Hydromethanation of a carbonaceous feedstock

• US 9,353,322 B2
• Filed: 10/28/2011
• Issued: 05/31/2016
• Est. Priority Date: 11/01/2010
• Status: Active Grant

• Current Assignee: Sure Champion Investments Limited
• Original Assignee: GreatPoint Energy, Inc.
• Inventors: Raman, Pattabhi K., Jiradilok, Veeraya, Robinson, Earl T., Sirdeshpande, Avinash
• Primary Examiner(s): Bullock, In Suk
• Assistant Examiner(s): Fadhel, Ali Z
• Application Number:
  US13/284,139
• Publication Number:
  US 20120102836A1
• Time in Patent Office: 1,677 Days
• Field of Search: None
• US Class Current: 1/1
• CPC Class Codes: C01B 2203/0283 containing a CO-shift step, i.e. a water gas shift step
• 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 2203/042 Purification by adsorption on solids
• 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 2203/0465 Composition of the impurity
• 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 2203/0495 the impurity being water
• CPC Class Codes: C01B 2203/147 Three or more purification steps in series
• CPC Class Codes: C01B 3/586 the reaction being a methanation reaction
• CPC Class Codes: C01B 32/40 Carbon monoxide
• CPC Class Codes: C01B 32/50 Carbon dioxide
• 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 2300/1807 Recycle loops, e.g. gas, solids, heating medium, water
• CPC Class Codes: C10J 2300/1838 Autothermal gasification by injection of oxygen or steam
• CPC Class Codes: C10J 3/463 : in stationary fluidised beds
• CPC Class Codes: C10L 3/08 : Production of synthetic natural gas

Abstract

The present invention relates to processes for hydromethanating a carbonaceous feedstock to a methane-enriched synthesis gas, where an oxygen-rich gas stream and the carbonaceous feedstock are fed into a fluidized-bed hydromethanation reactor at a specified zone in order to assist in heat management within the hydromethanation reactor.

Claims

1. A process for generating a methane-enriched raw product gas stream from a non-gaseous carbonaceous material, the process comprising the steps of:

(a) supplying to a hydromethanation reactor

(1) a carbonaceous feedstock derived from the non-gaseous carbonaceous material,

(2) a hydromethanation catalyst,

(3) a superheated steam stream and

(4) an oxygen-rich gas stream,

wherein the hydromethanation reactor comprises a fluidized bed having a upper portion above a lower portion, and a zone below the fluidized bed, said zone being separated from the fluidized bed by a divider, and wherein the superheated steam stream and the oxygen-rich gas stream are introduced into the lower portion of the fluidized bed;

(b) reacting a portion of the carbonaceous feedstock in the hydromethanation reactor in the presence of hydromethanation catalyst, carbon monoxide, hydrogen and steam at a target operating temperature of at least about 1000°

F. (about 538°

C.) to about 1400°

F. (about 760°

C.), to produce a methane-enriched raw gas and a solid by-product char, wherein the methane-enriched raw gas comprises methane, carbon monoxide, hydrogen, carbon dioxide, hydrogen sulfide, steam, heat energy and entrained fines; and

(c) reacting a portion of the carbonaceous feedstock with oxygen to produce carbon monoxide, hydrogen and heat energy;

wherein;

(i) the reaction of step (b) predominates in the upper portion of the fluidized bed;

(ii) the reaction of step (c) predominates in the lower portion of the fluidized bed;

(iii) the carbonaceous feedstock is supplied to the hydromethanation reactor into the lower portion of the fluidized bed in close proximity to the divider, and

(iv) the methane-enriched raw product stream comprises at least about 18 mol % methane (based on the moles of methane, carbon dioxide, carbon monoxide and hydrogen in the methane-enriched raw product stream).

2. The process of claim 1, wherein the carbonaceous feedstock is supplied to the hydromethanation at a feed location, a char by-product is generated by the reactions of steps (b) and (c), and char by-product is continuously or periodically withdrawn from the hydromethanation reactor at a withdrawal point above the feed point of the carbonaceous feedstock.

3. The process of claim 2, wherein char by-product is periodically or continuously withdrawn from the upper portion of the fluidized bed.

4. The process of claim 1, wherein the carbonaceous feedstock as fed to the hydromethanation reactor contains a moisture content of from greater than 10 wt % to about 25 wt % (based on the total weight of the carbonaceous feedstock), to the extent that the carbonaceous feedstock is substantially free-flowing.

5. The process of claim 1, wherein the reaction of step (b) has a syngas demand and a heat demand, and the syngas demand, and the heat demand and syngas demand are substantially satisfied by the reaction of step (c).

6. The process of claim 1, wherein the reaction of step (b) has a steam demand, and the steam demand is substantially satisfied by steam in the superheated steam stream, the oxygen-rich gas stream and the fines stream fed into the lower portion of the fluidized bed, and steam generated from the carbonaceous feedstock.

7. The process of claim 1, wherein the superheated steam stream, the oxygen-rich gas stream, the carbonaceous feedstock and the hydromethanation catalyst are introduced into the hydromethanation reactor at a temperature below the target operating temperature of the reaction of step (b).

8. The process of claim 1, wherein the superheated steam stream is fed to the hydromethanation reactor at a temperature of from about 500°

F. (about 260°

C.) to about 950°

F. (about 510°

C.).

9. The process of claim 1, wherein the superheated steam stream and the oxygen-rich stream are combined for feeding into the lower portion of the fluidized bed of the hydromethanation reactor, and the temperature of the combined stream is from about from about 500°

F. (about 260°

C.) to about 900°

F. (about 482°

C.).

10. The process of claim 1, wherein the methane-enriched raw product stream is introduced into a first heat exchanger unit to recover heat energy and generate a cooled methane-enriched raw product stream.

11. The process of claim 10, wherein the heat energy recovered in the first heat exchanger unit is used to generate a first process steam stream, and superheat the first process steam stream for use as all or a part of the superheated steam stream for introduction into the hydromethanation reactor.

12. The process of claim 10, wherein at least a portion of the carbon monoxide in the cooled methane-enriched raw product stream is steam shifted to generate heat energy and a hydrogen-enriched raw product stream;

the hydrogen-enriched raw product stream is substantially dehydrated to generate a dehydrated hydrogen-enriched raw product stream;

a substantial portion of the carbon dioxide and a substantial portion of the hydrogen sulfide are removed from the dehydrated hydrogen-enriched raw product stream to produce a sweetened gas stream comprising a substantial portion of the hydrogen, carbon monoxide (if present in the dehydrated hydrogen-enriched raw product stream) and methane from the dehydrated hydrogen-enriched raw product stream; and

carbon monoxide and hydrogen present in the sweetened gas stream are reacted in a catalytic methanator in the presence of a methanation catalyst to produce heat energy and a methane-enriched sweetened gas stream.

13. The process of claim 12, wherein heat energy is recovered from the steam shifting, and at least a portion of the recovered heat energy is utilized to preheat boiler feed water for use in generating process steam.

14. The process of claim 12, wherein heat energy from the catalytic methanation is recovered and at least a portion of the recovered heat energy is utilized to generate and superheat a second process steam stream.

15. The process of claim 14, wherein the heat energy recovered in the first heat exchanger unit is used to generate a first process steam stream, and superheat the first process steam stream for use as all or a part of the superheated steam stream for introduction into the hydromethanation reactor.

16. The process of claim 15, wherein the superheated steam stream substantially comprises steam from the first process steam stream and the second process steam stream.

17. The process of claim 15, wherein the process is steam neutral or steam positive.

18. The process of claim 1, wherein there is no fuel-fired superheater used to superheat the steam fed to the hydromethanation reactor during steady-state operation of the process.