid gas removal unit and hydrogen separation unit used in the second hydrogen production mode are also used in the first hydrogen production mode.

20. The process of claim 1, wherein when the first hydrogen production mode is operating, steps (a), (b), (c), (d), (e), (f), (g), (i), (j) and (k), and when present (h), are operated in a continuous manner, and when the second hydrogen production mode is operating, steps (1), (2), (3), (4), (5) and (6) are operated in a continuous manner.