AU2016269456B2

AU2016269456B2 - Power generation apparatus with integrated clp and sofc and operation and control method thereof

Info

Publication number: AU2016269456B2
Application number: AU2016269456A
Authority: AU
Inventors: Wen-Sheng Chang; Yu-Ching Chang; Hsi-Chuan Chen; Jar-Lu Huang; Chun-I Lee; Cheng-Hsien Shen; Fu-Pin Ting
Original assignee: Industrial Technology Research Institute ITRI
Current assignee: Industrial Technology Research Institute ITRI
Priority date: 2015-12-08
Filing date: 2016-12-07
Publication date: 2018-05-10
Anticipated expiration: 2036-12-07
Also published as: CN106856245A; CN106856245B; TWI557981B; TW201721949A; AU2016269456A1

Abstract

A power generation apparatus with integrated CLP (chemical looping process) and SOFC (solid oxide fuel cell) and an operation method thereof are provided. The power generation apparatus includes a chamber body, a SOFC stack, and a CLP device. The chamber body has a valve separating it into a first chamber and a second chamber, and the SOFC stack is disposed in the first chamber. The CLP device is disposed in the second chamber, and the CLP device produces hydrogen and carbon dioxide, wherein the produced hydrogen is used as anode fuel of the SOFC stack. By opening the valve, high-temperature carbon dioxide produced by the CLP device can enter the first chamber to heat the SOFC stack. ) C02 20-,A 212-- _ Air 210 , - 234 200a ,r - 220 222 228 / -228 Fuel- 216 224 230 H2 Steam <- Air

Description

POWER GENERATION APPARATUS WITH INTEGRATED CLP AND SOFC AND OPERATION AND CONTROL METHOD THEREOF

TECHNICAL FIELD

[0001] The disclosure relates to a power generation apparatus, and more particularly, to a power generation apparatus with integrated CLP (chemical looping process) and SOFC (solid oxide fuel cell) and an operation and control method thereof.

BACKGROUND

[0002] The operating temperature of a SOFC system is about 850 °C, and since a fuel cell needs to be in a high-temperature environment for stable operation and power generation, the current methods of system heating or maintaining system operating environment temperature generally adopt a gas heater to meet the heat requirements of the system. However, maintaining temperature using a gas heater is energy-consuming and energy benefits are lacking, and therefore a system having high-temperature gas production is also needed for operation for the need of fuel supply and efficient recycling of the heat energy of the high-temperature gas source to achieve the objects of system energy saving and simplification.

SUMMARY

[0003] The disclosure provides a power generation apparatus with integrated CLP and SOFC that has all of the effects of carbon dioxide capture, high energy usage, and high power generation efficiency.

[0004] The disclosure further provides an operation and control method of a power generation apparatus with integrated CLP and SOFC that can recycle waste heat.

[0005] The power generation apparatus with integrated CLP and SOFC of the disclosure includes a chamber body having a valve dividing the chamber body into a first and second chamber, a SOFC stack disposed in the first chamber, and a CLP device disposed in the second chamber. The CLP device produces high-temperature hydrogen and high-temperature carbon dioxide, wherein the hydrogen is used as an anode fuel of the SOFC stack and high-temperature carbon dioxide enters the first chamber by opening the first valve to heat the SOFC stack.

[0006] The operation and control method of the disclosure includes providing fuel to a CLP device of a power generation apparatus to produce hydrogen and carbon dioxide, wherein the power generation apparatus includes a chamber body divided into a first and second chamber by a first valve, and the CLP device is disposed in the second chamber. Then, the first valve is opened to make the carbon dioxide produced by the CLP device enter the first chamber via the open first valve to heat the SOFC stack disposed in the first chamber. The hydrogen produced by the CLP device is transported to the SOFC stack to be used as an anode fuel of the SOFC stack.

[0007] Based on the above, in the disclosure, carbon dioxide capture, high energy usage, and high power generation efficiency can all be achieved via the design of integrated CLP and SOFC with an operation interface and SOFC high-temperature steady-state operation.

[0008] Several exemplary embodiments accompanied with figures are described in detail below to further describe the disclosure in details.

BRIEF DESCRIPTION OF DRAWINGS

[0009] The accompanying drawings are included to provide further understanding, and are incorporated in and constitute a part of this specification. The drawings illustrate exemplary embodiments and, together with the description, serve to explain the principles of the disclosure.

[0010] FIG. 1 is a simplified diagram of a power generation apparatus with integrated CLP (chemical loop process) and SOFC (solid oxide fuel cell) according to the first embodiment of the disclosure.

[0011] FIG. 2 is a schematic diagram of a power generation apparatus with integrated CLP and SOFC according to the second embodiment of the disclosure.

[0012] FIG. 3 is a schematic diagram of a power generation apparatus with integrated CLP and SOFC according to the third embodiment of the disclosure.

[0013] FIG. 4 is a schematic diagram of a power generation apparatus with integrated CLP and SOFC according to the fourth embodiment of the disclosure.

[0014] FIG. 5 is a schematic diagram of a power generation apparatus with integrated CLP and SOFC according to the fifth embodiment of the disclosure.

[0015] FIG. 6 is a schematic diagram of a power generation apparatus with integrated CLP and SOFC according to the sixth embodiment of the disclosure.

DESCRIPTION OF EMBODIMENTS

[0016] FIG. 1 is a simplified diagram of a power generation apparatus with integrated CLP (chemical loop process) and SOFC (solid oxide fuel cell) according to the first embodiment of the disclosure.

[0017] Referring to FIG. 1, the main systems in a power generation apparatus 10 of the present embodiment are all disposed in a chamber body 100, and the chamber body 100 has a valve 102 dividing the chamber body 100 into a first chamber 104 and a second chamber 106, and a SOFC (solid oxide fuel cell) stack 108 and a CLP (chemical loop process) device 110 in the power generation apparatus 10 are respectively disposed in the first chamber 104 and the second chamber 106. When fuel is provided to the CLP device 110 of the power generation apparatus 10, high-temperature carbon dioxide and high-temperature hydrogen are produced, and the carbon dioxide temperature is about 900 °C or above. For instance, a carbon-based fuel is utilized as a reaction raw material in the CLP device 110, and an iron-based oxygen carrier is the source of oxygen in a chemical reaction process within the CLP device 110 so as to produce hydrogen and carbon dioxide. Then, high-temperature carbon dioxide can enter the first chamber 104 by opening the valve 102 to heat the SOFC stack 108 disposed in the first chamber 104. The valve 102 in the present embodiment can adopt different designs as needed. For instance, a high-temperature resistant shielding plate is included in the figures, but the disclosure is not limited thereto. The valve 102 (and the shielding plate) used in the power generation apparatus 10 is preferably heat resistant to 1000 °C or more, and the heat resistant range thereof is, for instance, between 1000 °C and 1800 °C. The hydrogen produced by the CLP device 110 is transported to the SOFC stack 108 to be used as an anode fuel of the SOFC stack 108. In the present embodiment, the first chamber 104 is located above the second chamber 106, but the disclosure is not limited thereto, and as long as high-temperature carbon dioxide can enter the first chamber 104 after the valve 102 is opened, either the principle that hot air rises to the top or assistance from other pumping devices can be adopted to achieve the effect.

[0018] In the present embodiment, the high-temperature carbon dioxide entering the first chamber 104 can heat the SOFC stack 108 so that the SOFC stack 108 reaches an applicable operating temperature, and the temperature of the SOFC stack 108 can be measured to decide whether to continue heating or decide the degree of heating. For instance, the valve opening degree of the valve 102 can be controlled based on the temperature of the SOFC stack 108 so as to control the flow rate of carbon dioxide entering the first chamber 104. The so-called “valve opening degree” refers to the degree to which the valve opens, i.e., a valve opening degree of 0 means the valve is fully closed, a valve opening degree of 100% means the valve is fully open, and a valve opening degree of 50% means the valve is half open, etc.

[0019] FIG. 2 is a schematic diagram of a power generation apparatus with integrated CLP and SOFC according to the second embodiment of the disclosure.

[0020] Referring to FIG. 2, the main systems in a power generation apparatus 20 of the present embodiment are disposed in a chamber body 200, and the chamber body 200 has a first valve 202 dividing the chamber body 200 into a first chamber 204 and a second chamber 206, and a SOFC (solid oxide fuel cell) stack 208 and a CLP (chemical loop process) device in the power generation apparatus 20 are respectively disposed in the first chamber 204 and the second chamber 206. In the present embodiment, the first chamber 204 can have a carbon dioxide vent port 200a, and a second valve 210 is disposed adjacent to the carbon dioxide vent port 200a to open or close the carbon dioxide vent port 200a. Moreover, since the temperature of the carbon dioxide airflow is very high, to prevent uneven dispersion of the airflow causing uneven distribution of battery temperature and affecting the reaction efficiency, an airflow distributor 212 can be disposed between the SOFC stack 208 in the first chamber 204 and the first and second valves 202 and 210. When high-temperature carbon dioxide airflow is to enter, airflow distribution can be performed by the airflow distributor 212 to achieve a uniformly-distributed flow field, wherein the airflow distributor 212 is, for instance, a plate having holes or other suitable designs.

[0021] The CLP device can contain a reduction reactor 214, an oxidation reactor 216, a burner 218, and a cyclone separator 220. The operating principle of the CLP device is as follows. An oxygen carrier is utilized in the CLP to perform an oxidation-reduction reaction, a fuel (such as carbon-based fuel) is first introduced via a fuel pipe 222, and then a chemical reaction is performed in the reduction reactor 214 to produce high-temperature carbon dioxide. The high-temperature carbon dioxide is exhausted via an exhaust pipe 228, the oxygen carrier continues to fall in the oxidation reactor 216, and steam is introduced in the oxidation reactor 216 via a steam pipe 224 at the same time to perform a second chemical reaction. In addition to exhausting upwards, the exhaust pipe 228 can also exhaust to the side, or exhaust upwards and to the side to the second chamber 206 at the same time, and the exhausted high-temperature carbon dioxide is converged to the first chamber 204 as a heat source to pre-heat the SOFC stack 208 or maintain the temperature of the SOFC stack 208. High-temperature hydrogen is produced in the oxidation reaction and also exhausted to a hydrogen pipe 230 via the oxidation reactor 216. At this point, the oxygen carrier not completely reacted keeps falling into the burner 218 and air is introduced in the burner 218 to react via the air pipe 226 so as to reduce the reacted oxygen carrier. Next, the oxygen carrier enters the cyclone separator 220 to continue the chemical loop reaction process. The SOFC stack 208 can include an anode pipe 232 for introducing anode fuel and a cathode pipe 234 for introducing cathode fuel, and the anode pipe 232 is connected to the hydrogen pipe 230 of the CLP device, and therefore hydrogen can be accepted as the anode fuel of the SOFC stack 208.

[0022] In the present embodiment, the first valve 202 and the second valve 210 can be designed into an airflow path with a high-temperature resistant shielding plate, and therefore after the first valve 202 and the second valve 210 are open, high-temperature carbon dioxide airflow passes through the first valve 202 and the airflow is uniformly distributed via the airflow distributor 212. At this point, high-temperature carbon dioxide airflow is spread out around the SOFC stack 208. After using the high-temperature airflow to heat the SOFC stack 208 such that the SOFC stack 208 reaches the desired operating temperature, the high-temperature airflow passes through the airflow distributor 212 again to enter the second valve 210 and then leaves the first chamber 204. Moreover, whether heating is continued can be decided by measuring the temperature of the SOFC stack 208. If heating is to be continued, then the first valve 202 and the second valve 210 are kept open; on the other hand, if the operating temperature of the SOFC stack 208 is reached, then the first valve 202 and the second valve 210 are closed. The flow rate of the high-temperature carbon dioxide airflow entering the first chamber 204 is decided based on the opening or closing of the first valve 202 and the second valve 210. Moreover, the flow rate of carbon dioxide exhausted from the first chamber 204 can further be controlled by controlling the valve opening degree of the second valve 210. For instance, during the heating up stage of the SOFC stack 208, the first valve 202 and the second valve 210 are both fully open; during the temperature maintenance stage of the SOFC stack 208, the first valve 202 and the second valve 210 are also both fully open; during the load operation stage of the SOFC stack 208, the first valve 202 and the second valve 210 are both fully closed; and during the shutdown cooling stage of the SOFC stack 208, the first valve 202 and the second valve 210 are both half open.

[0023] FIG. 3 is a schematic diagram of a power generation apparatus with integrated CLP and SOFC according to the third embodiment of the disclosure, wherein the same reference numerals as FIG. 2 are used to represent the same or similar components.

[0024] Referring to FIG. 3, in the present embodiment, in addition to the components of FIG. 2, the exhaust gas of the SOFC stack 208 or carbon dioxide exhausted from the first chamber 204 can be used as the steam heat source of the CLP device, and before the gases are used as the steam heat source, the exhaust gas or carbon dioxide can be heated first. For instance, the desired steam for the reaction in the oxidation reactor 216 can be produced by a steam generator 300, and the heat source needed for the steam generator 300 is provided by heating the carbon dioxide exhausted from the first chamber 204 with a first heating unit 302 (such as a heat exchanger) or provided by heating the exhaust gas exhausted from the SOFC stack 208 with a second heating unit 304, wherein the second heating unit 304 is, for instance, a device fonned by an afterburner 306 and a heat exchanger 308, and the exhaust gas can be from the heat exchanger 308. The water source needed for the steam generator 300 can be provided by a water pump 310, but the disclosure is not limited thereto. The water source needed for the steam generator 300 can also be water collected from the condensation of each of the heat exchangers.

[0025] Using the operation and control of the SOFC stack 208 as an example, when the SOFC stack 208 is in the heating up stage, neither the exhaust gas of the SOFC stack 208 nor carbon dioxide exhausted from the first chamber 204 needs to be heated; when the SOFC stack 208 is in a temperature maintenance stage, both the exhaust gas of the SOFC stack 208 and the carbon dioxide exhausted from the first chamber 204 need to be kept at high temperature; when the SOFC stack 208 is in a load operation stage, both the exhaust gas of the SOFC stack 208 and the carbon dioxide exhausted from the first chamber 204 need to be kept at high temperature; and when the SOFC stack 208 is in a shutdown cooling stage, neither the exhaust gas of the SOFC stack 208 nor the carbon dioxide exhausted from the first chamber 204 needs to be heated.

[0026] FIG. 4 is a schematic diagram of a power generation apparatus with integrated CLP and SOFC according to the fourth embodiment of the disclosure, wherein the same reference numerals as FIG. 2 are used to represent the same or similar components.

[0027] Referring to FIG. 4, in the present embodiment, in addition to the components of FIG. 2, an anode fuel supply unit 400 can further be included to receive a dilution gas or a carrier gas and hydrogen produced by the CLP device and provide the dilution gas or the carrier gas and the hydrogen to the SOFC stack 208. Since the hydrogen concentration of SOFC does not need to be too high, in the present embodiment, nitrogen or carbon dioxide can be used as the dilution gas or the carrier gas for diluting hydrogen, and the source of the nitrogen can be a liquid nitrogen cylinder or a nitrogen generator. The anode fuel supply unit 400 can include a heat exchanger 402, a bypass valve 404, a suction pump 406, a flowmeter 408, and a mixer 410. For instance, the high-temperature hydrogen airflow produced in the CLP enters the heat exchanger 402 via the hydrogen pipe 230. The heat exchanger 402 has at least two functions. The first is to drop the temperature of the high-temperature hydrogen to facilitate the subsequent gas dust removal step; and the second is to use the heat removed from the heat exchange to heat the dilution gas or the carrier gas. The hydrogen can directly enter a dust remover 414 after cooling for the dust removing step and then enter the bypass valve 404. Alternatively, the powder therein may be removed using a screen when the fuel enters the fuel pipe 222 to achieve dust removal effect, and therefore the cooled hydrogen can also directly enter the bypass valve 404 for bypass. During the process, a portion of the hydrogen produced by the CLP device can also be bypassed by the bypass valve 404 and stored in a hydrogen storage tank 412 to be used as the hydrogen source needed when the SOFC stack 208 enters a shutdown process when the CLP device is shutdown or malfunctioned, and a portion of hydrogen can also be directly transported to the back-end chemical production line to produce industrial or commercial chemical products. Another portion of the hydrogen can be pumped into the pipe via the suction pump 406 and the amount of hydrogen to flow into the mixer 410 is controlled by the flowmeter 408. The function of the mixer 410 is mainly to mix the gases (i.e. dilution (or carrier) gas and hydrogen) to enter the SOFC stack 208, and after the gases are mixed, the gases enter the anode pipe 232 of the SOFC stack 208 as fuel needed for the anode. The flowmeter 408 can be a mass flowmeter or a mass flow controller (MFC).

[0028] The gas source of the dilution or carrier gas can be nitrogen (N2) or carbon dioxide exhausted from the first chamber 204. If nitrogen is used as the dilution gas or the carrier gas, then heat exchange can be performed on the carbon dioxide exhausted from the first chamber 204 with nitrogen to heat the nitrogen and drop the temperature of carbon dioxide. After the airflow temperature of carbon dioxide is dropped, a carbon dioxide capture process can be performed. For instance, a gas supply unit 416 can be disposed to provide dilution gas or earner gas to the heat exchanger 402 of the anode fuel supply unit 400, and the gas supply unit 416 can include a heat exchanger 418 and bypass valves 420 and 422.

[0029] When nitrogen is selected as a gas source of the dilution gas or the carrier gas for the bypass valve 420, nitrogen enters the bypass valve 422, and the bypass valve 422 mainly controls whether nitrogen needs to pass through the heat exchanger 418 for nitrogen heating. Nitrogen passes through two heat exchangers in the entire power generation apparatus, i.e., the heat exchanger 418 and the heat exchanger 402. The heat source of the heat exchanger 402 is mainly hydrogen produced in the CLP, and is provided to heat nitrogen after the heat exchange. Nitrogen is transported to the mixer 410 after heating, but since the SOFC stack 208 does not need nitrogen at a very high temperature during initial heating and loading, nitrogen can bypass the heat exchanger 418 via the bypass valve 422. On the other hand, if the nitrogen heated by the heat exchanger 402 does not reach the needed temperature, then nitrogen passes through the heat exchanger 418 via the bypass valve 422 for an additional nitrogen heating process. The heat energy of the heat exchanger 418 is obtained from the carbon dioxide exhausted from the first chamber 204. The heated nitrogen is mixed in the mixer 410 with hydrogen according to a desired ratio, and then the mixture enters the anode pipe 232.

[0030] When carbon dioxide is selected as a gas source of the dilution gas or the carrier gas for the bypass valve 420, the carbon dioxide can be obtained by cooling the high-temperature carbon dioxide flowing out of the first chamber 204, and after the high-temperature carbon dioxide passes through the heat exchanger 418, the temperature of the carbon dioxide is dropped to a level suitable for capture, and then the carbon dioxide flows into the bypass valve 420 and carbon dioxide airflow enters the bypass valve 422 from the bypass valve 420. As described above for nitrogen, if the carbon dioxide for dilution needs additional heating, then the bypass valve 422 is used to make the carbon dioxide pass through the heat exchanger 418 for an additional process; and if the carbon dioxide for dilution does not need additional heating, then the bypass valve 422 is used to bypass the heat exchanger 418. The heated carbon dioxide is mixed in the mixer 410 with hydrogen according to a desired ratio, and then the mixture enters the anode pipe 232.

[0031] Using the operation and control of the SOFC stack 208 as an example, when the SOFC stack 208 is in the heating up stage, the dilution gar or the carrier gas does not pass through the heat exchanger 418, but passes through the heat exchanger 402; when the SOFC stack 208 is in the temperature maintenance stage, the dilution gas or the carrier gas passes through the heat exchanger 418, and also passes through the heat exchanger 402; when the SOFC stack 208 is in a load operation stage, the dilution gas or the carrier gas passes through the heat exchanger 418 and the heat exchanger 402; and when the SOFC stack 208 is in the shutdown cooling stage, the dilution gas or the carrier gas does not pass through the heat exchanger 418, but passes through the heat exchanger 402.

[0032] FIG. 5 is a schematic diagram of a power generation apparatus with integrated CLP and SOFC according to the fifth embodiment of the disclosure, wherein the same reference numerals as FIG. 2 are used to represent the same or similar components.

[0033] Referring to FIG. 5, in the present embodiment, in addition to the components of FIG. 2, an air supply unit 500 can further be included to respectively provide air to the burner 218 of the CLP device and the SOFC stack 208. The air supply unit 500 can include an air pump 502, flowmeters 504 and 506, and a bypass valve 508. For instance, the cathode fuel of the SOFC stack 208 is air, and the source thereof can be extracted via the air pump 502, wherein the air pump 502 can be replaced by a large air storage tank, an air compressor, or a blower. The extracted airflow is divided into two portions for use. One portion is used as the cathode fuel of the SOFC stack 208, and the other portion is used as the reaction air needed for the burner 218 in the CLP. The flowmeter 504 controls the amount of air from the air pump 502 with the amount of air needed for the SOFC stack 208; and the flowmeter 506 controls the amount of air from the air pump 502 with the amount of air needed for the CLP device.

[0034] If the air is utilized as the cathode fuel of the SOFC stack 208, its flow rate is first controlled by the flowmeter 504, and then the air enters the bypass valve 508, wherein the flowmeter 504 can adopt a large air storage tank and replaced by a back-end MFC. The bypass valve 508 can divide air into two airflows. One is an air intake pipe 516 disposed in the second chamber 206 and connected to the air supply unit 500, and the other is air for temperature regulation when the temperature of the SOFC stack 208 is increased or when the SOFC stack 208 is in a load operation. The air intake pipe 516 can increase the air preheat energy by being coiled on the inner wall of the chamber body 200, and the preheat energy can be decided by the number of windings of the pipe. When air enters the air intake pipe 516, the air passing through the air intake pipe 516 is affected by the high-temperature carbon dioxide produced by the CLP device and is heated for the first time. Next, heat exchange can be perfonned on the air in a hot box 510 using the exhaust gas of the SOFC stack 208 to heat the air, and the heated air is used as the cathode fuel. Specifically, if the temperature of the air is too high during the initial operation of the SOFC stack 208, then the air needs to be first mixed with air for temperature regulation before entering the hot box 510. The hot box 510 contains two units, which are respectively an afterburner 512 and a heat exchanger 514, wherein the afterburner 512 can bum unreacted exhaust gas again, and then heat exchange is performed via the heat exchanger 514 to extract heat energy for heating the air passing through the air intake pipe 516 a second time, and then the exhaust gas enters the cathode pipe 234 of the SOFC stack 208.

[0035] If the air from the air pump 502 is used as the reaction air needed for the burner 218 in the CLP, then the flowmeter 506 is used to control the flow rate needed for the burner.

The flowmeter 506 is, for instance, a mass flowmeter, or a large air storage tank can be used, and the flowmeter 506 is replaced by a back-end MFC.

[0036] Using the operation and control of the SOFC stack 208 as an example, when the SOFC stack 208 is in the heating up stage, the air is heated in the air intake pipe 516, but the afterburner 512 does not operate; when the SOFC stack 208 is in a temperature maintenance stage, the air is heated in the air intake pipe 516 and also heated by the afterburner 512; when the SOFC stack 208 is in a load operation stage, the air is heated in the air intake pipe 516 and the afterburner 512; and when the SOFC stack 208 is in a shutdown cooling stage, the air in the air intake pipe 516 is heated, but the afterburner 512 does not operate.

[0037] FIG. 6 is a schematic diagram of a power generation apparatus with integrated CLP and SOFC according to the sixth embodiment of the disclosure, wherein the same reference numerals as FIG. 2 to FIG. 5 are used to represent the same or similar components.

[0038] In FIG. 6, the hot box 510 used to heat air can be used as a second heating unit (such as 304 of FIG. 3) providing the heat source to the steam generator 300 at the same time. For instance, the locations of the afterburner 512 and the heat exchanger 514 in the hot box 510 are both unchanged, and under the premise that the air intake pipe 516 can provide sufficient gas preheat energy, the high-temperature exhaust gas heat energy produced by the hot box 510 can be provided to the steam generator 300 to produce sufficient steam to the CLP oxidation reactor 216 to produce hydrogen.

[0039] The heat exchanger 302 used to heat the heat source needed for the steam generator 300 can also be used as the heat exchanger heating the dilution gas or the carrier gas at the same time (such as 418 of FIG. 4); in other words, the carbon dioxide airflow after the heat exchanger 302 can be bypassed via a bypass valve 600. At this point, if carbon dioxide is to be used as the dilution gas or the carrier gas, then carbon dioxide airflow can be controlled to enter the bypass valve 420 from the bypass valve 600; and if carbon dioxide is to be used as the heat source needed for the steam generator 300, then carbon dioxide airflow can be controlled to be provided to the steam generator 300 from the bypass valve 600. Moreover, the low-temperature carbon dioxide exhausted by the steam generator 300 can be sent back to the location of the bypass valve 420 as a gas source of dilution gas or carrier gas.

[0040] Based on the above, in the disclosure, by integrating a CLP and a SOFC system, an electronic gas heater can be omitted to provide a high-temperature operating environment, and all of the waste heat in the electronic apparatus can be recycled for use. Therefore, the effects of carbon dioxide capture, high energy usage, and high power generation efficiency can all be achieved.

[0041] It will be apparent to those skilled in the art that various modifications and variations can be made to the structure of the disclosed embodiments without departing from the scope or spirit of the disclosure. In view of the foregoing, it is intended that the disclosure cover modifications and variations of this disclosure provided they fall within the scope of the following claims and their equivalents.

Claims

WHAT IS CLAIMED IS:

1. A power generation apparatus with integrated CLP (chemical looping process) and SOFC (solid oxide fuel cell), comprising: a chamber body having a first valve dividing the chamber body into a first chamber and a second chamber; a SOFC stack disposed in the first chamber; and a CLP device disposed in the second chamber, wherein the CLP device produces a hydrogen and a carbon dioxide, the hydrogen is used as an anode fuel of the SOFC stack, and the carbon dioxide enters the first chamber by opening the first valve to heat the SOFC stack.
2. The power generation apparatus with integrated CLP and SOFC of claim 1, wherein the first chamber is located above the second chamber.
3. The power generation apparatus with integrated CLP and SOFC of claim 1, wherein the first chamber further comprises a carbon dioxide vent port.
4. The power generation apparatus with integrated CLP and SOFC of claim 1, further comprising an airflow distributor disposed in the first chamber and between the first valve and the SOFC stack.
5. The power generation apparatus with integrated CLP and SOFC of claim 1, wherein the CLP device comprises a steam pipe for introducing a steam, a fuel pipe for introducing a fuel, a hydrogen pipe for exhausting the hydrogen, and an air pipe for introducing an air.
6. The power generation apparatus with integrated CLP and SOFC of claim 5, wherein the SOFC stack comprises an anode pipe for introducing an anode fuel and a cathode pipe for introducing a cathode fuel, and the anode pipe is connected to the hydrogen pipe of the CLP device.
7. The power generation apparatus with integrated CLP and SOFC of claim 1, further comprising: a steam generator providing a steam to the CLP device; a first heating unit to heat a carbon dioxide exhausted from the first chamber and transfer the carbon dioxide to the steam generator; a second heating unit to heat an exhaust gas exhausted from the SOFC stack and transfer the exhaust gas to the steam generator; and a water pump to provide a water to the steam generator.
8. The power generation apparatus with integrated CLP and SOFC of claim 1, further comprising an anode fuel supply unit to receive a dilution gas or a carrier gas and the hydrogen produced by the CLP device and then provide the dilution gas or the carrier gas and the hydrogen to the SOFC stack.
9. The power generation apparatus with integrated CLP and SOFC of claim 8, wherein the anode fuel supply unit comprises: a first heat exchanger to drop a temperature of the hydrogen and heat the dilution gas or the carrier gas using a heat energy recycle from a heat exchange; a first bypass valve to bypass the hydrogen entering from the first heat exchanger; a suction pump to extract the hydrogen passing through the first bypass valve; a first flowmeter controlling a flow rate of the hydrogen from the suction pump; and a mixer receiving the hydrogen for which the flow rate is controlled by the first flowmeter and the dilution gas or the carrier gas heated by the first heat exchanger.
10. The power generation apparatus with integrated CLP and SOFC of claim 9, wherein the anode fuel supply unit further comprises: a hydrogen storage tank to store a portion of the hydrogen passing through the first bypass valve and used as a desired hydrogen source when the SOFC stack enters a shutdown process when the CLP device is shut down or malfunctioned; and a dust collector disposed between the first heat exchanger and the first bypass valve to perform a dust removal step on the hydrogen after cooling.
11. The power generation apparatus with integrated CLP and SOFC of claim 8, further comprising a gas supply unit to provide the dilution gas or the carrier gas to the anode fuel supply unit, wherein the gas supply unit comprises: a second bypass valve to bypass a nitrogen and a carbon dioxide exhausted from the first chamber, wherein the dilution gas or the carrier gas is selected from one of the nitrogen and the carbon dioxide; a second heat exchanger to heat the dilution gas or the carrier gas passing through the second bypass valve; and a third bypass valve disposed between the second bypass valve and the second heat exchanger to bypass the dilution gas or the carrier gas around the second heat exchanger.
12. The power generation apparatus with integrated CLP and SOFC of claim 1, further comprising an air supply unit, the air supply unit comprises: an air pump; a second flowmeter controlling an amount of the air from the air pump with an amount needed for the SOFC stack; a third flowmeter controlling the amount from the air pump with an amount needed for the CLP device; and a fourth bypass valve to divide the air from the second flowmeter.
13. The power generation apparatus with integrated CLP and SOFC of claim 12, further comprising an air intake pipe disposed in the second chamber and connected to the air supply unit to heat the air entering the air intake pipe from the fourth bypass valve via the carbon dioxide produced from the CLP device.
14. The power generation apparatus with integrated CLP and SOFC of claim 13, further comprising a hot box to heat the air passing through the air intake pipe and transferring the heated air to the SOFC stack.
15. An operation and control method of a power generation apparatus with integrated CLP (chemical looping process) and SOFC (solid oxide fuel cell), wherein the power generation apparatus comprises a chamber body, the chamber body has a first valve dividing the chamber body into a first chamber and a second chamber, a SOFC stack is disposed in the first chamber, and a CLP device is disposed in the second chamber, the operation method comprising: providing a fuel to the CLP device in the second chamber to produce a hydrogen and a carbon dioxide; opening the first valve such that the carbon dioxide produced by the CLP device passes through the open first valve and enters the first chamber to heat the SOFC stack; and transporting the hydrogen produced by the CLP device to the SOFC stack as an anode fuel of the SOFC stack.
16. The operation and control method of claim 15, further comprising: controlling a valve opening degree of the first valve to control a flow rate of the carbon dioxide entering the first chamber based on a temperature of the SOFC stack; and controlling a valve opening degree of a second valve to control a flow rate of the carbon dioxide exhausted from the first chamber based on the temperature of the SOFC stack, wherein the second valve is disposed in an opening of the first chamber discharging the carbon dioxide.
17. The operation and control method of claim 15, further comprising using an exhaust gas of the SOFC stack or the carbon dioxide exhausted from the first chamber as a steam heat source of the CLP device.
18. The operation and control method of claim 15, further comprising supplying a gas source of a dilute gas or a carrier gas to the SOFC stack, and a method of supplying the gas source comprises performing a heat exchange on the carbon dioxide exhausted from the first chamber using a nitrogen to heat the nitrogen as the gas source, or using the carbon dioxide exhausted from the first chamber as the gas source.
19. The operation and control method of claim 15, further comprising performing a heat exchange on a gas source of a dilute gas or a carrier gas in the SOFC stack by using the hydrogen produced from the CLP device to heat the gas source and drop a temperature of the hydrogen.
20. The operation and control method of claim 15, further comprising storing a portion of the hydrogen produced by the CLP device to provide the hydrogen to the SOFC stack when the CLP device is shut down or malfunctioned as a desired hydrogen source when the SOFC stack enters a shutdown process.
21. The operation and control method of claim 15, further comprising heating an air in an air inlet pipe disposed in the second chamber via the carbon dioxide produced by the CLP device or heating the air by performing a heat exchange on the air with an exhaust gas of the SOFC stack so as to use the heated air as an anode fuel of the SOFC stack.