Fuel cell integrated with steam reformer

• US 4,670,359 A
• Filed: 06/10/1985
• Issued: 06/02/1987
• Est. Priority Date: 06/10/1985
• Status: Expired due to Fees

• Current Assignee: United States Of America As Represented By The Department Of Energy
• Original Assignee: Engelhard Corporation (BASF SE)
• Inventors: Whelan, James A., Beshty, Bahjat S.
• Primary Examiner(s): Skapars, Anthony
• Application Number:
  US06/743,714
• Time in Patent Office: 722 Days
• Field of Search: 429/20, 429/26, 429/19, 429/17, 429/40, 423/650
• US Class Current: 429/424
• CPC Class Codes: B01B 1/005 Evaporation for physical or chemical purposes; Evaporation apparatus therefor, e.g. evaporation of liquids for gas phase reactions
• CPC Class Codes: C01B 3/323 Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
• CPC Class Codes: H01M 8/06 Combination of fuel cells with means for production of reactants or for treatment of residues regenerative fuel cells H01M8/18
• CPC Class Codes: Y02E 60/50 Fuel cells

Abstract

A H₂ -air fuel cell integrated with a steam reformer is disclosed wherein a superheated water/methanol mixture is fed to a catalytic reformer to provide a continuous supply of hydrogen to the fuel cell, the gases exhausted from the anode of the fuel cell providing the thermal energy, via combustion, for superheating the water/methanol mixture.

Claims

1. A process of providing a continuous supply of hydrogen fuel to a fuel cell system, the system being comprised of a heat exchanger, a burner, a catalytic reactor containing a catalyst bed for catalyzing the production of hydrogen from a gaseous mixture of water and methanol and a fuel cell comprised of a fuel electrode, an oxygen electrode and an electrolyte disposed therebetween, the process comprising the steps of:

(a) passing a gaseous mixture consisting essentially of water and methanol to the heat exchanger to heat the mixture to a superheated state, the temperature and composition of the superheated mixture being sufficient to supply at least about 90% of the heat required for reforming the methanol contained in said mixture by condensation,

(b) passing the superheated gaseous mixture of water and methanol into the catalytic reactor to form hydrogen by an endothermic reaction of water and methanol over the catalyst bed, the catalytic reactor being in the form of a tube having a length to diameter ratio of from about 2 to about 6, said catalyst bed comprising a low activity, high stability zinc oxide and chromium oxide catalyst comprised of about 30 to 65 percent by weight Zn and about 5 to 35 percent by weight Cr, followed by a high activity zinc oxide and copper oxide catalyst on alumina comprised of about 5 to 20 percent by weight Zn, about 15 to 40 percent by weight Cu, and about 15 to 50 percent by weight alumina, the temperature of said superheated mixture being between about 425° and

about 600°

C. and the water to methanol ratio being between about 2 and about 9,

(c) directing hydrogen produced in step (b) to the fuel electrode of the fuel cell,

(d) directing air into the oxygen electrode of the fuel cell to effect an electrochemical reaction to produce electricity,

(e) exhausting the gaseous effluent from the fuel electrode, a portion of which is a combustible gas, burning the combustible portion of the fuel electrode exhaust in the burner, feeding the burner exhaust to the heat exchanger to supply heat for the superheating of the water and methanol in step (a) whereby the gases exhausted from the fuel electrode supply at least a major portion of the thermal energy, via combustion, to heat the water/methanol mixture to the superheated state.

2. A process of providing a continuous supply of hydrogen fuel to a fuel cell system, the system being comprised of a heat exchanger, a burner, a catalytic reactor containing a catalyst bed for catalyzing the production of hydrogen from a gaseous mixture consisting essentially of water and methanol and a fuel cell comprised of a fuel electrode, an oxygen electrode and an electrolyte disposed therebetween, the process comprising the steps of:

(a) passing a gaseous mixture of water and methanol to the heat exchanger to heat the mixture to a superheated state, the temperature and composition of the superheated mixture being sufficient to supply at least about 75% of heat required for reforming the methanol contained in said mixture by condensation,

(b) passing the superheated gaseous mixture of water and methanol into the catalytic reactor to form hydrogen by an endothermic reaction of water and methanol over the catalyst bed, the catalytic reactor being in the form of a simple tube having a length to diameter ratio of less than about 10 to 1,

(c) directing hydrogen produced in step (b) to the fuel electrode of the fuel cell,

(d) directing air into the oxygen electrode of the fuel cell to effect an electrochemical reaction to produce electricity,

(e) exhausting the gaseous effluent from the fuel electrode, a portion of which is a combustible gas, burning the combustible portion of the fuel electrode exhaust in the burner, feeding the burner exhaust to the heat exchanger to supply heat for the superheating of the water and methanol in step (a) whereby the gases exhausted from the fuel electrode supply the thermal energy, via combustion, to heat the water/methanol mixture to the superheated state.

3. The process of claim 2 wherein a portion of the catalytic reactor exhaust is comprised of water which is condensed and recycled for use in the catalytic steam reforming reaction.

4. The process of claim 2 wherein the water/methanol mixture is superheated to a temperature between about 800°

and about 1100°

F.

5. The process of claim 2 wherein the water/methanol mixture is superheated to a temperature of about 850°

to about 1000°

F.

6. The process of claim 2 wherein the water/methanol molar ratio in the superheated gaseous mixture is between about 2 to about 9.

7. The process of claim 2 wherein the fuel cell electrolyte is phosphoric acid.

8. The process of claim 2 wherein the catalyst in the catalyst bed is a combination of zinc and chromium oxides on alumina.

9. The process of claim 2 wherein the catalyst bed comprises a low activity, high stability zinc oxide and chromium oxide catalyst comprised of about 40 to 65 percent by weight Zn and about 10 to 30 percent by weight Cr, followed by a high activity zinc oxide and copper oxide catalyst on alumina comprised of about 5 to 20 percent by weight Zn, about 20 to 35 percent by weight Cu, and about 20 to 40 percent by weight alumina.

10. A process of providing a continuous supply of hydrogen fuel to a fuel cell system, the system being comprised of a heat exchanger, a burner, a catalytic reactor containing a catalyst bed for catalyzing the production of hydrogen from a gaseous mixture consisting essentially of water and methannol and a fuel cell comprised of a fuel electrode, an oxygen electrode and an electrolyte disposed therebetween, the process comprising the steps of:

(a) passing a gaseous mixture of water and methanol to the heat exchanger to heat the mixture to a superheated state,

(b) passing the superheated gaseous mixture of water and methanol into the catalytic reactor to form hydrogen by an endothermic reaction of water and methanol over the catalyst bed, the degree of superheat provided in step (a) supplying a major portion of the endothermic heat of reaction required therefor,

(c) directing hydrogen produced in step (b) to the fuel electrode of the fuel cell,

(d) directing air into the oxygen electrode of the fuel cell to effect an electrochemical reaction to produce electricity,

(e) exhausting the gaseous effluent from the fuel electrode, a portion of which is a combustible gas, burning the combustible portion of the fuel electrode exhaust in the burner, feeding the burner exhaust to the heat exchanger to supply heat for the superheating of the water and methanol in step (a) whereby the gases exhausted from the fuel electrode supply the thermal energy, via combustion, to heat the water/methanol mixture to the superheated state.

11. The process of claim 10 wherein a portion of the catalytic reactor exhaust is comprised of water which is condensed and recycled for use in the catalytic steam reforming reaction.

12. The process of claim 10 wherein the water/methanol mixture is superheated to a temperature between about 800°

and about 1100°

F.

13. The process of claim 10 wherein the water/methanol mixture is superheated to a temperature of about 850°

to about 1000°

F.

14. The process of claim 10 wherein the water/methanol molar ratio in the superheated gaseous mixture is between about 2 to about 9.

15. The process of claim 10 wherein the fuel cell electrolyte is phosphoric acid.

16. The process of claim 10 wherein the catalyst in the catalyst bed is a combination of zinc and chromium oxides on alumina.

17. The process of claim 10 wherein the catalyst bed comprises a low activity, high stability zinc oxide and chromium oxide catalyst comprised of about 40 to 65 percent by weight Zn and about 10 to 30 percent by weight Cr, followed by a high activity zinc oxide and copper oxide catalyst on alumina comprised of about 5 to 20 percent by weight Zn, about 20 to 35 percent by weight Cu, and about 20 to 40 percent by weight alumina.