TWI557981B - Power generation apparatus integrated clp and sofc and operation method thereof - Google Patents

Description

Power generation equipment integrating CLP and SOFC and operation method thereof

The present invention relates to a power generation apparatus, and more particularly to a power generation apparatus for integrating a chemical looping process (CLP) and a solid oxide fuel cell (SOFC) and a method of operating the same.

Solid oxide fuel cell system operating temperature is about 850 ° C, because this fuel cell needs to run stably in high temperature environment, the current system temperature rise or maintain the system operating environment temperature mode usually uses gas heater to meet the heat of the system demand. However, the use of gas heaters to maintain temperature is energy-intensive, so it needs to be operated in conjunction with a system with high-temperature gas production. By using its fuel supply requirements and effectively recovering the heat energy of high-temperature gas sources, the system can be achieved. The goal of energy saving and simplification.

The invention provides a power generation device integrating a chemical loop program and a solid oxide fuel cell, which can combine the effects of carbon dioxide capture, high energy utilization rate and high power generation efficiency.

The invention further provides an operation method for integrating a chemical circuit program and a power generation device for a solid oxide fuel cell, which can recycle waste heat.

The integrated chemical circuit program of the present invention and the power generation device of the solid oxide fuel cell include a cavity having a valve to divide the first and second chambers, and a solid oxide fuel cell disposed in the first chamber (solid An oxide fuel cell (SOFC) device and a chemical looping process (CLP) device disposed in the second chamber. The CLP device generates high temperature hydrogen and high temperature carbon dioxide, wherein the hydrogen acts as the anode fuel of the SOFC device, and the high temperature carbon dioxide enters the first chamber by the opening of the first valve to heat the SOFC device.

The method of operation of the present invention includes supplying a fuel to a CLP device of a power plant for generating hydrogen and carbon dioxide, wherein the power plant includes a cavity partitioned into a first and a second chamber by a first valve, and the CLP device is Set in the second chamber. Then, the first valve is opened to cause the carbon dioxide generated by the CLP device to enter the first chamber through the opened first valve to heat the SOFC device disposed in the first chamber. The hydrogen produced by the CLP unit is sent to the SOFC unit to serve as the anode fuel for the SOFC unit.

Based on the above, the present invention can be integrated with a solid oxide fuel cell by a chemical loop program, and is matched with a running interface configuration and a high-temperature steady state operation of a solid oxide fuel cell to have both carbon dioxide capture and high energy use rate. High power efficiency.

The above described features and advantages of the invention will be apparent from the following description.

1 is a simplified diagram of a power plant incorporating a chemical loop process (CLP) and a solid oxide fuel cell (SOFC) in accordance with a first embodiment of the present invention.

Referring to FIG. 1, the main systems in the power generating apparatus 10 of the present embodiment are all disposed in a cavity 100, and the cavity 100 has a valve 102 to divide it into a first chamber 104 and a second chamber 106, and A solid oxide fuel cell (SOFC) device 108 and a chemical loop program (CLP) device 110 in the power plant 10 are disposed within the first chamber 104 and the second chamber 106, respectively. When the fuel is supplied to the CLP device 110 of the power generating apparatus 10, high-temperature carbon dioxide and high-temperature hydrogen are generated, and the carbon dioxide temperature is about 900 ° C or higher. For example, the CLP device 110 uses a carbon-based fuel as a reaction material, and the iron-based oxygen carrier provides a source of oxygen source during the chemical reaction, thereby generating hydrogen and carbon dioxide. Then, by opening the valve 102, high temperature carbon dioxide can be introduced into the first chamber 102, thereby heating the SOFC device 108 disposed in the first chamber 102. The valve 102 in this embodiment can be designed differently according to requirements, as shown in the figure, with a high temperature resistant baffle, but the invention is not limited thereto, and the valve 102 (and the baffle) for the power generating device 10 is preferably It can withstand temperatures above 1000 °C, and its temperature range is, for example, between 1000 °C and 1800 °C. The hydrogen produced by the CLP device 110 is then delivered to the SOFC device 108 to serve as the anode fuel for the SOFC device 108. In the present embodiment, the first chamber 104 is located above the second chamber 106, but the invention is not limited thereto, as long as high temperature carbon dioxide can enter the first chamber 102 after the valve 102 is opened, either by The principle that the hot gas rises or is assisted by other air suction devices can be used to achieve the above effects.

In this embodiment, the high temperature carbon dioxide entering the first chamber 102 can heat the SOFC device 108 to an applicable operating temperature and can be determined by measuring the temperature of the SOFC device 108 (e.g., a fuel cell stack). Whether to continue heating or heating. For example, the valve opening of the valve 102 can be controlled based on the temperature of the SOFC device 108, thereby controlling the flow of carbon dioxide into the first chamber 102. The term "valve opening" in the text refers to the degree to which the valve is opened, that is, the valve opening degree is 0, the valve is fully closed, the valve opening degree is 100%, the valve is fully open, the valve opening is 50%, the valve is half open, and so on.

2 is a schematic diagram of a power plant for integrating a chemical loop process with a solid oxide fuel cell in accordance with a second embodiment of the present invention.

Referring to FIG. 2, the main system in the power generating device 20 of the present embodiment is disposed in a cavity 200, and the cavity 200 has a first valve 202 separating the first chamber 204 and the second chamber 206. The solid oxide fuel cell (SOFC) device 208 and the chemical circuit program (CLP) device in the power plant 20 are disposed in the first chamber 204 and the second chamber 206, respectively. In the present embodiment, the first chamber 204 may have a carbon dioxide discharge port 200a, and a second valve 210 is disposed beside the carbon dioxide discharge port 200a for opening or closing the carbon dioxide discharge port 200a. In addition, because the temperature of the carbon dioxide gas stream is extremely high, in order to avoid uneven distribution of the temperature of the SOFC device 208 to avoid the uneven distribution of the gas flow, thereby affecting the reaction efficiency, the SOFC device 208 in the first chamber 204 can be first and second. An air flow distributor 212 is added between the valves 202 and 210. When a high temperature carbon dioxide gas stream is desired to enter, the gas flow distribution can be achieved by the gas flow distributor 212 to achieve a uniformly dispersed flow field, such as a flat plate having a plurality of holes or other suitable design.

The CLP device may include a reduction reactor 214, an oxidation reactor 216, a burner 218, and a cyclone separator 220, which operate on the application of an oxygen carrier to a redox reaction in a chemical loop process, such as a carbon-based fuel. First, it is introduced into the fuel line 222, and a chemical reaction is performed in the reduction reactor 214 to generate high-temperature carbon dioxide. The high-temperature carbon dioxide will be discharged through the exhaust line 228, and the oxygen carrier will continue to fall into the oxidation reactor 216 while Steam is also introduced into the steam line 224 from the oxidation reactor 216 for a second chemical reaction. The exhaust line 228 can be discharged to the side, or the upper side and the side side are simultaneously discharged to the second chamber 206, and the discharged high-temperature carbon dioxide is merged into the first chamber 204 to be preheated or held as the SOFC device 208. The source of heat. The oxidation reaction will generate high temperature hydrogen, which will also be discharged from the oxidation reactor 216 into the hydrogen line 230. At this point, the unreacted oxygen carrier will continue to fall into the combustor 218 and pass air through the air line 226 to the combustor 218 for reaction, thereby reducing the oxygen carrier of the reaction, and then the oxygen carrier will enter. The cyclone separator 220 continues this chemical loop reaction procedure. The SOFC device 208 may include an anode line 232 for the anode fuel and a cathode line 234 for the cathode fuel, and the anode line 232 is in communication with the hydrogen line 230 of the CLP unit, thereby accepting hydrogen as the SOFC unit. 208 anode fuel.

In this embodiment, the first valve 202 and the second valve 210 can be designed with a high temperature resistant baffle to design an air flow path, so that when the first valve 202 and the second valve 210 are opened, the high temperature carbon dioxide gas flow passes through the first valve. 202 and uniformly distributes the airflow through the airflow distributor 212. At this time, the high temperature carbon dioxide gas flow is distributed around the SOFC device 208. After the high temperature airflow is used to heat the SOFC device 208 to reach the required operating temperature, the high temperature airflow will again pass through the airflow distribution. The device 212 enters the second valve 210 and then exits the first chamber 204. Moreover, the heating of the SOFC device 208 can be measured to determine whether to continue the heating. If the heating is to be continued, the first valve 202 and the second valve 210 are continuously turned on; otherwise, if the operating temperature of the SOFC device 208 has been reached, then The first valve 202 and the second valve 210 will be closed, and the flow rate of the high-temperature carbon dioxide gas flow into the first chamber 204 is determined by the opening or closing of the first valve 202 and the second valve 210. In addition, the flow rate of carbon dioxide out of the first chamber 204 can also be controlled by controlling the valve opening of the second valve 210. For example, when the SOFC device 208 is in the startup temperature rising phase, the first valve 202 and the second valve 210 are fully open; when the SOFC device 208 is in the temperature holding phase, the first valve 202 and the second valve 210 are also fully open; when the SOFC When the device 208 is in the load phase, the first valve 202 and the second valve 210 are both fully closed; when the SOFC device 208 is in the shutdown and cooling phase, the first valve 202 and the second valve 210 are both half open.

3 is a schematic diagram of a power generating apparatus incorporating a chemical loop procedure and a solid oxide fuel cell in accordance with a third embodiment of the present invention, wherein the same reference numerals as in FIG. 2 are used to denote the same or similar components.

Referring to FIG. 3, in addition to the components of FIG. 2, the exhaust gas of the SOFC device 208 or the carbon dioxide discharged from the first chamber 204 may be used as a steam heat source of the CLP device, and the gas is used as a steam heat source. Previously, the above exhaust or carbon dioxide may be heated first. For example, the steam required for the reaction in oxidation reactor 216 can be generated by a steam generator 300, and the heat source required for steam generator 300 is heated from first chamber 204 via a first heating unit 302, such as a heat exchanger. The exhausted carbon dioxide is provided; or alternatively, the exhaust gas discharged from the SOFC device 208 is heated by the second heating unit 304, wherein the second heating unit 304 is, for example, a device composed of the afterburner 306 and the heat exchanger 308, the exhaust gas may be It is the exhaust gas after the heat exchanger 308. As for the water source required for the steam generator 300, it may be provided by the water pump 310, but the present invention is not limited thereto. The water source required for the steam generator 300 can also be condensed with water collected by each heat exchanger.

Taking the operation of the SOFC device 208 as an example, when the SOFC device 208 is in the startup temperature rising phase, the exhaust gas of the SOFC device 208 and the carbon dioxide discharged from the first chamber 204 do not need to be heated; when the SOFC device 208 is in the temperature holding phase, the SOFC device 208 The exhaust gas and the carbon dioxide discharged from the first chamber 204 are maintained at a high temperature; when the SOFC device 208 is in the load phase, the exhaust gas of the SOFC device 208 and the carbon dioxide discharged from the first chamber 204 are maintained at a high temperature; when the SOFC device 208 is During the shutdown and cooling phase, the exhaust gas of the SOFC device 208 and the carbon dioxide discharged from the first chamber 204 do not need to be heated.

4 is a schematic diagram of a power generating apparatus incorporating a chemical loop procedure and a solid oxide fuel cell in accordance with a fourth embodiment of the present invention, wherein the same reference numerals as in FIG. 2 are used to denote the same or similar components.

Referring to FIG. 4, in addition to the components of FIG. 2, an anode fuel supply unit 400 may be included in the present embodiment for accepting dilution gas and hydrogen gas generated from the CLP device and supplying it to the SOFC device 208. Since the hydrogen concentration of the SOFC does not need to be too high, in the present embodiment, nitrogen or carbon dioxide may be used as the gas for diluting hydrogen, and the source of the nitrogen may be from a liquid nitrogen cylinder or a nitrogen generator. The anode fuel supply unit 400 described above may include a heat exchanger 402, a diverter valve 404, an exhaust pump 406, a flow meter 408, and a mixer 410. For example, the high temperature hydrogen gas stream generated in the chemical loop process enters heat exchanger 402 via hydrogen line 230. The heat exchanger 402 has at least two functions, the first is to lower the temperature of the high-temperature hydrogen gas to facilitate the subsequent gas dust removal step, and the second is to use the heat extracted by the heat exchange as the heating diluent gas. After cooling, the hydrogen gas can directly enter a dust remover 414 for dust removal step, and then enter the diverter valve 404; or by using a sieve to remove the powder when the fuel enters the fuel line 222, the dust removal effect is achieved, so the temperature is lowered. The hydrogen can also be passed directly into the diverter valve 404 for splitting. In the process, part of the hydrogen generated by the CLP device may be shunted through the diverter valve 404 and stored in the hydrogen storage tank 412 to serve as a source of hydrogen for the SOFC device 208 to enter the shutdown process when the CLP device is shut down or failed. Part of the hydrogen is transported to the back-end chemical process line for the manufacture of industrial or residential chemicals. Another portion of the hydrogen can be pumped into the pipeline using a pumping pump 406, and the flow meter 408 is used to control the amount of hydrogen required to flow into the mixer 410. The function of the mixer 410 is primarily to mix into the SOFC unit 208. The gas (dilution gas and hydrogen), when the gas is mixed there, will then enter the anode line 232 of the SOFC unit 208 as the fuel required for the anode. The flow meter 408 described above may be a mass flow meter or a mass flow controller (MFC).

The source of the above diluent gas may be nitrogen (N ₂ ) or carbon dioxide discharged from the first chamber 204. If nitrogen is used as the diluent gas, carbon dioxide discharged from the first chamber 204 may be exchanged with nitrogen (N ₂ ) to heat the nitrogen gas and lower the temperature of the carbon dioxide. When the temperature of the carbon dioxide gas stream is lowered, the carbon dioxide capture process can be performed. For example, a dilution gas supply unit 416 can be provided to supply the dilution gas to the heat exchanger 402 of the anode fuel supply unit 400, and the dilution gas supply unit 416 can include the heat exchanger 418 and the diverter valves 420 and 422.

When the diverter valve 420 selects nitrogen as the diluent gas, the nitrogen gas then enters the diverter valve 422, which primarily controls whether the nitrogen gas needs to be heated by the heat exchanger 418 for nitrogen heating. Nitrogen will pass through two heat exchangers in the entire power generation equipment, namely the heat exchanger 418 and the heat exchanger 402. The heat source of the heat exchanger 402 is mainly heated by hydrogen generated in the chemical loop program, and then supplied after being exchanged by heat exchange. Nitrogen and nitrogen are sent to the mixer 410 after being heated, but since the SOFC device 208 does not require too high temperature nitrogen during the initial temperature rise and pull, the nitrogen gas can be applied to the heat exchanger 418 by using the diverter valve 422; If the temperature of the nitrogen heated by the heat exchanger 402 does not reach the desired temperature, then the diverter valve 422 will be used to pass nitrogen through the heat exchanger 418 for a further nitrogen heating sequence. Here, the thermal energy of the heat exchanger 418 is taken from the carbon dioxide discharged from the first chamber 204. The heated nitrogen will be mixed with hydrogen in the desired ratio in the mixer 410 and then passed into the anode line 232.

When the diverter valve 420 selects carbon dioxide as the diluent gas, it can be obtained by cooling the high temperature carbon dioxide flowing out of the first chamber 204, and the high temperature carbon dioxide flowing out of the heat exchanger 418 reduces the temperature of the carbon dioxide to a trapable temperature, and then flows in. The diverter valve 420 is controlled from the diverter valve 420 to cause the carbon dioxide gas stream to enter the diverter valve 422. As described above for the nitrogen gas, if the carbon dioxide for dilution requires additional heating, the diverter valve 422 will be applied to pass the carbon dioxide through the heat exchanger 418. A further heating sequence; if the carbon dioxide for dilution does not require additional heating, the diverter valve 422 will be applied to bypass the heat exchanger 418. The heated carbon dioxide will be mixed with hydrogen in the desired ratio in the mixer 410 and then passed into the anode line 232.

Taking the operation of the SOFC device 208 as an example, when the SOFC device 208 is in the startup temperature rising phase, the dilution gas does not pass through the heat exchanger 418 but passes through the heat exchanger 402; when the SOFC device 208 is in the temperature holding phase, the dilution gas passes through the heat exchange. The 418, also passes through the heat exchanger 402; when the SOFC device 208 is in the load phase, the dilution gas passes through the heat exchanger 418 and the heat exchanger 402; when the SOFC device 208 is in the shutdown cooling phase, the dilution gas does not pass through the heat exchanger 418, However, it will pass through the heat exchanger 402.

Figure 5 is a schematic diagram of a power generating apparatus incorporating a chemical loop procedure and a solid oxide fuel cell in accordance with a fifth embodiment of the present invention, wherein the same reference numerals as in Figure 2 are used to denote the same or similar components.

Referring to FIG. 5, in addition to the components of FIG. 2, an air supply unit 500 may be included in the present embodiment for supplying air to the burner 218 of the CLP device and to the SOFC device 208, respectively. The air supply unit 500 described above may include an air pump 502, flow meters 504 and 506, and a diverter valve 508. For example, the cathode fuel of the SOFC device 208 is air, the source of which can be extracted by the air pump 502, wherein the air pump 502 can also be replaced with a large air reservoir, an air compressor or a blower. The extracted air stream will be used in two parts, one for the cathode fuel of the SOFC unit 208 and the other for the reaction air required by the burner 218 in the chemical loop procedure. While flow meter 504 is the amount of air required to match SOFC device 208, the amount of air from air pump 502 is controlled; flow meter 506 is the amount of air required to match the CLP device to control the amount of air from air pump 502.

When used as the cathode fuel of the SOFC device 208, the flow rate is first controlled by the flow meter 504 and enters the diverter valve 508, wherein the flow meter 504 can be replaced with a large air reservoir and coupled to a mass flow controller (MFC) at the rear end. The above-mentioned diverter valve 508 can divide the air into two air flows, one into an air intake pipe 516 disposed in the second chamber 206 and connected to the air supply unit 500, and the other as the SOFC device 208 for warming or load operation. The air for temperature adjustment. The air intake line 516 can be coiled around the inner wall of the cavity 200 to increase the preheating of the air. The amount of preheating can be determined by the number of windings of the pipeline. When air enters the air intake line 516, the air flowing through the interior of the air intake line 516 is affected by the high temperature carbon dioxide generated by the CLP device for the first heating. The air can then be heat exchanged in the hot box 510 using the exhaust of the SOFC unit 208 to heat the air and use the heated air as the cathode fuel. In detail, if the temperature of the air in the initial operation of the SOFC device 208 is too high, it is necessary to mix with the air for temperature adjustment before entering the hot box 510 and then enter the hot box 510. The hot box 510 includes two units, an afterburner 512 and a heat exchanger 514, wherein the afterburner 512 can re-burn the unreacted exhaust gas, and then exchange heat through the heat exchanger 514 to extract heat. The second heating is used by the air in the air intake line 516, and then enters the cathode line 234 of the SOFC unit 208.

If the air from the air pump 502 is the reactive air required for the burner 218 in the chemical circuit program, the flow meter 506 will be applied to control the flow to be entered into the burner. The flow meter 506, such as a mass flow meter, or a large air storage tank, can be replaced with a rear end mass flow controller (MFC).

Taking the operation of the SOFC device 208 as an example, when the SOFC device 208 is in the startup temperature rising phase, the air is heated in the air intake line 516, but the afterburner 512 is not actuated; when the SOFC device 208 is in the temperature holding phase, the air is in the air. The intake line 516 is heated and also heated by the afterburner 512; when the SOFC unit 208 is in the load phase, air is heated in the air intake line 516 and the afterburner 512; when the SOFC unit 208 is in the shutdown and cooling stage, the air The air intake line 516 is heated, but the afterburner 512 is not actuated.

Figure 6 is a schematic diagram of a power generating apparatus incorporating a chemical loop procedure and a solid oxide fuel cell in accordance with a sixth embodiment of the present invention, wherein the same reference numerals as in Figures 2 through 5 are used to designate the same or similar components.

In FIG. 6, the hot box 510 for heating the air may simultaneously serve as a second heating unit (such as 304 of FIG. 3) that supplies the heat source of the steam generator 300, such as the afterburner 512 and the heat exchanger 514 in the hot box 510. The same is true, before the air intake line 516 can provide sufficient gas preheating, the high temperature exhaust heat generated by the hot box 510 can be transferred to the steam generator 300 to generate sufficient steam for the oxidation of the chemical loop program. Reactor 216 produces hydrogen.

The heat exchanger 302 for heating the heat source required for the steam generator 300 can also serve as a heat exchanger for heating the dilution gas (Fig. 4, 418); that is, the carbon dioxide gas stream after passing through the heat exchanger 302. , can be shunted through the shunt 600. At this time, if carbon dioxide is to be used as the diluent gas, the carbon dioxide gas stream can be controlled from the diverter valve 600 to enter the diverter valve 420; if carbon dioxide is to be used as a heat source for the steam generator 300, it can be controlled from the diverter valve 600. A carbon dioxide gas stream is supplied to the steam generator 300. In addition, the low temperature carbon dioxide emitted by the steam generator 300 can also be returned to the position of the diverter valve 420 as a source of diluent gas.

In summary, the present invention can realize the high-temperature operating environment without using an electronic gas heater by integrating the chemical loop program and the solid oxide fuel cell system, and can recycle all waste heat in the power generation equipment, thereby achieving It combines the effects of carbon dioxide capture, high energy use and high power generation efficiency.

Although the present invention has been disclosed in the above embodiments, it is not intended to limit the present invention, and any one of ordinary skill in the art can make some changes and refinements without departing from the spirit and scope of the present invention. The scope of the invention is defined by the scope of the appended claims.

10, 20‧‧‧Power equipment integrating CLP and SOFC
100, 200‧‧‧ cavity
102, 202, 210‧‧‧ valves
104, 204‧‧‧ first chamber
106, 206‧‧‧ second chamber
108, 208‧‧‧ solid oxide fuel cell device
110‧‧‧Chemical loop program device
212‧‧‧Airflow distributor
214‧‧‧Reduction reactor
216‧‧‧Oxidation reactor
218‧‧‧ burner
220‧‧‧Cyclone separator
222‧‧‧fuel pipeline
224‧‧‧Steam pipeline
226‧‧‧Air line
228‧‧‧Exhaust line
230‧‧‧Hydrogen pipeline
232‧‧‧Anode line
234‧‧‧Cathode piping
300‧‧‧Steam generator
302‧‧‧First heating unit
304‧‧‧second heating unit
306, 512‧‧‧ afterburner
308, 402, 418, 514‧ ‧ heat exchangers
310‧‧‧Water pump
400‧‧‧Anode fuel supply unit
404, 420, 422, 508, 600‧‧‧ diverter valves
406‧‧‧Exhaust pump
408, 504, 506‧‧‧ flowmeter
410‧‧‧ Mixer
412‧‧‧ Hydrogen storage tank
414‧‧‧Dust collector
416‧‧‧Dilution gas supply unit
500‧‧‧Air supply unit
502‧‧‧Air pump
510‧‧‧ hot box

BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic diagram of a power generating apparatus incorporating a chemical loop procedure and a solid oxide fuel cell in accordance with a first embodiment of the present invention. 2 is a schematic diagram of a power plant for integrating a chemical loop process with a solid oxide fuel cell in accordance with a second embodiment of the present invention. 3 is a schematic diagram of a power plant for integrating a chemical loop process with a solid oxide fuel cell in accordance with a third embodiment of the present invention. 4 is a schematic diagram of a power generating apparatus integrating a chemical loop program and a solid oxide fuel cell in accordance with a fourth embodiment of the present invention. Figure 5 is a schematic illustration of a power plant incorporating a chemical loop procedure and a solid oxide fuel cell in accordance with a fifth embodiment of the present invention. Figure 6 is a schematic illustration of a power plant incorporating a chemical loop procedure and a solid oxide fuel cell in accordance with a sixth embodiment of the present invention.

10‧‧‧Power equipment integrating CLP and SOFC

100‧‧‧ cavity

102‧‧‧ valve

104‧‧‧First chamber

106‧‧‧Second chamber

108‧‧‧Solid oxide fuel cell device

110‧‧‧Chemical loop program device

Claims (33)

A power generation device integrating a chemical loop program and a solid oxide fuel cell, comprising: a cavity having a first valve to divide the cavity into a first chamber and a second chamber; a solid oxide fuel cell (solid oxide a fuel cell (SOFC) device disposed in the first chamber; and a chemical looping process (CLP) device disposed in the second chamber, the CLP device generating hydrogen and carbon dioxide, wherein the hydrogen gas As the anode fuel of the SOFC device, the carbon dioxide is introduced into the first chamber by the opening of the first valve to heat the SOFC device. The integrated chemical circuit program of claim 1, wherein the first chamber is located above the second chamber. The integrated chemical circuit program of claim 1, wherein the first chamber further comprises a carbon dioxide discharge port. The integrated chemical circuit program and the power generating device for a solid oxide fuel cell according to claim 3, further comprising a second valve disposed adjacent to the carbon dioxide discharge port for opening or closing the carbon dioxide discharge port. The integrated chemical circuit program and the power generating device for a solid oxide fuel cell according to claim 1, further comprising a gas flow distributor disposed in the first chamber and interposed between the first valve and the SOFC device between. The integrated chemical circuit program of claim 5, wherein the gas flow distributor is a flat plate having a plurality of holes. The integrated chemical circuit program according to claim 1, wherein the CLP device includes a steam line for introducing steam, a fuel line for introducing fuel, and discharging hydrogen gas. The hydrogen pipeline and the air pipeline for air. The integrated chemical circuit program and the power generating apparatus for a solid oxide fuel cell according to claim 7, wherein the SOFC device includes an anode line for introducing an anode fuel and a cathode line for introducing a cathode fuel, and The anode line is in communication with the hydrogen line of the CLP unit. The integrated chemical circuit program and the power generating device for a solid oxide fuel cell according to claim 1, further comprising a steam generator for supplying the CLP device steam. The integrated chemical circuit program of claim 9 and the power generating device for a solid oxide fuel cell, further comprising a first heating unit for heating carbon dioxide discharged from the first chamber and transmitting the steam to the steam Generator. The integrated chemical circuit program and the power generating device for a solid oxide fuel cell according to claim 9 further comprising a second heating unit for heating the exhaust gas discharged from the SOFC device and transmitting the same to the steam generator. . The integrated chemical circuit program and the power generating device for a solid oxide fuel cell as described in claim 9 further include a water pump for supplying water to the steam generator. The integrated chemical circuit program and the power generating device for a solid oxide fuel cell according to claim 1, further comprising an anode fuel supply unit for receiving the dilution gas and the hydrogen gas generated from the CLP device, and supplying To the SOFC device. The power plant of the integrated chemical circuit program and the solid oxide fuel cell according to claim 13, wherein the anode fuel supply unit comprises: a first heat exchanger for reducing the temperature of the hydrogen and applying heat exchange The extracted heat energy heats the dilution gas; the first diverter valve is configured to divert the hydrogen gas entering from the first heat exchanger; and the pumping pump is configured to extract the hydrogen gas passing through the first diverter valve; a flow meter that controls a flow rate of the hydrogen gas from the pumping pump; and a mixer that receives the hydrogen gas controlled by the first flow meter and the diluent gas heated by the first heat exchanger. The integrated chemical circuit program of claim 14, wherein the anode fuel supply unit further comprises a hydrogen storage tank for storing the portion passing through the first diverter valve. Hydrogen, as a source of hydrogen required for the SOFC unit to enter the shutdown process when the CLP unit is shut down or fails. The power plant of the integrated chemical circuit program and the solid oxide fuel cell according to claim 14, wherein the anode fuel supply unit further comprises a dust collector disposed on the first heat exchanger and the first diverter valve Between the steps, the dust removal step is performed on the cooled hydrogen gas. The integrated chemical circuit program of claim 13 and the power generating device of the solid oxide fuel cell, further comprising a diluent gas supply unit for supplying the diluent gas to the anode fuel supply unit, and the diluent gas The supply unit includes: a second diverter valve for diverting nitrogen gas and carbon dioxide discharged from the first chamber, wherein the diluent gas is one selected from the group consisting of the nitrogen gas and the carbon dioxide; Heating the diluent gas passing through the second diverter valve; and a third diverter valve disposed between the second diverter valve and the second heat exchanger for bypassing the dilute gas Switch. The integrated chemical circuit program and the power generating device for a solid oxide fuel cell according to claim 1, further comprising an air supply unit for supplying air to the CLP device and the SOFC device, respectively. The power plant of the integrated chemical circuit program and the solid oxide fuel cell according to claim 18, wherein the air supply unit comprises: an air pump; and the second flow meter, the amount of air required to match the SOFC device, Controlling the amount of the air from the air pump; a third flow meter that controls the amount of the air from the air pump in conjunction with the amount of air required by the CLP device; and a fourth diverter valve for diverting The air from the second flow meter. The integrated chemical circuit program and the power generating device for a solid oxide fuel cell according to claim 19, further comprising an air intake pipe disposed in the second chamber and connected to the air supply unit to borrow The carbon dioxide produced by the CLP device heats the air entering the air intake line from the fourth diverter valve. The integrated chemical circuit program and the power generating device for a solid oxide fuel cell according to claim 20, further comprising a heat box for heating the air passing through the air intake pipe and transmitting the heated Air to the SOFC unit. The integrated chemical circuit program and the power generation device for a solid oxide fuel cell according to claim 1, wherein the CLP device uses a carbon-based fuel and an iron-based oxygen carrier as a reaction raw material to generate the hydrogen gas Carbon dioxide. A method of operating a power plant that integrates a chemical loop process with a solid oxide fuel cell, wherein the power plant includes a cavity having a first valve that divides it into a first chamber and a second chamber, And a solid oxide fuel cell (SOFC) device is disposed in the first chamber, and a chemical looping process (CLP) device is disposed in the second chamber, the operation method includes: Supplying fuel to the CLP device in the second chamber to generate hydrogen and carbon dioxide; opening the first valve, causing the carbon dioxide generated by the CLP device to enter the first chamber through the opened first valve to heat The SOFC device; and the hydrogen gas generated by the CLP device is delivered to the SOFC device to serve as an anode fuel for the SOFC device. The method of operation of claim 23, further comprising controlling a valve opening of the first valve to control a flow rate of the carbon dioxide into the first chamber according to a temperature of the SOFC device. The operating method of claim 23, further comprising controlling a valve opening degree of a second valve to control a flow rate of the carbon dioxide to discharge the first chamber according to a temperature of the SOFC device, wherein the second A valve is disposed at an opening of the first chamber to discharge the carbon dioxide. The method of operation of claim 23, further comprising using the exhaust gas of the SOFC device or the carbon dioxide discharged from the first chamber as a steam heat source of the CLP device. The method of operation of claim 26, wherein before the use of the off-gas or the carbon dioxide discharged from the first chamber as the steam heat source, further comprising heating the tail gas or the carbon dioxide. The method of operation of claim 23, further comprising: performing heat exchange of the carbon dioxide discharged from the first chamber with nitrogen gas to heat the nitrogen gas and lower the temperature of the carbon dioxide, wherein the heated The nitrogen gas is a source of dilution gas for the SOFC device. The method of operation of claim 23, further comprising using the carbon dioxide discharged from the first chamber as a source of diluent gas for the SOFC device. The operation method of claim 23, further comprising performing heat exchange of the dilute gas source of the SOFC device using the hydrogen generated by the CLP device to heat the diluent gas source and lower the temperature of the hydrogen gas. . The operating method of claim 23, further comprising storing a portion of the hydrogen generated by the CLP device to be supplied to the SOFC device when the CLP device is shut down or malfunctioning, and entering the shutdown program as the SOFC device A source of hydrogen is required. The operating method of claim 23, further comprising heating the air disposed in the air intake duct of the second chamber by the carbon dioxide generated by the CLP device, and heating the Air acts as the cathode fuel for the SOFC device. The method of operation of claim 23, further comprising exchanging heat with air using the exhaust gas of the SOFC device to heat the air and using the heated air as a cathode fuel of the SOFC device.