阅读说明：本技术 一种固体氧化物燃料电池与工艺加热炉的热电联产方法及装置 (Cogeneration method and device for solid oxide fuel cell and process heating furnace ) 是由 张小康 韩保平 曲志祎 侯丹丹 张周岁 谢飚 于 2019-08-20 设计创作，主要内容包括：本发明公开了一种固体氧化物燃料电池与工艺加热炉的热电联产方法及装置,其燃料和燃烧空气首先进入合成气发生器,用以产生燃料电池发电所需要的高温合成气。生成的高温合成气通过换热器与燃料电池电化学反应所需要的空气进行换热,使合成气及电堆空气的温度均满足燃料电池发电的需要。换热后的合成气以及电堆空气分成多个支路、分别通往各个电堆的入口,进行燃料电池发电。完成发电反应的乏合成气及乏空气分别合并,进入工艺加热炉中进行燃烧、换热,以充分利用乏合成气及乏空气中剩余的化学能及余热。本发明在充分利用燃料气中的高位能量的同时,利用了工艺加热炉回收余热,可大幅节省同等项目的建设投资,并大幅提高燃料的经济价值。(The invention discloses a method and a device for cogeneration of a solid oxide fuel cell and a process heating furnace, wherein fuel and combustion air firstly enter a synthesis gas generator to generate high-temperature synthesis gas required by the fuel cell for power generation. The generated high-temperature synthesis gas exchanges heat with air required by the electrochemical reaction of the fuel cell through the heat exchanger, so that the temperature of the synthesis gas and the air of the electric pile both meet the power generation requirement of the fuel cell. The synthesis gas and the electric pile air after heat exchange are divided into a plurality of branches which are respectively led to the inlets of the electric piles to carry out fuel cell power generation. And respectively combining the exhausted synthetic gas and the exhausted air which finish the power generation reaction, and entering the technical heating furnace for combustion and heat exchange so as to fully utilize the residual chemical energy and the residual heat in the exhausted synthetic gas and the exhausted air. The invention makes full use of the high-level energy in the fuel gas, and simultaneously utilizes the process heating furnace to recover the waste heat, thereby greatly saving the construction investment of the same project and greatly improving the economic value of the fuel.)

1. A combined heat and power generation method for solid oxide fuel cell and process heating furnace features that the fuel and oxidizing medium are first introduced into synthetic gas generator to generate CO and CO, which are needed by solid oxide fuel cellH₂High temperature synthesis gas as a main component; the generated high-temperature synthesis gas exchanges heat with the air of the electric pile required by the electrochemical reaction of the solid oxide fuel cell through the heat exchanger, so that the temperatures of the high-temperature synthesis gas and the air of the electric pile both meet the power generation requirement of the solid oxide fuel cell; the synthesis gas after heat exchange and the air of the electric pile are divided into a plurality of branches which are respectively led to the inlets of the solid oxide fuel cells to carry out the power generation of the solid oxide fuel cells; and respectively combining the exhausted synthetic gas and the exhausted air which finish the power generation reaction, and entering the technical heating furnace for combustion and heat exchange so as to fully utilize the residual chemical energy and the residual heat in the exhausted synthetic gas and the exhausted air.

2. The method for co-generation of heat and power between a solid oxide fuel cell and a process heating furnace according to claim 1, wherein the fuel is one or a mixture of two or more of fuel oil, natural gas, domestic biogas, refinery pipe network gas, low-pressure gas, coke oven gas and raw coke oven gas.

3. The method of claim 2, wherein the sulfur content of the fuel oil, natural gas, biogas for civil use, refinery pipe network gas, low pressure gas, coke oven gas, and raw coke oven gas is strictly controlled.

4. The method for co-generating heat and power for a solid oxide fuel cell and a process heater of claim 1, wherein the oxidizing medium is pure oxygen, oxygen-enriched air, or air.

5. The method for co-generation of heat and power for a solid oxide fuel cell and a process heater as claimed in claim 1, wherein the temperature of the high temperature syngas at the outlet of the syngas generator is 800-1300 ℃.

6. A co-generation process of a solid oxide fuel cell and a process heater in accordance with claim 1, wherein a load adjusting burner is additionally provided in the process heater, and independent fuel gas and air inlets are provided to meet the load adjustment requirements of the heater under fluctuating conditions of the process equipment and the fuel cell.

7. A cogeneration device of a solid oxide fuel cell and a process heating furnace is characterized by comprising a synthesis gas generator, a heat exchanger, a plurality of solid oxide fuel cell groups and a process heating furnace, wherein a fuel inlet on the synthesis gas generator is connected with a fuel source through a fuel input pipe, an oxidizing medium inlet on the synthesis gas generator is connected with an oxidizing medium source through an oxidizing medium input pipe, a high-temperature synthesis gas outlet of the synthesis gas generator is connected with a high-temperature synthesis gas inlet of the heat exchanger through a high-temperature synthesis gas conveying pipe, a pile air inlet of the heat exchanger is connected with an air source through a pile air input pipe, a synthesis gas outlet of the heat exchanger is connected with a synthesis gas output header pipe, and a pile air outlet of the heat exchanger is connected with a pile air output header pipe; the synthesis gas output main pipe and the electric pile air output main pipe are respectively provided with a plurality of synthesis gas input branch pipes and a plurality of electric pile air input branch pipes, each synthesis gas input branch pipe and the corresponding electric pile air input branch pipe are respectively connected with a synthesis gas input port and an electric pile air input port of a solid oxide fuel battery pack, spent synthesis gas output ports of all the solid oxide fuel battery packs are respectively connected with a spent synthesis gas output main pipe through a spent synthesis gas output branch pipe, and spent air output ports of all the solid oxide fuel battery packs are respectively connected with a spent air output main pipe through a spent air output branch pipe; the exhausted synthetic gas output main pipe and the exhausted air output main pipe are also respectively connected with an exhausted synthetic gas input port and an exhausted air input port of the process heating furnace.

8. The solid oxide fuel cell and process furnace cogeneration apparatus of claim 7, wherein said process furnace is further provided with a conditioning fuel inlet and a conditioning combustion air inlet, said conditioning fuel inlet being connected to a fuel source through a conditioning fuel inlet pipe, and said conditioning combustion air inlet being connected to an air source through a conditioning combustion air inlet pipe.

9. The solid oxide fuel cell and process furnace cogeneration apparatus of claim 7, wherein said syngas generator is a hydro-carbon reformer or a partial oxidation syngas generator, preferably a partial oxidation syngas generator.

10. The solid oxide fuel cell and process furnace cogeneration apparatus of claim 7, wherein said heat exchanger is a plate heat exchanger or a tube bundle heat exchanger.

Technical Field

The invention belongs to the field of fuel cell power generation, particularly relates to a Solid Oxide Fuel Cell (SOFC) power generation system for carrying out heat and power cogeneration with a petrochemical heating furnace, and particularly relates to a heat and power cogeneration method and a heat and power cogeneration device for a solid oxide fuel cell and a process heating furnace.

Background

A fuel cell is a device that can directly convert chemical energy in fuel into electrical energy. Compared with the traditional combustion-based fire power generation mode, the device is cleaner and more efficient, and can be more flexibly applied to occasions with medium and low power generation scales. Moreover, a Solid Oxide Fuel Cell (SOFC) among fuel cells is more suitable for being coupled with other industries because it is suitable for syngas with CO components, has the advantages of high conversion efficiency, all-solid structure, suitability for various fuels, and the like.

Existing Solid Oxide Fuel Cells (SOFC) can only achieve power generation efficiency of around 50%, while spent syngas leaving the fuel cell stack still contains significant amounts of active components, such as H₂、CO、CO₂And CH₄And the temperature is still about 600-750 ℃. The spent air leaving the fuel cell stack also contains residual O₂And the temperature is about 600 ℃ and 750 ℃. How to utilize the residual low-grade energy greatly affects the economy of fuel cell power generation, and becomes a limiting factor for large-scale application of fuel cells.

In industries such as oil refining, petrochemical industry, coal chemical industry and the like, a large number of heating furnaces are arranged in the technical process to heat technical materials. The heating furnace uses refinery pipe network gas, natural gas, fuel oil and the like as fuels, and the combusted flue gas heats materials in a heat exchange mode. The heating furnace is often a high energy consuming device in the process plant, and the total energy consumption generally accounts for 30-70% of the total energy consumption of the plant. The high energy consumption of the heating furnace also makes the energy-saving technology related to the heating furnace highly attach attention, and at present, the fuel thermal efficiency of large and medium-sized heating furnaces in the petrochemical industry can generally reach 90% -92%.

Although the heating furnace is already popularRelatively high fuel thermal efficiency is achieved, but the fuel is used to heat a process medium, typically only 500 ℃, at a theoretical combustion temperature of approximately 2000 ℃There is a significant penalty in terms of (2). How to use the combustion energy of the fuel to generate high-grade energy (such as power generation) firstly, and then use the residual low-grade waste heat to heat materials, so that the process materials are heated, and high-grade electric energy is generated, and the maximum value of the fuel is exerted.

According to the above-mentioned ideas, the petrochemical industry has tried the idea of cogeneration of a gas turbine and a large heating furnace, i.e. fuel is firstly combusted in a flue gas turbine to generate electricity, and the discharged flue gas enters a process heating furnace to further recover heat. The idea is once applied to large ethylene cracking furnaces, large atmospheric and vacuum heating furnaces and the like, and good economic benefit is achieved. However, due to the high investment, high failure rate, complex operation switching and the like of the gas turbine, the technology is not generally popularized and used in the industry, and is not applied to a large number of medium and small-sized heating furnaces.

Disclosure of Invention

One of the objectives of the present invention is to provide a method for co-generation of solid oxide fuel cell and process heating furnace, which utilizes Solid Oxide Fuel Cell (SOFC) and petrochemical heating furnace to perform co-generation of heat and power to maximize fuel value.

The second purpose of the invention is to provide a device for realizing the cogeneration method of the solid oxide fuel cell and the process heating furnace.

The CO-generation method of the solid oxide fuel cell and the process heating furnace as the first aspect of the present invention first feeds fuel and oxidizing medium into the syngas generator for generating CO and H required for the solid oxide fuel cell power generation₂High temperature synthesis gas as a main component; the generated high-temperature synthesis gas passes through a heat exchanger to be in contact with the air of the electric pile required by the electrochemical reaction of the solid oxide fuel cellHeat exchange is carried out, so that the temperatures of the high-temperature synthesis gas and the air of the electric pile meet the power generation requirement of the solid oxide fuel cell; the synthesis gas after heat exchange and the air of the electric pile are divided into a plurality of branches which are respectively led to the inlets of the solid oxide fuel cells to carry out the power generation of the solid oxide fuel cells; and respectively combining the exhausted synthetic gas and the exhausted air which finish the power generation reaction, and entering the technical heating furnace for combustion and heat exchange so as to fully utilize the residual chemical energy and the residual heat in the exhausted synthetic gas and the exhausted air.

In a preferred embodiment of the invention, the fuel is one or a mixture of any two or more of fuel oil, natural gas, civil biogas, refinery pipe network gas, low-pressure gas, coke oven gas and crude gas.

In a preferred embodiment of the present invention, the sulfur content of fuel oil, natural gas, domestic biogas, refinery pipe network gas, low pressure gas, coke oven gas, raw gas should be strictly controlled in consideration of possible poisoning of sulfur to the fuel cell electrodes and electrolyte.

In a preferred embodiment of the invention, the oxidizing medium is pure oxygen, oxygen-enriched air or air. Air is preferred to reduce the operating costs of the system.

In a preferred embodiment of the present invention, the high temperature syngas temperature at the syngas generator outlet is 800-1300 ℃. The specific outlet temperature is selected to meet the requirements of the galvanic pile on the composition and temperature of the synthesis gas and the heat exchange requirement on the temperature of the air inlet.

In a preferred embodiment of the present invention, the high temperature syngas at the outlet of the partial oxidation syngas generator comprises the following main components: h₂、CO、N₂、CO₂And the remaining CH₄、O₂Etc., the specific composition depending on the composition of the fuel and the operating temperature and pressure of the syngas generator. Wherein N is₂、CO₂And can pass through the stack without adversely affecting the stack, while other components can participate in the electrochemical reaction for power generation by the fuel cell.

In a preferred embodiment of the present invention, the synthesis gas and the air for the stack after heat exchange are divided into required branch pipes according to the number of the fuel cell stacks, and the branch pipes are respectively fed into the fuel cell stacks to generate electricity. And respectively combining the exhausted synthetic gas and the exhausted air after power generation, and leading the combined gas to a heating furnace for further energy recovery.

In a preferred embodiment of the invention, a proportion of H in the high temperature synthesis gas entering the fuel cell is based on the performance of the fuel cell₂CO can participate in the electrochemical reaction, and the rest of unreacted H₂、CO、CH₄And the like, can be continuously combusted in the heating furnace to continuously recover energy. The spent air leaving the fuel cell still contains residual O₂Can be continuously used as combustion improver in the heating furnace for fuel combustion.

In a preferred embodiment of the invention, in order to ensure that the thermal load of the furnace can meet the possible regulation requirements of the process unit, the furnace is additionally provided with a load regulation burner, and independent fuel gas and air inlets are adopted, so that the load regulation requirements of the furnace can be met under the condition of fluctuation of the process unit and the fuel cell.

The cogeneration device of the solid oxide fuel cell and the process heating furnace as the second aspect of the invention comprises a synthesis gas generator, a heat exchanger, a plurality of solid oxide fuel cell groups and a process heating furnace, wherein a fuel inlet on the synthesis gas generator is connected with a fuel source through a fuel input pipe, an oxidizing medium inlet on the synthesis gas generator is connected with an oxidizing medium source through an oxidizing medium input pipe, a high-temperature synthesis gas outlet of the synthesis gas generator is connected with a high-temperature synthesis gas inlet of the heat exchanger through a high-temperature synthesis gas conveying pipe, a stack air inlet of the heat exchanger is connected with an air source through a stack air input pipe, a synthesis gas outlet of the heat exchanger is connected with a synthesis gas output header pipe, and a stack air outlet of the heat exchanger is connected with a stack air output header pipe; the synthesis gas output main pipe and the electric pile air output main pipe are respectively provided with a plurality of synthesis gas input branch pipes and a plurality of electric pile air input branch pipes, each synthesis gas input branch pipe and the corresponding electric pile air input branch pipe are respectively connected with a synthesis gas input port and an electric pile air input port of a solid oxide fuel battery pack, spent synthesis gas output ports of all the solid oxide fuel battery packs are respectively connected with a spent synthesis gas output main pipe through a spent synthesis gas output branch pipe, and spent air output ports of all the solid oxide fuel battery packs are respectively connected with a spent air output main pipe through a spent air output branch pipe; the exhausted synthetic gas output main pipe and the exhausted air output main pipe are also respectively connected with an exhausted synthetic gas input port and an exhausted air input port of the process heating furnace.

In a preferred embodiment of the invention, a conditioning fuel inlet and a conditioning combustion air inlet are also provided on the process heating furnace, the conditioning fuel inlet being connected to a fuel source via a conditioning fuel inlet line, and the conditioning combustion air inlet being connected to an air source via a conditioning combustion air inlet line.

In a preferred embodiment of the invention, the synthesis gas generator is a water-hydrocarbon reformer or a partial oxidation synthesis gas generator, preferably a partial oxidation synthesis gas generator.

In a preferred embodiment of the invention, the heat exchanger is used for exchanging heat between the high-temperature synthesis gas and the air for the electric pile, so that the temperature of the synthesis gas and the air for the electric pile after heat exchange can meet the requirement of an inlet of the electric pile. The heat exchanger may be of the plate or tube bundle type, depending on the particular process design in relation to throughput, heat exchange capacity.

In conclusion, the solid oxide fuel cell is combined with the petrochemical heating furnace, and the combination of a synthesis gas generator, a heat exchanger, a fuel cell set and a heating furnace is adopted, so that the aims of cogeneration and improvement of the economic value of the fuel are fulfilled.

Drawings

Fig. 1 is a basic process flow diagram for cogeneration of a Solid Oxide Fuel Cell (SOFC) and a petrochemical heating furnace.

FIG. 2 is a flow chart of a 0.9MW conventional furnace process.

Fig. 3 is a flow chart of the co-generation process of the 0.9MW heating furnace and the SOFC fuel cell.

Detailed Description

The invention is described in detail below with reference to the drawings and the detailed description.

Referring to fig. 1, fig. 1 is a basic process flow diagram for co-generation of heat and power with a Solid Oxide Fuel Cell (SOFC) and a petrochemical heating furnace.

The cogeneration unit of solid oxide fuel cells and process furnaces shown in fig. 1 consists of a syngas generator 10, a heat exchanger 20, several solid oxide fuel cell stacks 30 and a process furnace 40.

The fuel inlet 11 of the syngas generator 10 is connected to a fuel source through a fuel inlet pipe 50, the oxidizing medium inlet 12 of the syngas generator 10 is connected to an oxidizing medium source through an oxidizing medium inlet pipe 60, and the high-temperature syngas outlet 13 of the syngas generator 10 is connected to the high-temperature syngas inlet 21 of the heat exchanger 20 through a high-temperature syngas duct 70.

The stack air inlet 22 of the heat exchanger 20 is connected with an air source through a stack air input pipe 80, the synthesis gas outlet 23 of the heat exchanger 20 is connected with a synthesis gas output manifold 90, and the stack air outlet 24 of the heat exchanger 20 is connected with a stack air output manifold 90 a.

A plurality of synthesis gas input branch pipes 91 and a plurality of electric pile air input branch pipes 91a are respectively arranged on the synthesis gas output header pipe 90 and the electric pile air output header pipe 90a, each synthesis gas input branch pipe 91 and the corresponding electric pile air input branch pipe 91a are respectively connected with a synthesis gas input port 31 and an electric pile air input port 32 of one solid oxide fuel battery pack 30, a spent synthesis gas output port 33 of all the solid oxide fuel battery packs 30 is respectively connected with a spent synthesis gas output header pipe 100 through one spent synthesis gas output branch pipe 110, and spent air output ports 34 of all the solid oxide fuel battery packs 30 are respectively connected with a spent air output header pipe 200 through one spent synthesis gas output branch pipe 210; the spent synthesis gas output main pipe 100 and the spent air output main pipe 200 are also respectively connected with a spent synthesis gas input port 41 and a spent air input port 42 of the process heating furnace 40.

Solid oxygen is carried out by utilizing the solid oxide fuel cell and the combined heat and power generation device of the process heating furnaceThe combined heat and power generation method of the chemical fuel cell and the process heating furnace comprises the following steps: the fuel and oxidizing medium are first introduced into the syngas generator 10 through the fuel inlet line 50 and the oxidizing medium inlet line 60 to produce the CO and H required for solid oxide cell power generation₂High temperature synthesis gas as a main component; the generated high-temperature synthesis gas is input into the heat exchanger 20 through a high-temperature synthesis gas conveying pipe 70, and exchanges heat with the air of the electric pile required by the electrochemical reaction of the battery, which is input into the heat exchanger 20 through an electric pile air input pipe 80, so that the temperatures of the high-temperature synthesis gas and the air of the electric pile both meet the power generation requirement of the solid oxide fuel battery; the synthesis gas and the stack air after heat exchange are respectively input to each solid oxide fuel cell stack 30 through a synthesis gas output header pipe 90, a stack air output header pipe 90a, a plurality of synthesis gas input branch pipes 91 and a plurality of stack air input branch pipes 91a to generate electricity. Spent synthesis gas and spent air which finish power generation reaction of each solid oxide fuel cell set 30 are respectively merged through the spent synthesis gas output branch pipe 110 and the spent air output branch pipe 210, and then enter the process heating furnace 40 through the spent synthesis gas output header pipe 100 and the spent air output header pipe 200 for combustion and heat exchange, so that the residual chemical energy and residual heat in the spent synthesis gas and the spent air are fully utilized.

The fuel used by the solid oxide fuel cell and the cogeneration device of the process heating furnace is one or the mixture of more than two of fuel oil, natural gas, civil biogas, refinery pipe network gas, low-pressure gas, coke oven gas and raw coke oven gas. In consideration of possible toxicity of sulfur to the fuel cell electrode and electrolyte, the sulfur content in the fuel oil, natural gas, civil biogas, refinery pipe network gas, low-pressure gas, coke oven gas and raw coke oven gas should be strictly controlled.

The oxidation medium used by the solid oxide fuel cell and the cogeneration device of the process heating furnace is pure oxygen, oxygen-enriched air or air. Air is preferred to reduce the operating costs of the system.

The syngas generator 10 of the cogeneration unit of the solid oxide fuel cell and the process heating furnace is a water-hydrocarbon reformer or a partial oxidation syngas generator, preferably a partial oxidation syngas generator. The temperature of the high-temperature synthesis gas at the outlet is 800-1300 ℃. The specific outlet temperature is selected to meet the requirements of the galvanic pile on the composition and temperature of the synthesis gas and the heat exchange requirement on the temperature of the air inlet.

The high-temperature synthesis gas at the outlet of the partial oxidation synthesis gas generator mainly comprises the following components: h₂、CO、N₂、CO₂And the remaining CH₄、O₂Etc., the specific composition depending on the composition of the fuel and the operating temperature and pressure of the syngas generator 10. Wherein N is₂、CO₂And can pass through the stack without adversely affecting the stack, while other components can participate in the electrochemical reaction for power generation by the fuel cell.

Depending on the performance of the fuel cell, a certain proportion of H in the high temperature syngas entering the solid oxide fuel cell stack 30₂CO can participate in the electrochemical reaction, and the rest of unreacted H₂、CO、CH₄Etc. can continue to be burned in the process furnace 40 to continue recovering energy. The spent air leaving the sofc 30 still contains residual O₂It can continue to be used as an oxidizer in the process furnace 40 for fuel combustion.

In order to ensure that the thermal load of the furnace can meet the possible regulation requirements of the process plant, a burner for regulating the load is additionally arranged in the furnace, and a fuel inlet 43 for regulating and a combustion air inlet 44 for regulating are adopted, wherein the fuel inlet 43 for regulating is connected with a fuel source through a fuel inlet pipe 300 for regulating, and the combustion air inlet 44 for regulating is connected with an air source through a combustion air inlet pipe 400 for regulating. The requirement of load adjustment of the heating furnace can be still met under the condition of fluctuation of process devices and fuel cells.

The heat exchanger 20 of the cogeneration device of the solid oxide fuel cell and the process heating furnace is used for exchanging heat between high-temperature synthesis gas and air for the electric pile, so that the temperature of the synthesis gas and the air for the electric pile after heat exchange can meet the requirement of an inlet of the electric pile. The heat exchanger may be of the plate or tube bundle type, depending on the particular process design in relation to throughput, heat exchange capacity.

The following describes the embodiments of the present invention with reference to fig. 2 and 3.

FIG. 2 is a flow diagram of a process furnace 40 with an effective heat load of 0.9 MW. Assuming that the process furnace 40 is 90% thermally efficient, the process furnace 10 needs to burn 1.0MW of fuel to achieve a heat output of 0.9 MW.

Fig. 3 is a flow diagram of a process system after cogeneration using a solid oxide fuel cell stack 30 and a 0.9MW furnace. The details are as follows.

The fuel (fuel oil or fuel gas) of 1.4MW enters the partial oxidation synthesis gas generator (i.e. the synthesis gas generator 10) together with a proper amount of air, the generated high-temperature synthesis gas with the temperature of 800-. Assuming that the overall power generation efficiency of the fuel cell system is 50%, the power generation amount of the present system is 0.7 MW.

The spent synthesis gas and spent air at the outlet of the sofc 30 still carry the remaining 50% of the energy, i.e., 0.7MW, in the form of sensible heat (600 to 750 ℃) and residual chemical energy (e.g., residual unreacted H)₂、CO、CH₄、O₂Etc.).

The spent syngas and spent air carrying 0.7MW of energy are fed to the burners of the process furnace 40 for continued combustion. In order to ensure that the spent synthesis gas is stably combusted and the requirement of timely adjusting the heat load of the heating furnace is considered, the heating furnace is additionally supplemented with fuel gas of 0.3MW, and the requirement of stable operation of the heating furnace is met together.

The total input energy of the heating furnace is 1.0MW (0.7+ 0.3), and the effective heat output by the heating furnace is 0.9MW calculated according to 90% of the thermal efficiency of the heating furnace.

The total input energy of the cogeneration system illustrated in fig. 3 is (1.4+0.3 ═ 1.7MW, the output power generation is 0.7MW, and the output effective heat of the furnace is 0.9 MW. The total fuel heat efficiency of the above cogeneration system is (0.7+ 0.9)/1.7-94.1%.

The combined heat and power generation system described in fig. 3 is also significant in that it produces high potential energy of high added value. Compared with the conventional heating furnace system shown in fig. 2, under the condition that the external output heat of the heating furnace is not changed, the cogeneration system comprises:

the added input energy is: 1.7-1.0 ═ 0.7 MW;

the increased power generation is 0.7 MW;

assuming the price of fuel natural gas is 3.0 yuan/m³And the electricity price is 0.7 yuan/degree, the system is used for every hour:

the increased payout was 0.7 x 3600/35.53 x 3.0 ═ 212.8 yuan;

the increased income is 0.7 × 1000.0 × 0.7 ═ 490 yuan;

i.e. the gross profit per hour for the above additional system is 490-212.8-277.2 yuan. The gross profit that the 0.9MW heating furnace cogeneration system can realize every year is 232.8 ten thousand yuan calculated according to 8400 hours.

The above examples are merely illustrative of the process principles of cogeneration of solid oxide cells with process furnaces and are not exhaustive of all possible process solutions. And such as whether the air of the galvanic pile is preheated by the preheater of the process heating furnace, whether the air of the galvanic pile is optimized by the cascade heat exchange, whether the combustion air preheater is arranged on the process heating furnace, and the like, the technical details are considered according to project conditions in the specific implementation process, and the limitation of the patent is not formed.

It should be understood that the above-described examples are merely illustrative of the technical concepts and features of the present invention, which are intended to provide those skilled in the art with an understanding of the content of the present invention and to make decisions regarding its implementation. It should be understood that the technical solutions according to the present invention may be partially modified or partially replaced with equivalents without departing from the spirit and scope of the technical solutions of the present invention, and the technical solutions of the present invention are included in the claims of the present invention.