CA1176306A - Apparatus and method for producing high pressure steam in a fuel cell system - Google Patents
Apparatus and method for producing high pressure steam in a fuel cell systemInfo
- Publication number
- CA1176306A CA1176306A CA000394010A CA394010A CA1176306A CA 1176306 A CA1176306 A CA 1176306A CA 000394010 A CA000394010 A CA 000394010A CA 394010 A CA394010 A CA 394010A CA 1176306 A CA1176306 A CA 1176306A
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- CA
- Canada
- Prior art keywords
- gas
- process gas
- fuel
- exhausted
- fuel cell
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
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Classifications
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
- H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
Abstract
ABSTRACT
High pressure steam is generated in a fuel cell system utilizing a quantity of process gas which has been exhausted from the system fuel cell and whose temperature has been raised through heat exchange with a higher tem-perature gas generated elsewhere in the fuel cell system.
High pressure steam is generated in a fuel cell system utilizing a quantity of process gas which has been exhausted from the system fuel cell and whose temperature has been raised through heat exchange with a higher tem-perature gas generated elsewhere in the fuel cell system.
Description
~ ~763~6 I Background of the Invention This invention pertains to fuel cell systems and, in particular, to fuel cell systems which utilize steam. I
Fuel cell systems often ukilize high pressure S ! steam for reforming reaction (fuel processing) and for use as process steam for waste heat utilization. In reforming reaction, the steam is combined with a hydrocarbon fuel and the combination applied to a reformer which provides at its output fuel process gas to be used in the fuel cell or fuel cell stack of the system~
U.S. patent 3,969,145 discloses one steam generating ¦ practice wherein use is made of the heated oxidant and fuel ¦ process gases passing through the system fuel cell. Metallic ¦ tubes carrying coolant water are situated internal to the ¦ cell stack and in heat exchanging relationship with the ¦ respective flows of fuel and oxidant gases. The water in ¦ the tubes is thereby heated to produce steam which is also simultaneously heated in the same manner. The steam is then removed from the tubes and used elsewhere in the system as, for example, in steam reforming reaction of the type des-cribed above.
It has also been proposed to use the exhausted oxidant gas of the fuel cell system itself for steam genera-tion external to the cell. In this case, the exhausted oxidant gas and water are supplied to a heat exchangPr with the resultant production of steam.
In both the above practices, increased fuel cell temperature is required to provide a desired amount of steam at increased pressures. This can be seen from the equation governing the ratio of generated steam to generating fuel 1 ~ 76306 1 cell gas which is as follows-Q = b/hr steam ~ ~H
where QH is ~he latent heat of s~eam Cp is the heat capacity of gas to is the initial temperature of S the gas tp is a tempera~ure equal to the steam saturation temperature ts which increases with desired steam pressure plus a small differential td referred to as the pinch point.
Assuming that the gas stream is at a temperature of 375F
and that steam ~t 105 psia is required (this corresponds to ts = 332F and QH = 885 Btu/lb~ and further that a differential td = 20F is used and Cp = 0.28 Btu/lb F, then the ratio Q
is calculated as follows:
Q = 0.28 (375 ~ 352) , 885 lS Q = 0.007 For steam at a pressure above 1~ psia, the value of tp is increased while the values of ~H and Cp remain sub-stantially the same. As a result, to obtain at the higher l pressure the same quantity of steam as obtained at the 105 l psia level, the value of the fuel gas temperature to must be increased by the amount of the increase in the value tp.
This of course requires an increase in fuel cell operating temperature.
At steam pressures of the order of 100 to 180 psi, ¦ which pressures are desirable for many fuel cell systems or for many industrial process steam applications, the required increase in fuel cell tempera~ure over con~entional temperatures is such as to measurably decrease fuel cell life. As a l result, use of the aforesaid practices to pxovide steam at ¦ these high pressures is undesirable.
Z !176306 1 one possible alternative to providing the increased pressure steam without raising fuel cell temperature, would : be to use a compressGr. However, this alternative is undesirable because of cost and power requirement considerations.
It is therefore an object of the present invention f to provide a fuel cell system having an improved capability for generating steam.
` It is a further object of the present invention to provide a fuel cell system capable of providing a given amount of steam at increasing pressu~es and useable for process gas reforming without having to increase fuel cell temperature.
Summary of the Invention In accordance with the principles of the present invention, the above and other objectives are realized in a fuel cell system wherein process gas exhausted from the fuel cell of the system is heated to a temperature sufficient to produce a predetermined amount of steam at a predetenmined pressure by gas at a higher tempera~ture generated elsewhere in the system. The heating of the exhausted process gas occurs in a heat exchanger external to the cell and the resultant gas is then utilized to produce the desired steam.
In the preferred form of the invention, the fuel cell is operated with excess process gas for cooling the cell to a desired operating temperature and the exhausted cooling process gas is used for steam generation. In still further preferred form, excess oxidant gas is utilized for fuel cell cooling and exhausted oxidant gas for steam generation.
Description ~f_ b- D~_~.Ue~
The above and other features and spects of the ~ il76306 1 present invention will become more apparent upon reading the following detailed description in conjunction with the accompanying sole drawing which shows a fuel cell system in accordance with the principles of the present invention.
Detailed Description In F~G. 1, the fuel cell system 1 comprises a fuel cell 2 which, preferably, is a phosphoric acid cell, although the principles of the invention extend to other cell types such as, for example, molten carbonate cells and solid oxide cells. An anode section 3 and a cathode section 4 communicating with an electrolyte section 50 receive respective fuel process gas and oxidant process gas along input lines 5 and 6, respectively. In conventional practice, the fuel and oxidant gases are at substantially the same pressure which might, typically, be in the range of 30 to 150 psia, so as to promote fuel cell efficiency. Also, in the present illustrative example/ the flow of oxidant process gas is further of an amount in excess of that re~uired for electro-chemical reaction, the excess gas being of a quantity sufficient to cool the fuel cell to a predetermined temperature promotive of desired fuel cell lie.
The oxidant process gas is derived from a compressor section 7 of a turbocompressor unit 10, the compressor 7 raising the pressure of the oxidant gas from a supply 8 to the desired pressure. The fuel process gas is derived from a reformer 9 which receives from a common line 11 a mixture of preheated hydrocarbon fuel and steam coupled to the line 11 by respective lines 12 and 13. ~he hydrocarbon fuel is provided to the line 12 from a compressor section 14 of the turbocompressor 10, the section being fed from a fuel supply ! ~76306 1 15. A pre-heater in the form of a heat exchanger 16 situated in the line 12 preheats the fresh fuel pxior to coupling to the common line 11.
In order for the fuel process gas produced by the reformer 9 to be at the desired pressure, the steam provided to the line 11 from the line 13 must be at least at that pressure, since the steam pressure controls the resultant fuel process gas pressure. Perferably, the steam pressure should be higher than the required fuel process gas pressure, in order to account for pressure losses in the reformer and in the lines carrying the gas to the anode section 3.
Additionally, to prevent carbon formation in the reformer, a certain ratio of steam to fuel is required. For example, with liquid naptha as a fuel, a ratio of 4 moles steam to 1 lS mole carbon is desirable. Preferably, that amount of steam should be at a pressure above the fuel gas pressure.
In accordance with the principles of the present invention, steam at the desired pressure and of a desired amount is generated in the fuel cell system utilizing a quantity of excess oxidant gas exhausted from the cathode section 4 and, therefore, at the predetermined fuel cell temperature, and a further quantity of higher temperature gas derived from elsewhere in the fuel cell system. These gases are carried via lines 18 and 21 to an auxiliary heater or heat exchanger 17, the temperature of the higher temperature gas being sufficient to raise the temperature of the quantity of oxidant gas to that required to produce the desired amount of steam at the desired pressure. The increased temperature oxidant gas is, ~hereafter, applied to a steam generator in the form of a heat exchanger 22 having a pressure ~ ~6306 1 valve for allowing steam issuance at the desired pressure.
Water from a supply 23 is coupled to the generator 22 and is raised therein to steam at such pressure, the steam then being coupled to the generator output line 24 which feeds steam line 13.
As above indicated, the higher temperature gas in the line 21 is obtained from gas dexived in the fuel cell system from elsewhere than the fuel cell 2. As shown in dotted line, such gas may be obtained by passage of a portion of the unburned anode gas exhausted into anode exhaust line 25 through a burner 41, thereby producing gas at a signifi-cantly higher temperature than the cell operating temperature.
Other gases which also can be used as the higher temperature gas will be pointed out below in the discussion of the remainder of the system 1.
The reformer 9 is provided with reaction heat from a burner 26 which burns a combination of preheated fresh supply fuel, exhausted fuel gas and compressed oxidant : supply gas. The latter gases are coupled to the burner 26 via lines 27 and 28, respectively in which are situated heat exchangers 29 and 31 for raising the temperatures of the respective gases. The latter exchangers are in stacked relationship with the reformer 9 and the burner 26 and are heated by the burner gas~ The burner gas is thereafter coupled via line 32 to an exit line 33 which also receives a quantity of exhausted oxidant process gas from the line 19.
The gas in the line 33 is expanded in a turboexpander section 42 o the turbocompressor 10 and is exhausted from the system via line 34. As indicated in dotted line, the gas in line 34 also can be coupled to line 21 for providing gas for - I 1763~6 1 ¦ heating the exhausted oxidant gas coupled to the heat exchanger 1 17.
¦ The combi~ed fuel and steam in the line 11 is pre-heated prior to application to reformer 9 via a heat exchanger 35 to which is also applied the outgoing fuel process gas generated by the reformer. The latter gas is thereafter cooled by passage via line 36 through heat exchanger 16 and a high temperature low temperature shift converter 37, the high temperature converter of which includes a heat exchanger section 38.for heat exchange with the steam in the line 13 prior to coupling to ~he line 11 and the low temperature converter of which includes a heat exchanger section 39 to which is coupled water from a further water supply 43.
The fuel process gas is brought to an intermediate temperature by the converter 37 and, as shown, in dotted line, the gas at the output line 44 of the converter is also suitable for coupling -to the line 21 for application to the heat exchanger 17 for heating the exhausted oxidant gas coupled thereto. A further heat exchanger 45 in the line 44 receives the intermediate temperature fuel ~rocess gas and water from a supply 45 further lowering the temperature of same to the predetermined cell temperature for application to the line 5 feeding anode section 3.
As can be appreciated, the degree to which the tempèrature of the exhausted oxidant gas applied to the heat exchanger 17 is to be r~ised and, thus, the temperature of the higher temperature gas, as well as the amount of exhausted oxidant gas supplied will depend upon the desired pressure and amount of steam to be produced. The latter, in turn, will depend upon system requirements including, amongst ~ ~ 76306 1 ¦ other things, ~he desired fuel cell pressure and operating ¦ temperature, as well as the quantity and pressure of steam ¦ required in the reformer 9. The particular values of these ¦ parameters will of course depend upon each individual applica-S ¦ tion.
In a typical situation of a phosphoric acid fuel cell stack at an operating temperature of 375F and fuel and oxidant gases at pressures of approximately 50 psia, and a reformer requiring a steam flow of 1.8 lb , the quantity of exhaust oxidant gas delivered to heat exchanger 17 might be 205 lb . In such case, the temperature of the further hr-kw gas delivered to heat exchanger might be 500 to 1500F, thereby raising the oxidant gas to a temperature of approximately 400F. Production of this further gas at such tempera~ure might, in turn, be realized by burning exhausted fuel gas.
Alternatively, a similar flow of fuel gas at such temperature from the converter 37 or from the line 34 might also be used.
In all cases, it is understood that the above-
Fuel cell systems often ukilize high pressure S ! steam for reforming reaction (fuel processing) and for use as process steam for waste heat utilization. In reforming reaction, the steam is combined with a hydrocarbon fuel and the combination applied to a reformer which provides at its output fuel process gas to be used in the fuel cell or fuel cell stack of the system~
U.S. patent 3,969,145 discloses one steam generating ¦ practice wherein use is made of the heated oxidant and fuel ¦ process gases passing through the system fuel cell. Metallic ¦ tubes carrying coolant water are situated internal to the ¦ cell stack and in heat exchanging relationship with the ¦ respective flows of fuel and oxidant gases. The water in ¦ the tubes is thereby heated to produce steam which is also simultaneously heated in the same manner. The steam is then removed from the tubes and used elsewhere in the system as, for example, in steam reforming reaction of the type des-cribed above.
It has also been proposed to use the exhausted oxidant gas of the fuel cell system itself for steam genera-tion external to the cell. In this case, the exhausted oxidant gas and water are supplied to a heat exchangPr with the resultant production of steam.
In both the above practices, increased fuel cell temperature is required to provide a desired amount of steam at increased pressures. This can be seen from the equation governing the ratio of generated steam to generating fuel 1 ~ 76306 1 cell gas which is as follows-Q = b/hr steam ~ ~H
where QH is ~he latent heat of s~eam Cp is the heat capacity of gas to is the initial temperature of S the gas tp is a tempera~ure equal to the steam saturation temperature ts which increases with desired steam pressure plus a small differential td referred to as the pinch point.
Assuming that the gas stream is at a temperature of 375F
and that steam ~t 105 psia is required (this corresponds to ts = 332F and QH = 885 Btu/lb~ and further that a differential td = 20F is used and Cp = 0.28 Btu/lb F, then the ratio Q
is calculated as follows:
Q = 0.28 (375 ~ 352) , 885 lS Q = 0.007 For steam at a pressure above 1~ psia, the value of tp is increased while the values of ~H and Cp remain sub-stantially the same. As a result, to obtain at the higher l pressure the same quantity of steam as obtained at the 105 l psia level, the value of the fuel gas temperature to must be increased by the amount of the increase in the value tp.
This of course requires an increase in fuel cell operating temperature.
At steam pressures of the order of 100 to 180 psi, ¦ which pressures are desirable for many fuel cell systems or for many industrial process steam applications, the required increase in fuel cell tempera~ure over con~entional temperatures is such as to measurably decrease fuel cell life. As a l result, use of the aforesaid practices to pxovide steam at ¦ these high pressures is undesirable.
Z !176306 1 one possible alternative to providing the increased pressure steam without raising fuel cell temperature, would : be to use a compressGr. However, this alternative is undesirable because of cost and power requirement considerations.
It is therefore an object of the present invention f to provide a fuel cell system having an improved capability for generating steam.
` It is a further object of the present invention to provide a fuel cell system capable of providing a given amount of steam at increasing pressu~es and useable for process gas reforming without having to increase fuel cell temperature.
Summary of the Invention In accordance with the principles of the present invention, the above and other objectives are realized in a fuel cell system wherein process gas exhausted from the fuel cell of the system is heated to a temperature sufficient to produce a predetermined amount of steam at a predetenmined pressure by gas at a higher tempera~ture generated elsewhere in the system. The heating of the exhausted process gas occurs in a heat exchanger external to the cell and the resultant gas is then utilized to produce the desired steam.
In the preferred form of the invention, the fuel cell is operated with excess process gas for cooling the cell to a desired operating temperature and the exhausted cooling process gas is used for steam generation. In still further preferred form, excess oxidant gas is utilized for fuel cell cooling and exhausted oxidant gas for steam generation.
Description ~f_ b- D~_~.Ue~
The above and other features and spects of the ~ il76306 1 present invention will become more apparent upon reading the following detailed description in conjunction with the accompanying sole drawing which shows a fuel cell system in accordance with the principles of the present invention.
Detailed Description In F~G. 1, the fuel cell system 1 comprises a fuel cell 2 which, preferably, is a phosphoric acid cell, although the principles of the invention extend to other cell types such as, for example, molten carbonate cells and solid oxide cells. An anode section 3 and a cathode section 4 communicating with an electrolyte section 50 receive respective fuel process gas and oxidant process gas along input lines 5 and 6, respectively. In conventional practice, the fuel and oxidant gases are at substantially the same pressure which might, typically, be in the range of 30 to 150 psia, so as to promote fuel cell efficiency. Also, in the present illustrative example/ the flow of oxidant process gas is further of an amount in excess of that re~uired for electro-chemical reaction, the excess gas being of a quantity sufficient to cool the fuel cell to a predetermined temperature promotive of desired fuel cell lie.
The oxidant process gas is derived from a compressor section 7 of a turbocompressor unit 10, the compressor 7 raising the pressure of the oxidant gas from a supply 8 to the desired pressure. The fuel process gas is derived from a reformer 9 which receives from a common line 11 a mixture of preheated hydrocarbon fuel and steam coupled to the line 11 by respective lines 12 and 13. ~he hydrocarbon fuel is provided to the line 12 from a compressor section 14 of the turbocompressor 10, the section being fed from a fuel supply ! ~76306 1 15. A pre-heater in the form of a heat exchanger 16 situated in the line 12 preheats the fresh fuel pxior to coupling to the common line 11.
In order for the fuel process gas produced by the reformer 9 to be at the desired pressure, the steam provided to the line 11 from the line 13 must be at least at that pressure, since the steam pressure controls the resultant fuel process gas pressure. Perferably, the steam pressure should be higher than the required fuel process gas pressure, in order to account for pressure losses in the reformer and in the lines carrying the gas to the anode section 3.
Additionally, to prevent carbon formation in the reformer, a certain ratio of steam to fuel is required. For example, with liquid naptha as a fuel, a ratio of 4 moles steam to 1 lS mole carbon is desirable. Preferably, that amount of steam should be at a pressure above the fuel gas pressure.
In accordance with the principles of the present invention, steam at the desired pressure and of a desired amount is generated in the fuel cell system utilizing a quantity of excess oxidant gas exhausted from the cathode section 4 and, therefore, at the predetermined fuel cell temperature, and a further quantity of higher temperature gas derived from elsewhere in the fuel cell system. These gases are carried via lines 18 and 21 to an auxiliary heater or heat exchanger 17, the temperature of the higher temperature gas being sufficient to raise the temperature of the quantity of oxidant gas to that required to produce the desired amount of steam at the desired pressure. The increased temperature oxidant gas is, ~hereafter, applied to a steam generator in the form of a heat exchanger 22 having a pressure ~ ~6306 1 valve for allowing steam issuance at the desired pressure.
Water from a supply 23 is coupled to the generator 22 and is raised therein to steam at such pressure, the steam then being coupled to the generator output line 24 which feeds steam line 13.
As above indicated, the higher temperature gas in the line 21 is obtained from gas dexived in the fuel cell system from elsewhere than the fuel cell 2. As shown in dotted line, such gas may be obtained by passage of a portion of the unburned anode gas exhausted into anode exhaust line 25 through a burner 41, thereby producing gas at a signifi-cantly higher temperature than the cell operating temperature.
Other gases which also can be used as the higher temperature gas will be pointed out below in the discussion of the remainder of the system 1.
The reformer 9 is provided with reaction heat from a burner 26 which burns a combination of preheated fresh supply fuel, exhausted fuel gas and compressed oxidant : supply gas. The latter gases are coupled to the burner 26 via lines 27 and 28, respectively in which are situated heat exchangers 29 and 31 for raising the temperatures of the respective gases. The latter exchangers are in stacked relationship with the reformer 9 and the burner 26 and are heated by the burner gas~ The burner gas is thereafter coupled via line 32 to an exit line 33 which also receives a quantity of exhausted oxidant process gas from the line 19.
The gas in the line 33 is expanded in a turboexpander section 42 o the turbocompressor 10 and is exhausted from the system via line 34. As indicated in dotted line, the gas in line 34 also can be coupled to line 21 for providing gas for - I 1763~6 1 ¦ heating the exhausted oxidant gas coupled to the heat exchanger 1 17.
¦ The combi~ed fuel and steam in the line 11 is pre-heated prior to application to reformer 9 via a heat exchanger 35 to which is also applied the outgoing fuel process gas generated by the reformer. The latter gas is thereafter cooled by passage via line 36 through heat exchanger 16 and a high temperature low temperature shift converter 37, the high temperature converter of which includes a heat exchanger section 38.for heat exchange with the steam in the line 13 prior to coupling to ~he line 11 and the low temperature converter of which includes a heat exchanger section 39 to which is coupled water from a further water supply 43.
The fuel process gas is brought to an intermediate temperature by the converter 37 and, as shown, in dotted line, the gas at the output line 44 of the converter is also suitable for coupling -to the line 21 for application to the heat exchanger 17 for heating the exhausted oxidant gas coupled thereto. A further heat exchanger 45 in the line 44 receives the intermediate temperature fuel ~rocess gas and water from a supply 45 further lowering the temperature of same to the predetermined cell temperature for application to the line 5 feeding anode section 3.
As can be appreciated, the degree to which the tempèrature of the exhausted oxidant gas applied to the heat exchanger 17 is to be r~ised and, thus, the temperature of the higher temperature gas, as well as the amount of exhausted oxidant gas supplied will depend upon the desired pressure and amount of steam to be produced. The latter, in turn, will depend upon system requirements including, amongst ~ ~ 76306 1 ¦ other things, ~he desired fuel cell pressure and operating ¦ temperature, as well as the quantity and pressure of steam ¦ required in the reformer 9. The particular values of these ¦ parameters will of course depend upon each individual applica-S ¦ tion.
In a typical situation of a phosphoric acid fuel cell stack at an operating temperature of 375F and fuel and oxidant gases at pressures of approximately 50 psia, and a reformer requiring a steam flow of 1.8 lb , the quantity of exhaust oxidant gas delivered to heat exchanger 17 might be 205 lb . In such case, the temperature of the further hr-kw gas delivered to heat exchanger might be 500 to 1500F, thereby raising the oxidant gas to a temperature of approximately 400F. Production of this further gas at such tempera~ure might, in turn, be realized by burning exhausted fuel gas.
Alternatively, a similar flow of fuel gas at such temperature from the converter 37 or from the line 34 might also be used.
In all cases, it is understood that the above-
2~ described arrangements are merely illustrative of the many possible specific embodiments which represent applications of the present invention. Numerous and varied other arrangements can readily be devised in accordance with the principles of the present invention ~ithout departing from the spirit and scope of the invention. Thus, for example, the steam generator 22 and the auxiliary heater 17 could be combined into a single heat exchange unit, instead of two separate units as specifically illustrated in the figure.
Claims (27)
1. A fuel cell system comprising:
a fuel cell including a cathode section for receiving oxidant process gas and an anode section for receiving fuel process gas;
and means responsive to exhausted process gas and to gas at a higher temperature for producing steam, said steam producing means including:
heat exchanger means for receiving said exhausted process gas and said higher temperature gas in heat exchange relationship to increase the temperature of said exhausted process gas to a point where said exhausted process gas can be placed in heat exchange relationship with water to produce steam.
a fuel cell including a cathode section for receiving oxidant process gas and an anode section for receiving fuel process gas;
and means responsive to exhausted process gas and to gas at a higher temperature for producing steam, said steam producing means including:
heat exchanger means for receiving said exhausted process gas and said higher temperature gas in heat exchange relationship to increase the temperature of said exhausted process gas to a point where said exhausted process gas can be placed in heat exchange relationship with water to produce steam.
2. A fuel cell system in accordance with claim 1 wherein:
said higher temperature gas is derived from gas of said system.
said higher temperature gas is derived from gas of said system.
3. A fuel cell system in accordance with claim 2 wherein:
the quantity of exhausted process gas received by said heat exchanger and the increased temperature of said received exhausted process gas are such as to enable production of said steam at a predetermined pressure.
the quantity of exhausted process gas received by said heat exchanger and the increased temperature of said received exhausted process gas are such as to enable production of said steam at a predetermined pressure.
4. A fuel cell system in accordance with claim 3 wherein:
said fuel cell receives one of said oxidant and fuel process gases in excess of that required for electrochemical reaction for cooling of said cell;
and the exhausted of said one of said oxidant and fuel process gases is the exhausted gas to which said steam producing means is responsive.
said fuel cell receives one of said oxidant and fuel process gases in excess of that required for electrochemical reaction for cooling of said cell;
and the exhausted of said one of said oxidant and fuel process gases is the exhausted gas to which said steam producing means is responsive.
5. A fuel cell system in accordance with claim 3 wherein:
said exhausted process gas is exhausted oxidant process gas.
said exhausted process gas is exhausted oxidant process gas.
6. A fuel cell system in accordance with claim 5 further including:
means for burning exhausted fuel process gas to produce said higher temperature gas.
means for burning exhausted fuel process gas to produce said higher temperature gas.
7. A fuel cell system in accordance with claim 5 wherein:
said fuel process gas is at a preselected pressure.
said fuel process gas is at a preselected pressure.
8. A fuel cell system in accordance with claim 7 further including:
means for combining fresh supply fuel with said steam;
and reforming means responsive to said combined fresh supply fuel and steam for providing said fuel process gas through a reforming reaction.
means for combining fresh supply fuel with said steam;
and reforming means responsive to said combined fresh supply fuel and steam for providing said fuel process gas through a reforming reaction.
9. A fuel cell system in accordance with claim 8 wherein:
said predetermined pressure of said steam is such that said fuel process gas from said gas reforming means is at least at said preselected pressure.
said predetermined pressure of said steam is such that said fuel process gas from said gas reforming means is at least at said preselected pressure.
10. A fuel cell system in accordance with claim 9 wherein:
the quantity of exhausted process gas received by said heat exchanger and the increased temperature of said received exhausted process gas are such as to enable production of a predetermined quantity of steam at said predetermined pressure said predetermined quantity being sufficient for said reforming reaction.
the quantity of exhausted process gas received by said heat exchanger and the increased temperature of said received exhausted process gas are such as to enable production of a predetermined quantity of steam at said predetermined pressure said predetermined quantity being sufficient for said reforming reaction.
11. A fuel cell system in accordance with claim 9 wherein:
said steam producing means further includes a steam generator for receiving water and said increased temperature process gas in heat exchange relationship to thereby generate said steam.
said steam producing means further includes a steam generator for receiving water and said increased temperature process gas in heat exchange relationship to thereby generate said steam.
12. A fuel cell system in accordance with claim 8 wherein:
said fuel process gas from said reforming means is at a first temperature higher than a preselected operating temperature for said cell;
and said system further includes means for reducing the temperature of said fuel process gas to a second temperature between said first temperature and said preselected operating temperature; and a quantity of said second temperature fuel process gas forms said higher temperature gas.
said fuel process gas from said reforming means is at a first temperature higher than a preselected operating temperature for said cell;
and said system further includes means for reducing the temperature of said fuel process gas to a second temperature between said first temperature and said preselected operating temperature; and a quantity of said second temperature fuel process gas forms said higher temperature gas.
13. A fuel cell system in accordance with claim 8 further including:
means for burning a quantity of said fresh supply fuel to produce heating gas and for coupling said heating gas to said reformer for providing heat for said reforming reaction;
means for combining a portion of said heating gas with a portion of exhausted oxidant process gas;
and means for reducing the pressure of said combination of said heating gas and said portion of exhausted oxidant process gas, a quantity of said reduced pressure combination of gases forming said higher temperature gas.
means for burning a quantity of said fresh supply fuel to produce heating gas and for coupling said heating gas to said reformer for providing heat for said reforming reaction;
means for combining a portion of said heating gas with a portion of exhausted oxidant process gas;
and means for reducing the pressure of said combination of said heating gas and said portion of exhausted oxidant process gas, a quantity of said reduced pressure combination of gases forming said higher temperature gas.
14. A fuel cell system in accordance with claim 7 wherein:
said preselected pressure is within the range of 30 to 200 psia.
said preselected pressure is within the range of 30 to 200 psia.
15. A fuel cell in accordance with claim 1 or 2 wherein said fuel cell system further includes:
a phosphoric acid electrolyte disposed between said anode and cathode sections.
a phosphoric acid electrolyte disposed between said anode and cathode sections.
16. A method of producing steam in a fuel cell system including a fuel cell having anode and cathode sections receiving fuel and oxidant process gases, the method comprising:
obtaining a quantity of exhausted process gas;
utilizing said quantity of exhausted process gas and a quantity of higher temperature gas to produce steam including:
placing said quantities of exhausted process gas and higher temperature gas in heat exchange relationship to increase the temperature of said exhausted process gas to a point where said exhausted process gas can be placed in heat exchange relationship with water to produce steam.
obtaining a quantity of exhausted process gas;
utilizing said quantity of exhausted process gas and a quantity of higher temperature gas to produce steam including:
placing said quantities of exhausted process gas and higher temperature gas in heat exchange relationship to increase the temperature of said exhausted process gas to a point where said exhausted process gas can be placed in heat exchange relationship with water to produce steam.
17. A method in accordance with claim 16 wherein:
said step of utilizing includes placing said increased temperature process gas in heat exchange relationship with water to produce steam.
said step of utilizing includes placing said increased temperature process gas in heat exchange relationship with water to produce steam.
18. A method in accordance with claim 16 wherein:
said step of utilizing includes placing said quantities of exhausted process gas and higher temperature gas in heat exchange relationship, whereby the temperature of said quantity of exhausted process gas in increased.
said step of utilizing includes placing said quantities of exhausted process gas and higher temperature gas in heat exchange relationship, whereby the temperature of said quantity of exhausted process gas in increased.
19. A method in accordance with claim 16 wherein:
said higher temperature gas is derived from a gas of said system.
said higher temperature gas is derived from a gas of said system.
20. A method in accordance with claim 19 wherein:
the amount and temperature of said quantity of increased temperature exhausted process gas results in steam at a predetermined pressure.
the amount and temperature of said quantity of increased temperature exhausted process gas results in steam at a predetermined pressure.
21. A method in accordance with claim 20 wherein:
said fuel cell receives one of said oxidant and fuel process gases in excess of that required for electrochemical reaction for cooling of said cell;
and said step of obtaining is carried out by deriving a quantity of exhausted of said one of said oxidant and fuel process gases.
said fuel cell receives one of said oxidant and fuel process gases in excess of that required for electrochemical reaction for cooling of said cell;
and said step of obtaining is carried out by deriving a quantity of exhausted of said one of said oxidant and fuel process gases.
22. A method in accordance with claim 20 wherein:
said exhausted process gas is exhausted oxidant process gas.
said exhausted process gas is exhausted oxidant process gas.
23. A method in accordance with claim 22 wherein:
said method further includes burning exhausted fuel process gas;
and said step of utilizing is carried by employing a quantity of said burned exhausted fuel process gas as said higher temperature gas.
said method further includes burning exhausted fuel process gas;
and said step of utilizing is carried by employing a quantity of said burned exhausted fuel process gas as said higher temperature gas.
24. A method in accordance with claim 22 further comprising:
combining a quantity of said steam with fresh supply fuel;
and subjecting said combination of steam and fresh supply fuel to a reforming reaction to provide said fuel process gas.
combining a quantity of said steam with fresh supply fuel;
and subjecting said combination of steam and fresh supply fuel to a reforming reaction to provide said fuel process gas.
25. A method in accordance with claim 24 wherein:
said method further includes reducing the temperature of said fuel process gas produced by said reforming reaction;
and said step of utilizing is carried out employing a quantity of said reduced temperature fuel process gas as said higher temperature gas.
said method further includes reducing the temperature of said fuel process gas produced by said reforming reaction;
and said step of utilizing is carried out employing a quantity of said reduced temperature fuel process gas as said higher temperature gas.
26. A method in accordance with claim 22 wherein:
said method further includes:
burning a quantity of fresh supply fuel to produce heated gas for use in said reforming reaction;
combining a quantity of such heated gas with a portion of exhausted oxidant gas;
and reducing the pressure of said combination of gases, a quantity of said reduced pressure combination of gases forming said higher temperature gas.
said method further includes:
burning a quantity of fresh supply fuel to produce heated gas for use in said reforming reaction;
combining a quantity of such heated gas with a portion of exhausted oxidant gas;
and reducing the pressure of said combination of gases, a quantity of said reduced pressure combination of gases forming said higher temperature gas.
27. A method in accordance with claims 16, 18 or 19 wherein:
a phosphoric acid electrolyte is disposed between the anode and cathode sections of said fuel cell.
a phosphoric acid electrolyte is disposed between the anode and cathode sections of said fuel cell.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US06/226,901 US4352863A (en) | 1981-01-21 | 1981-01-21 | Apparatus and method for producing high pressure steam in a fuel cell system |
| US226,901 | 1981-01-21 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1176306A true CA1176306A (en) | 1984-10-16 |
Family
ID=22850902
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000394010A Expired CA1176306A (en) | 1981-01-21 | 1982-01-12 | Apparatus and method for producing high pressure steam in a fuel cell system |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US4352863A (en) |
| EP (1) | EP0056654B1 (en) |
| JP (1) | JPS57141877A (en) |
| CA (1) | CA1176306A (en) |
| DE (1) | DE3270915D1 (en) |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60195880A (en) * | 1984-03-19 | 1985-10-04 | Hitachi Ltd | Power generation system using solid electrolyte fuel cell |
| JPH0622148B2 (en) * | 1984-07-31 | 1994-03-23 | 株式会社日立製作所 | Molten carbonate fuel cell power plant |
| JPS6171561A (en) * | 1984-09-14 | 1986-04-12 | Mitsubishi Heavy Ind Ltd | Composite plant of fuel cell |
| US4567033A (en) * | 1984-10-25 | 1986-01-28 | United Technologies Corporation | Low-energy method for freeing chemically bound hydrogen |
| US4539267A (en) * | 1984-12-06 | 1985-09-03 | United Technologies Corporation | Process for generating steam in a fuel cell powerplant |
| JPH0658806B2 (en) * | 1985-03-22 | 1994-08-03 | 株式会社日立製作所 | Fuel cell power plant |
| US4670359A (en) * | 1985-06-10 | 1987-06-02 | Engelhard Corporation | Fuel cell integrated with steam reformer |
| JPH0789494B2 (en) * | 1986-05-23 | 1995-09-27 | 株式会社日立製作所 | Combined power plant |
| JPS63141269A (en) * | 1986-12-01 | 1988-06-13 | Jgc Corp | Fuel cell generating system |
| JPS6412468A (en) * | 1987-07-03 | 1989-01-17 | Sanyo Electric Co | Refining device for metanol fuel of fuel cell |
| US4743517A (en) * | 1987-08-27 | 1988-05-10 | International Fuel Cells Corporation | Fuel cell power plant with increased reactant pressures |
| JPH01157065A (en) * | 1987-12-14 | 1989-06-20 | Sanyo Electric Co Ltd | Fuel cell power generating system |
| DE19903168C2 (en) * | 1999-01-27 | 2002-06-20 | Xcellsis Gmbh | Spiral heat exchanger |
| DE10037825A1 (en) * | 2000-08-03 | 2002-05-16 | Xcellsis Gmbh | The fuel cell system |
| US6926748B2 (en) * | 2001-11-19 | 2005-08-09 | General Motors Corporation | Staged lean combustion for rapid start of a fuel processor |
| US7700207B2 (en) * | 2006-11-09 | 2010-04-20 | Gm Global Technology Operations, Inc. | Turbocompressor shutdown mechanism |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5091730A (en) * | 1973-12-19 | 1975-07-22 | ||
| US4004947A (en) * | 1975-02-12 | 1977-01-25 | United Technologies Corporation | Pressurized fuel cell power plant |
| US3976506A (en) * | 1975-02-12 | 1976-08-24 | United Technologies Corporation | Pressurized fuel cell power plant with air bypass |
| US4001041A (en) * | 1975-02-12 | 1977-01-04 | United Technologies Corporation | Pressurized fuel cell power plant |
| US3973993A (en) * | 1975-02-12 | 1976-08-10 | United Technologies Corporation | Pressurized fuel cell power plant with steam flow through the cells |
| DE2604981C2 (en) * | 1975-02-12 | 1985-01-03 | United Technologies Corp., Hartford, Conn. | Pressurized fuel cell power systems and methods for their operation |
| US3982962A (en) * | 1975-02-12 | 1976-09-28 | United Technologies Corporation | Pressurized fuel cell power plant with steam powered compressor |
| US3976507A (en) * | 1975-02-12 | 1976-08-24 | United Technologies Corporation | Pressurized fuel cell power plant with single reactant gas stream |
| US3969145A (en) * | 1975-07-21 | 1976-07-13 | United Technologies Corporation | Fuel cell cooling system using a non-dielectric coolant |
| US4046956A (en) * | 1976-05-27 | 1977-09-06 | United Technologies Corporation | Process for controlling the output of a selective oxidizer |
| US4041210A (en) * | 1976-08-30 | 1977-08-09 | United Technologies Corporation | Pressurized high temperature fuel cell power plant with bottoming cycle |
| US4128700A (en) * | 1977-11-26 | 1978-12-05 | United Technologies Corp. | Fuel cell power plant and method for operating the same |
-
1981
- 1981-01-21 US US06/226,901 patent/US4352863A/en not_active Expired - Lifetime
-
1982
- 1982-01-12 CA CA000394010A patent/CA1176306A/en not_active Expired
- 1982-01-13 JP JP57002909A patent/JPS57141877A/en active Granted
- 1982-01-20 DE DE8282100369T patent/DE3270915D1/en not_active Expired
- 1982-01-20 EP EP82100369A patent/EP0056654B1/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6326514B2 (en) | 1988-05-30 |
| EP0056654B1 (en) | 1986-05-07 |
| JPS57141877A (en) | 1982-09-02 |
| US4352863A (en) | 1982-10-05 |
| EP0056654A1 (en) | 1982-07-28 |
| DE3270915D1 (en) | 1986-06-12 |
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