Hydroxide carbon fuel continuous reaction cell device

Abstract

The present invention discloses a hydroxide carbon fuel continuous reaction battery device, comprising a heat preservation oven, a waste liquid storage tank, a cathode and cathode reaction chamber, a carbon slurry mixed feed chamber and a hydroxide feed chamber, a partition is arranged inside the cathode and cathode reaction chamber, the cathode and cathode reaction chambers are separated into an anode reaction chamber and a cathode reaction chamber, a current collecting screen is arranged inside the cathode and cathode reaction chambers, a wire connection end is arranged at the upper end of the current collecting screen, the wire connection end is connected to the equipment outside the heat preservation oven through a wire, and the waste liquid storage tank is used to receive the waste liquid discharged from the cathode and cathode reaction chambers. The hydroxide carbon fuel continuous reaction battery device provided by the present invention can transform the anode reaction area from a single fixed rod-shaped electrode to an anode reaction chamber that continuously supplements the fluid carbon material, thereby increasing the reaction area, and preventing the cathode and cathode distance from becoming larger so as to increase the battery ohmic polarization, and the continuous addition of carbon material can promote the continuous flow of the internal electrolyte to prevent carbonate deposition.

Description

Technical Field

[0001] The invention relates to the technical field of carbon fuel cells, in particular to a hydroxide carbon fuel continuous reaction cell device. Background Art

[0002] Population growth, rapid economic growth and development all require a safe, reliable and continuous supply of electricity. Most of the electricity in most countries around the world (about 67%) comes from non-renewable energy sources such as coal (41%), crude oil (4%) or natural gas (22%), among which coal is still the main fuel source for power plants at home and abroad. my country has relatively abundant coal resources and is the world's largest coal producer and consumer. Due to the dominant position of coal in the primary energy structure, my country's electricity production is dominated by coal-fired power. Among the existing thermal power units in my country, coal-fired units account for about 93%. However, the coal-fired and power generation efficiency of traditional power plants is usually low (30% to 45%), and they emit a large amount of pollutants (sulfur dioxide, nitrogen oxides, particulate matter and carbon dioxide). Traditional thermal power generation technology is subject to the limitations of the thermal engine Carnot cycle, resulting in low power generation efficiency and serious pollution to the environment. Therefore, there is an urgent need for emerging efficient and environmentally friendly power generation technologies to replace traditional technologies.

[0003] Improving the efficiency of coal energy conversion has become the focus of global energy utilization technology development. Among them, fuel cells, as an emerging power generation technology, can directly convert the chemical energy in the fuel into electrical energy, breaking away from the limitations of the Carnot cycle. It has attracted widespread attention from scholars around the world for its outstanding features of low energy consumption, energy saving and environmental protection, and efficient power generation.

[0004] Direct carbon fuel cells (DCFCs) in the fuel cell classification generate electricity directly without gasification. They are not only clean but also have high energy conversion efficiency. The actual electrical efficiency is as high as 80%. Fuel cells using natural gas have not yet exceeded 61%, and hydrogen fuel cells are only 47%.

[0005] At present, the main problems of DCFC batteries using molten hydroxide as electrolyte are:

[0006] (1) When fixed rod-shaped carbon is used as the anode, the overall battery reaction stops quickly as the fixed rod-shaped carbon is consumed. The fixed rod-shaped electrode cannot expand the anode reaction area, thereby limiting the further improvement of battery performance. The direct carbon fuel cell field lacks structural designs that can expand the electrode reaction area.

[0007] (2) As the reaction time increases, the anode carbon fuel is consumed irregularly, causing the distance between the anode and cathode to increase irregularly, thereby increasing the battery's ohmic polarization and causing the battery performance to deteriorate;

[0008] (3) The battery has a rod-shaped electrode with fixed raw materials. During the intermittent reaction discharge process, as the operating time increases, the carbon is irregularly consumed and dissolved, resulting in a decrease in the volume of the anode electrode and a decrease in the effective reaction contact area, causing the battery to have unstable working power output;

[0009] (4) The electrolyte retention area inside the reactor is fixed and has no fluidity. The alkali absorbs CO2 and converts it into CO3 2- , which can easily cause carbonate deposition and thus lead to battery deactivation. The mechanism is the electrode reaction that generates carbonate:

[0010] C+6OH - =CO3 2- +3H2O+4e - ,

[0011] Therefore, there is an urgent need to study an efficient direct-combustion hydroxide carbon fuel continuous reaction cell device that can expand the reaction area, continuously replenish electrolyte and carbon fuel, and achieve high-power stable power generation at a lower temperature. Summary of the invention

[0012] In order to solve the problems existing in the above-mentioned prior art, the present invention provides a hydroxide carbon fuel continuous reaction battery device. Specifically, the present invention includes the following contents.

[0013] The present invention provides a hydroxide carbon fuel continuous reaction cell device, comprising a heat preservation oven (1000) and a waste liquid storage tank (2000) at the bottom layer, a cathode and cathode reaction chamber (3000) at the middle layer, and a carbon slurry mixing feed chamber (4000) and a hydroxide feed chamber (5000) arranged in parallel at the upper layer in the heat preservation oven (1000) in order from bottom to top.

[0014] The carbon slurry mixing feed chamber (4000) and the hydroxide feeding chamber (5000) are both provided with a feeding port, the bottom of the carbon slurry mixing feed chamber (4000) is provided with a carbon slurry mixing liquid discharge port (4300) for discharging the liquid of the carbon slurry mixing feed chamber (4000) into the cathode and anode reaction chambers (3000), and the bottom of the hydroxide feeding chamber (5000) is provided with a hydroxide liquid discharge port (5500) for discharging the liquid of the hydroxide feeding chamber (5000) into the cathode and anode reaction chambers (3000), and the raw materials include hydroxide and carbon fuel;

[0015] The cathode and cathode reaction chamber (3000) is a trough structure with an opening at the upper end. A vertical partition (3100) is arranged inside the cathode and cathode reaction chamber (3000) to divide the cathode and cathode reaction chamber (3000) into an anode reaction chamber (3200) and a cathode reaction chamber (3300). Current collecting screens (3400) are arranged inside the anode reaction chamber (3200) and the cathode reaction chamber (3300), respectively being an anode current collecting screen (3410) and a cathode current collecting screen (3420). A wire connection end is arranged at the upper end of the current collecting screen (3400), and the wire connection end is connected to a current collecting device outside the heat preservation oven (1000) via a connecting wire.

[0016] The waste liquid storage tank (2000) is used to receive waste liquid discharged from the anode and cathode reaction chambers (3000).

[0017] In certain embodiments, according to the hydroxide carbon fuel continuous reaction cell device described in the present invention, wherein, in the anode reaction chamber (3200), a vertically placed anode reaction chamber baffle plate (3210) and an anode reaction chamber overflow plate (3220) are sequentially arranged from right to left, the height of the anode reaction chamber baffle plate (3210) is higher than the anode reaction chamber overflow plate (3220), the bottom surface of the anode reaction chamber baffle plate (3210) is at a certain distance from the bottom wall of the anode reaction chamber (3200), and the bottom surface of the anode reaction chamber overflow plate (3220) is sealed and connected to the bottom wall of the anode reaction chamber (3200).

[0018] In certain embodiments, according to the hydroxide carbon fuel continuous reaction cell device described in the present invention, the carbon slurry mixing feed chamber (4000) and the hydroxide feed chamber (5000) are both trough structures with an open upper end, and the feeding port is a groove arranged on the side wall of the trough body, and the groove is a structure with open ends on the upper end face and the inner side face, and a feeder is arranged in the groove, and the feeder is a circular tube, and the lower end face of the circular tube is at a certain distance from the bottom face of the groove, and the top face of the circular tube extends above the shell of the heat preservation oven (1000).

[0019] In certain embodiments, according to the hydroxide carbon fuel continuous reaction cell device of the present invention, an anode reaction chamber drain port (3230) is provided at the bottom of the anode reaction chamber (3200), and the anode reaction chamber drain port (3230) is a through hole penetrating the bottom wall of the anode reaction chamber (3200), and the anode reaction chamber drain port (3230) is located between the anode reaction chamber overflow plate (3220) and the left side wall of the anode reaction chamber (3200);

[0020] The bottom of the anode and cathode reaction chamber (3000) is provided with a washing liquid port (3500), the washing liquid port (3500) is a through hole that penetrates the bottom wall of the anode and cathode reaction chamber (3000), the washing liquid port (3500) is provided with a plug, and the number and size of the washing liquid ports (3500) are set according to needs.

[0021] In certain embodiments, according to the hydroxide carbon fuel continuous reaction cell device described in the present invention, a vertically placed hydroxide baffle (5100) and a hydroxide overflow plate (5200) are arranged in the hydroxide feed chamber (5000), a certain distance is set between the bottom surface of the hydroxide baffle (5100) and the bottom surface of the hydroxide feed chamber (5000), the bottom surface of the hydroxide baffle (5100) is lower than the top surface of the hydroxide overflow plate (5200), the bottom surface of the hydroxide overflow plate (5200) is sealed and connected to the bottom surface of the hydroxide feed chamber (5000), and the top surface of the hydroxide overflow plate (5200) is lower than the top surface of the hydroxide baffle (5100).

[0022] In certain embodiments, according to the hydroxide carbon fuel continuous reaction cell device described in the present invention, the current collecting screen (3400) is movably connected to the anode and cathode reaction chambers (3000), and the spacing between the anode current collecting screen (3410) and the cathode current collecting screen (3420) can be flexibly adjusted.

[0023] In certain embodiments, according to the hydroxide carbon fuel continuous reaction cell device described in the present invention, a stirrer is provided in the anode reaction chamber (3200) and the carbon slurry mixing feed chamber (4000), and the stirrer includes a stirring shaft and blades, and the stirring shaft is connected to the motor (6000), and the blades of the stirrer extend to the anode reaction chamber (3200) and the carbon slurry mixing feed chamber (4000), respectively.

[0024] In certain embodiments, according to the hydroxide carbon fuel continuous reaction cell device described in the present invention, a sampling port (1100) is provided on the upper surface of the shell of the heat preservation oven (1000), and a cover plate (1110) and a sampler (1120) are provided on the sampling port (1100), wherein the cover plate (1110) is used to seal the sampling port (1100), and the sampler (1120) extracts liquid through the sampling port (1100).

[0025] In certain embodiments, according to the hydroxide carbon fuel continuous reaction cell device of the present invention, the hydroxide is selected from a mixture of one or more of sodium hydroxide, potassium hydroxide, and lithium hydroxide, and the carbon fuel particles have a particle size of millimeters or micrometers and a density range of 0.5-1.7 g / cm 3 , with a specific surface area of ​​5-700 m2 / g, and the conductivity range is 100-12900 S / m.

[0026] The present invention also provides a method for generating electricity by using the above-mentioned battery device, comprising the following steps:

[0027] (1) adding a hydroxide raw material into the cathode and anode reaction chambers (3000) and the hydroxide feed chamber (5000), and adding a carbon slurry mixture including a carbon fuel and a hydroxide mixed in proportion into the carbon slurry mixing feed chamber (4000);

[0028] (2) After the heat preservation oven is preheated to the target temperature, the carbon slurry mixture is continuously added to the carbon slurry mixing feed chamber (4000), and the molten mixed reaction liquid obtained by stirring and mixing flows into the anode reaction chamber (3200) below through the carbon slurry mixing discharge port (4300) at a suitable rate; the hydroxide is continuously added to the hydroxide feed chamber (5000), and the molten hydroxide flows into the cathode reaction chamber (3300) below through the hydroxide discharge port (5500) at a suitable rate; the carbon slurry mixture and the molten hydroxide undergo an oxidation reaction in the anode and cathode reaction chambers (3000) to lose electrons, and the electrons are conducted to the current collecting device through the current collecting screen (3400);

[0029] (3) After the battery device has been running stably for a period of time, the liquid levels in the cathode and anode reaction chambers (3000) gradually rise and exceed the height of the overflow plate (3220) of the anode reaction chamber, and the reaction waste liquid is discharged into the waste liquid storage tank (2000) through the anode reaction chamber discharge port (3230);

[0030] (4) After the battery device is operated, a cleaning agent is injected to clean the battery device, and the cleaning waste liquid is discharged through the cleaning liquid port (3500) at the bottom of the anode and cathode reaction chamber, thereby achieving rapid cleaning of the anode and cathode reaction chamber (3000).

[0031] The beneficial effects of the present invention include:

[0032] (1) The anode reaction area is transformed from a single fixed rod-shaped electrode to an anode reaction chamber that continuously replenishes the fluid carbon material, thereby increasing the reaction area;

[0033] (2) By fixing the distance and shape of the current collecting screen, the distance between the anode and cathode is prevented from becoming larger, which will increase the ohmic polarization of the battery;

[0034] (3) The continuous addition of carbon fuel allows the carbon raw material to be continuously replenished, so that the battery can output stable power for a long time;

[0035] (4) The continuous addition of carbon fuel and the assistance of the stirring device can promote the continuous flow of the internal electrolyte, avoid the formation of sediment and inhibit the formation of carbonate. BRIEF DESCRIPTION OF THE DRAWINGS

[0036] Figure 1 It is a schematic diagram of an exemplary overall structure of the present invention.

[0037] Figure 2 It is an exemplary overall structural cross-sectional view of the present invention.

[0038] Figure 3 Schematic diagram of an exemplary internal reaction device of the present invention.

[0039] Figure 4 Schematic diagram of the internal structure of the cathode and anode reaction chambers according to the present invention.

[0040] Figure 5 It is an enlarged schematic diagram of the top of an exemplary heat preservation oven of the present invention.

[0041] Figure 6 This is a schematic diagram of an exemplary current-voltage performance of the present invention.

[0042] Figure 7 Schematic diagram of an exemplary NPT threaded plug with different numbers of through holes according to the present invention.

[0043] Description of reference numerals:

[0044] 1000. Insulated oven; 1100. Sampling port; 1110. Cover plate; 1120. Sampler; 1200. Visualization window; 2000. Waste liquid storage tank; 3000. Anode and cathode reaction chambers; 3100. Screen; 3200. Anode reaction chamber; 3210. Anode reaction chamber baffle; 3220. Anode reaction chamber overflow plate; 3230. Anode reaction chamber drain port; 3300. Cathode reaction chamber; 3400. Current collecting screen; 3410. Anode current collecting screen; 3411. Anode wire connection end; 3412. Anode current collecting wire; 3420. Cathode current collecting screen; 3421. Cathode wire connection end; 3422. Cathode current collecting wire; 3500. washing liquid inlet; 3600. ceramic frame; 3700. fixed seat; 4000. carbon slurry mixing feed chamber; 4100. carbon slurry mixing feed port; 4200. carbon slurry mixing feeder; 4300. carbon slurry mixing discharge port; 5000. hydroxide feed chamber; 5100. hydroxide baffle; 5200. hydroxide overflow plate; 5300. hydroxide feeding port; 5400. hydroxide feeder; 5500. hydroxide discharge port; 6000. motor; 6100. motor base; 7000. fixed bracket; 8000. mixing assembly; 8100. anode reaction chamber agitator; 8200. carbon slurry mixing feed chamber agitator. DETAILED DESCRIPTION

[0045] Various exemplary embodiments of the present invention will now be described in detail. This detailed description should not be considered as limiting the present invention, but should be understood as a more detailed description of certain aspects, features, and embodiments of the present invention.

[0046] It should be understood that the terms described in the present invention are only for describing special embodiments and are not intended to limit the present invention. In addition, for the numerical range in the present invention, it should be understood that the upper and lower limits of the scope and each intermediate value therebetween are specifically disclosed. Each smaller range between the intermediate value in any stated value or stated range and any other stated value or intermediate value in the described range is also included in the present invention. The upper and lower limits of these smaller ranges can be independently included or excluded in the scope.

[0047] Unless otherwise specified, all technical and scientific terms used herein have the same meaning as commonly understood by those skilled in the art to which the invention belongs. Although the present invention describes only preferred structures and materials, any structures and materials similar or equivalent to those described herein may also be used in the implementation or testing of the present invention.

[0048] In addition, the terms "center", "up", "down", "left", "right", "vertical", "horizontal", "inside", "outside", etc. in the specification and claims indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operate in a specific orientation, and therefore cannot be understood as limiting the present invention. In addition, terms such as "first", "second", etc. are also used to describe various elements, regions, parts, etc., and do not specifically refer to order or sequence, and should not be regarded as limiting. It should be understood that the terms used in this way are interchangeable under appropriate conditions, and the embodiments of the present invention described herein can be operated in other orientations than those described or exemplified herein.

[0049] The term "fixed connection" of the present invention includes a detachable fixed connection or a non-detachable fixed connection. The detachable fixed connection includes bolt connection, etc., and the non-detachable fixed connection includes welding, etc.

[0050] Example

[0051] Combine the following Figure 1-Figure 7 , various embodiments of the present invention are described in further detail.

[0052] The hydroxide carbon fuel continuous reaction cell device disclosed in the present invention comprises a heat preservation oven 1000 and three layers of devices placed from bottom to top in the heat preservation oven: a waste liquid storage tank 2000 at the bottom, a cathode and anode reaction chamber 3000 at the middle layer, and a carbon slurry mixing feed chamber 4000 and a hydroxide feed chamber 5000 arranged in parallel at the upper layer.

[0053] The structure of the supporting device for placing the three-layer device in the incubator is not limited, and any structure that can play a supporting role can be used, for example, it can be a fixed bracket 7000 containing multiple layers of partitions, and the fixed bracket includes a door-shaped frame and a horizontal partition arranged inside it, which divides the interior of the insulated oven 1000 into three layers of space, upper, middle and lower. The lower layer of the fixed bracket 7000 is placed with a waste liquid storage tank 2000, the middle layer is placed with a cathode and cathode reaction chamber 3000, and the left and right sides of the upper layer are respectively placed with a carbon slurry mixing feed chamber 4000 and a hydroxide feed chamber 5000. When the battery is running, the above three layers of devices are placed inside the insulated oven for unified heating. The insulated oven 1000 is preferably provided with a visualization window 1200 to facilitate observation of the reaction in the insulated oven. The insulated oven can use existing products on the market, and the appropriate type of insulated oven can be selected according to actual conditions.

[0054] like Figure 4 As shown, the anode and cathode reaction chamber 3000 placed in the middle layer is a trough structure with an opening at the upper end, and the trough is preferably a hollow rectangular parallelepiped. A vertical partition 3100 is arranged inside the anode and cathode reaction chamber 3000 to divide the anode and cathode reaction chamber 3000 into two left and right spaces. The left space is the anode reaction chamber 3200, and the right space is the cathode reaction chamber 3300.

[0055] A vertically placed current collecting screen 3400 is provided in the anode reaction chamber 3200 and the cathode reaction chamber 3300, which are respectively the anode current collecting screen 3410 and the cathode current collecting screen 3420. The current collecting screen 3400 is preferably a straight plate structure with holes. The current collecting screen 3400 is fixed on the rear side wall of the cathode and cathode reaction chamber 3200. The current collecting screen 3400 is preferably movably connected to the cathode and cathode reaction chamber 3000, and the spacing between the anode and cathode current collecting screen 3410 and the cathode current collecting screen 3420 can be flexibly adjusted. If the distance between the cathode and cathode electrodes of the fuel cell is too small, the high-density current causes fine bubbles to be generated inside the reaction electrolyte, and a certain gap is generated for the contact between the electrode material and the electrolyte solution, thereby causing the "cavitation" phenomenon to occur and the electrochemical corrosion phenomenon to intensify; if the electrode spacing is too large, the corresponding ohmic overpotential will be increased, resulting in a decrease in battery performance. Therefore, an adjustable battery cathode and cathode spacing is designed to maximize battery performance while extending the service life of the corresponding electrode material.

[0056] There is no limitation on the connection method between the current collecting screen 3400 and the anode and cathode reaction chamber 3000. In this embodiment, the current collecting screen 3400 is fixed by setting a ceramic frame 3600 on both sides thereof. The ceramic frame 3600 is preferably an L-shaped plate. The vertical plate of the ceramic frame 3600 is perpendicular to and close to the rear wall of the anode and cathode reaction chamber 3000. The horizontal plate of the ceramic frame 3600 is located at the upper end of the current collecting screen 3400. The ceramic frames 3600 on both sides of the current collecting screen 3400 clamp the current collecting screen in the middle. The ceramic frame 3600 is fixed on the upper surface of the rear wall of the anode and cathode reaction chamber 3000 through a fixing seat 3700. The fixing seat is preferably an L-shaped angle plate. The L-shaped angle plate is fixed to the ceramic frame 3600 and the rear wall of the anode and cathode reaction chamber 3000 respectively by screws.

[0057] Furthermore, the material of the collecting screen 3400 can be selected from corrosion-resistant and conductive materials, such as copper mesh, titanium-plated iron mesh, gold mesh, silver mesh, platinum mesh, etc., preferably Ni metal mesh, which has strong corrosion resistance and oxidation resistance, and has good high temperature stability and conductivity.

[0058] The anode current collecting screen 3410 is used to collect the electrons generated by the anode reaction and form a large current for external output. The cathode current collecting screen 3420 receives the current from the external circuit and performs related reduction reactions. The upper ends of the anode current collecting screen 3410 and the cathode current collecting screen 3420 are respectively provided with an anode wire connecting end 3411 and a cathode wire connecting end 3421. The anode wire connecting end 3411 and the cathode wire connecting end 3421 are respectively connected to the anode current collecting wire 3412 and the cathode current collecting wire 3422. The other ends of the anode collecting wire 3412 and the cathode current collecting wire 3422 are respectively ringed with ceramic tubes and extended to the outside of the heat preservation oven 1000 to connect the current collecting device.

[0059] An anode reaction chamber baffle 3210 and an anode reaction chamber overflow plate 3220 are vertically arranged from right to left in the anode reaction chamber 3200. The height of the anode reaction chamber baffle 3210 is higher than the anode reaction chamber overflow plate 3220. The bottom surface of the anode reaction chamber baffle 3210 is lower than the top surface of the anode reaction chamber overflow plate 3220. There is a certain distance between the bottom surface of the anode reaction chamber baffle 3210 and the bottom surface of the anode reaction chamber 3200. The bottom surface of the anode reaction chamber overflow plate 3220 is sealedly connected to the bottom surface of the anode reaction chamber 3200. The side surfaces of the anode reaction chamber baffle 3210 and the anode reaction chamber overflow plate 3220 are sealedly connected to the side walls of the anode reaction chamber 3200.

[0060] An anode reaction chamber drain port 3230 is provided at the bottom of the anode reaction chamber 3200. The anode reaction chamber drain port 3230 is located between the anode reaction chamber overflow plate 3220 and the left side wall of the anode reaction chamber 3200. It is preferably a through hole that penetrates the bottom wall of the anode reaction chamber 3200. The liquid can be discharged to the waste liquid storage tank 2000 below the anode reaction chamber drain port 3230. The anode reaction chamber drain port 3230 can be provided with a plug as needed, preferably a through-hole NPT threaded plug, such as Figure 7 As shown, NPT threaded plugs with different numbers of through holes can be selected. The number of through holes can be used to adjust the drainage speed, thereby adjusting the reaction time. NPT threaded plugs have the advantages of good sealing, pressure resistance, temperature resistance, and strong corrosion resistance. When using a threaded plug, the drainage port needs to be provided with a corresponding internal thread.

[0061] Before the battery is operated, a certain amount of hydroxide powder is stored in the cathode and anode reaction chambers 3000 and the hydroxide feed chamber 5000 respectively, and a carbon slurry mixture composed of a certain amount of carbon fuel and hydroxide powder mixed in proportion is stored in the carbon slurry mixing feed chamber 4000.

[0062] Carbon fuel can be selected from fuels with different active specific surface areas, electrical conductivity and density. It can be biomass charcoal, such as straw, activated carbon, orange peel ash, grapefruit peel prefabricated powder; it can also be selected from Inner Mongolia's unique lignite ore powder, Yulin anthracite powder, special carbon black, etc. The particle size of carbon fuel is millimeter or micron level, and the density range is 0.5-1.7 g / cm 3 Specific surface area: 5-700m 2 / g, conductivity range is 100-12900 S / m.

[0063] The hydroxide may include at least one or more mixtures of sodium hydroxide, potassium hydroxide, and lithium hydroxide.

[0064] The ratio of carbon fuel to hydroxide powder is preferably: 10-25 parts by weight of carbon fuel to 90-75 parts by weight of hydroxide powder, and the ratio can be adjusted according to actual conditions.

[0065] The battery operating temperature range is preferably 350°C-550°C, more preferably 400°C-500°C, and further preferably 450°C, which can be adjusted accordingly according to actual operating conditions.

[0066] When the battery has been running stably for a certain period of time, as the reaction liquid from the carbon slurry mixing feed chamber 4000 and the hydroxide feed chamber 5000 continues to flow into the anode and cathode reaction chambers 3000, the liquid level inside the anode and cathode reaction chambers 3000 gradually rises. When the liquid level exceeds the height of the overflow plate 3220 of the anode reaction chamber, overflow is triggered, causing the reaction waste liquid to be discharged into the waste liquid storage tank 2000 through the anode reaction chamber drain port 3230.

[0067] The purpose of providing the anode reaction chamber baffle 3210 is to prevent the mixed carbon slurry flowing in from the carbon slurry mixing feed chamber 4000 from overflowing into the waste liquid storage tank 2000 without reacting, thereby causing unnecessary loss of raw materials.

[0068] Further, a washing liquid port 3500 is provided at the bottom of the anode reaction chamber 3200 and the cathode reaction chamber 3300. The washing liquid port 3500 is preferably a through hole that penetrates the bottom wall of the cathode and cathode reaction chambers 3000. When the battery operation is completed and the battery device is cleaned, the washing liquid port 3500 at the bottom of the cathode and cathode reaction chambers is opened after the cleaning agent is injected to achieve rapid cleaning of the cathode and cathode reaction chambers 3000. The waste liquid flowing out of the washing liquid port 3500 is discharged into the waste liquid storage tank 2000 below it. The number and size of the washing liquid port 3500 can be set as needed. The washing liquid port 3500 needs to be provided with a plug to prepare for plugging when not cleaning. The plug is preferably a closed NPT threaded plug, which has the advantages of good sealing, pressure resistance, temperature resistance, and strong corrosion resistance. When a threaded plug is selected, the washing liquid port needs to be provided with a corresponding internal thread.

[0069] Further, a mixing assembly 8000 is provided in both the anode reaction chamber 3200 and the carbon slurry mixing feed chamber 4000 to make the liquid in the chamber more evenly mixed. The mixing assembly 8000 is preferably a stirrer, and the stirrer mainly includes a motor and a stirring paddle, and the stirring paddle mainly includes a stirring shaft and a blade. Preferably, the motor 6000 is provided on the upper surface of the shell of the heat preservation oven 1000, and the upper part of the stirring shaft is connected to the motor. The blade at the lower end of the anode reaction chamber stirrer 8100 extends into the anode reaction chamber baffle 3210 and the anode current collecting screen 3410, and the blade at the lower end of the carbon slurry mixing feed chamber stirrer 8200 extends into the carbon slurry mixing feed chamber 4000, and the stirring paddle is driven by the motor to rotate in the container, so as to mix and stir the liquid in the container. The mixing assembly 8000 can also select other mixing devices as needed, such as ultrasonic stirrers, pneumatic stirrers, etc. The main function of the anode reaction chamber stirrer 8100 provided in the anode reaction chamber 3200 is to make the mixed reaction liquid flow continuously to avoid the formation of carbonate.

[0070] Furthermore, the motor 6000 is placed on a motor base 6100, and the motor base 6100 is fixed on the upper surface of the shell of the heat preservation oven 1000 to make the motor more firmly installed.

[0071] Furthermore, a sampling port 1100 is provided on the upper surface of the shell of the heat preservation oven 1000, and a cover plate 1110 is provided on the sampling port 1100 for sealing. When a sample needs to be taken during the reaction process, the cover plate 1110 is removed, and a sampler 1120 is used to extract liquid through the sampling port 1100. After the operation is completed, the cover plate 1110 is used again for sealing. The sampler 1120 can be an existing product on the market, and any device that can extract liquid in the device can be used. The waste liquid is extracted through the sampler 1120 to observe and detect experimental phenomena such as whether the fuel is exhausted and whether carbonate is produced.

[0072] Furthermore, a reaction liquid transfer propulsion device is provided in the sampling port 1100, which can be selected as a high temperature resistant and corrosion resistant liquid conveying equipment to push and circulate the reaction liquid. If the fuel reacts completely, the reaction liquid is pure molten hydroxide, which can be circulated through the liquid conveying equipment and injected into the reactor to continue the reaction.

[0073] The carbon slurry mixing feed chamber 4000 and the hydroxide feeding chamber 5000 placed on the upper layer are both trough structures with an opening at the upper end. The trough is preferably a hollow cylinder. The carbon slurry mixing feed chamber 4000 is located on the left side, above the anode reaction chamber 3200, and the hydroxide feeding chamber 5000 is located on the right side, above the cathode reaction chamber 3300. A groove-shaped carbon slurry mixing feed port 4100 is arranged on one side of the annular upper end surface of the carbon slurry mixing feed chamber 4000 close to the left side wall of the heat preservation oven 1000. The groove is a structure with openings at both ends of the upper end surface and the inner side surface. Preferably, the bottom surface of the groove is a plane inclined downward from the outside to the inside, so as to facilitate the inflow of the carbon slurry mixture. A carbon slurry mixing feeder 4200 is arranged in the groove. The structure of the carbon slurry mixing feeder 4200 is preferably a round tube. The round tube is placed vertically. The bottom surface of the round tube is at a certain distance from the bottom surface of the groove to facilitate the discharge of liquid. The bottom surface of the round tube is preferably a plane inclined upward from left to right, which is more conducive to the discharge of liquid. The top surface of the round tube is located above the shell of the heat preservation oven. Similarly, a groove-shaped hydroxide feeding port 5300 is arranged on one side of the annular upper end surface of the hydroxide feeding chamber 5000 close to the right side wall of the heat preservation oven 1000. The groove is an open structure at both ends of the upper end surface and the inner side surface. The bottom surface of the groove is preferably a plane inclined downward from the outside to the inside to facilitate the addition of hydroxide powder. A hydroxide feeder 5400 is arranged in the groove. The structure of the hydroxide feeder 5400 is preferably a round tube. The round tube is placed vertically. The lower end surface of the round tube is at a certain distance from the bottom surface of the groove to facilitate the discharge of hydroxide. Preferably, the bottom surface of the round tube is a plane inclined downward from left to right, which is more conducive to the discharge of hydroxide powder. The top surface of the round tube is located above the shell of the insulation oven 1000.

[0074] Furthermore, auxiliary feeding funnels are respectively arranged on the top of the carbon slurry mixing feeder 4200 and the hydroxide feeder 5400. The vertical cross-sectional shape of the funnel is preferably a trapezoid. The lower part of the funnel is connected to the upper end of the feeder circular tube. The size of the lower part of the funnel is adapted to the size of the circular tube so that the funnel can be smoothly inserted into the circular tube. The material enters the circular tube through the funnel, and then enters the carbon slurry mixing feeding chamber or the hydroxide feeding chamber through the circular tube. The setting of the feeding funnel facilitates the feeding operation and avoids leakage of materials during feeding.

[0075] The carbon slurry mixing feed chamber 4000 and the hydroxide feed chamber 5000 are both provided with drainage ports, which are arranged at the bottom of the side wall or on the bottom wall. A carbon slurry mixing drainage port 4300 is arranged at the bottom of the carbon slurry mixing feed chamber 4000, and the carbon slurry mixing drainage port 4300 is preferably arranged at the bottom end of the right side wall of the carbon slurry mixing feed chamber 4000, and the molten mixed reaction liquid flows into the anode reaction chamber 3200 below at a certain rate through the carbon slurry mixing drainage port 4300. The carbon slurry mixing drainage port 4300 is preferably a circular tube type, one end of the drainage port circular tube passes through the side wall of the carbon slurry mixing feed chamber 4000, and the other end extends out of the carbon slurry mixing feed chamber 4000 for a distance, and the end face of the right side extension end of the carbon slurry mixing drainage port 4300 is located between the anode reaction chamber baffle 3210 and the anode current collecting screen 3410. The hydroxide discharge port 5500 is disposed at the bottom of the hydroxide feed chamber 5000, preferably at a position near the left side of the bottom wall of the hydroxide feed chamber 5000, so that the molten hydroxide flows into the cathode reaction chamber 3300 below at a certain rate through the hydroxide discharge port 5500. The hydroxide discharge port 5500 is preferably a circular channel, and the center of the hydroxide discharge port 5500 is preferably aligned with the center of the cathode reaction chamber 3300 below it.

[0076] Furthermore, the carbon slurry mixture drain port 4300 and the hydroxide drain port 5500 are provided with plugs for use when plugging is required, preferably closed NPT threaded plugs, which have the advantages of good sealing, pressure resistance, temperature resistance, and strong corrosion resistance. When the threaded plug is selected, the drain port needs to be provided with corresponding internal threads.

[0077] A vertically placed molten hydroxide baffle 5100 and a hydroxide overflow plate 5200 are arranged in the hydroxide feed chamber 5000. There is a gap between the lower surface of the hydroxide baffle 5100 and the bottom wall of the hydroxide feed chamber 5000. At the same time, the lower surface height of the hydroxide baffle 5100 is lower than the upper surface height of the hydroxide overflow plate 5200. The bottom surface of the hydroxide overflow plate 5200 is sealed and connected to the bottom surface of the hydroxide feed chamber 5000. The upper surface height of the hydroxide overflow plate 5200 is lower than the upper surface height of the hydroxide baffle 5100. The hydroxide baffle 5100 is used to prevent unmelted hydroxide particles from directly entering the cathode reaction chamber 3300 to prevent the reaction effect from being affected; the hydroxide overflow plate 5200 allows a certain amount of molten hydroxide to always exist in the hydroxide feed chamber 5000, so that the solid granular hydroxide can be quickly converted and fused into a molten state.

[0078] The materials used for the cathode and anode reaction chambers 3000, the carbon slurry mixing feeder 4200, the hydroxide feeder 5400, the anode reaction chamber agitator 8100 and the carbon slurry mixing feed chamber agitator 8200 are corrosion-resistant materials, preferably copper-nickel monel alloy 400, which has excellent corrosion resistance and good mechanical properties. Other materials may also be selected according to actual conditions.

[0079] The materials used for the heat preservation oven 1000, the waste liquid storage tank 2000, the carbon slurry mixing feed chamber 4000, the hydroxide feed chamber 5000, and the sampler 1120 are corrosion-resistant materials, preferably stainless steel.

[0080] The cover plate material is a corrosion-resistant material, preferably 99 alumina ceramic, which has the advantages of corrosion resistance, high temperature resistance, and wear resistance. Other materials can also be selected according to actual conditions.

[0081] Working process:

[0082] Before the battery is operated, a certain amount of hydroxide powder is stored in the cathode and anode reaction chambers 3000 and the hydroxide feed chamber 5000 respectively, and a carbon slurry mixture composed of a certain amount of carbon fuel and hydroxide powder mixed in proportion is stored in the carbon slurry mixing feed chamber 4000.

[0083] When the heat preservation oven is preheated to the target temperature and starts to operate, the carbon slurry mixing feeder 4200 continuously replenishes the carbon slurry mixture into the carbon slurry mixing feeding chamber 4000 through the carbon slurry mixing feeding port 4100, and the molten mixed reaction liquid obtained by stirring and mixing flows into the anode reaction chamber 3200 below at a certain rate through the carbon slurry mixing discharge port 4300; at the same time, the hydroxide feeder 5400 continuously replenishes hydroxide powder into the hydroxide feeding chamber 5000 through the hydroxide feeding port 5300, and the blocking effect of the hydroxide baffle 5100 and the hydroxide overflow plate 5200 can increase the reaction time of the hydroxide, and because the reaction temperature inside the heat preservation oven is higher than the melting point of the hydroxide, the hydroxide can be completely converted from a solid state to a molten state, and flows into the cathode reaction chamber 3300 below at a certain rate through the hydroxide discharge port 5500; the carbon slurry mixture and the molten sodium hydroxide undergo oxidation reaction in the anode and cathode reaction chambers 3000 to lose electrons, and the electrons are exported to the external collector through the anode and cathode current collecting screens. The battery of this embodiment is initially activated at a temperature of about 450° C., and the output current reaches 76 mA.

[0084] After the battery has been running stably for a certain period of time, as the reaction liquid in the carbon slurry mixing feed chamber 4000 and the hydroxide feed chamber 5000 continues to flow into the anode and cathode reaction chambers 3000, the liquid levels inside the anode and cathode reaction chambers gradually rise. When the height exceeds the overflow plate 3220 of the anode reaction chamber, overflow is triggered, causing the reaction waste liquid to be discharged into the waste liquid storage tank 2000 through the anode reaction chamber drain port 3230.

[0085] When the battery operation is completed and the battery structure is cleaned, after the cleaning agent is injected, the cleaning liquid outlet 3500 at the bottom of the anode and cathode reaction chamber is opened to discharge the cleaning waste liquid, thereby achieving rapid cleaning of the anode and cathode reaction chamber 3000.

[0086] In this embodiment, Figure 6 The power density curve of the battery shows that the maximum power output can reach 74.69 milliwatts per square centimeter at a fixed current.

[0087] Working principle:

[0088] Direct carbon fuel cells (DCFCs) in the fuel cell classification can directly use carbon and oxygen without gasification and reforming to generate electricity through electrochemical reactions. DCFCs using molten hydroxide as the electrolyte: the conductive ions are OH － , its operating temperature is 400~500℃. The overall battery reaction is as follows:

[0089] Cathode reaction: O2+2NaOH=2NaOOH - -2e - ,

[0090] Anode reaction: C+2NaOOH - =CO2+2NaOH+2e - ,

[0091] Overall reaction: C + O2 = CO 2 。

[0092] The present invention is based on a molten hydroxide direct carbon fuel cell, and the continuous reaction operation principle of the direct combustion hydroxide carbon fuel cell involved is as follows: within a selected temperature range, the oxygen in the cathode reaction chamber that contacts the electrolyte undergoes a reduction reaction and correspondingly releases oxygen anions, which move to the anode reaction chamber through the electrolyte channel, thereby forming a potential difference with the external circuit. At the same time, the carbon fuel in the anode reaction chamber reacts with the oxygen anions in the cathode reaction chamber to generate CO2, and continuously releases electrons, which then flow back to the cathode through the external circuit, and continuous power generation is achieved through the circulation of oxygen anions and electrons.

[0093] Although the present invention has been described with reference to exemplary embodiments, it should be understood that the present invention is not limited to the disclosed exemplary embodiments. Various adjustments or changes may be made to the exemplary embodiments of the present specification without departing from the scope or spirit of the present invention. The scope of the claims should be based on the broadest interpretation to cover all modifications and equivalent structures and functions.

Claims

1. A hydroxide carbon fuel continuous reaction cell device, characterized in that: It comprises a heat preservation oven (1000) and a waste liquid storage tank (2000) at the bottom layer, a cathode and cathode reaction chamber (3000) at the middle layer, and a carbon slurry mixing feed chamber (4000) and a hydroxide feed chamber (5000) arranged in parallel at the upper layer, which are arranged in sequence from bottom to top in the heat preservation oven (1000); The carbon slurry mixing feed chamber (4000) and the hydroxide feeding chamber (5000) are both provided with a feeding port for adding raw materials, the bottom of the carbon slurry mixing feed chamber (4000) is provided with a carbon slurry mixing liquid discharge port (4300) for discharging the liquid of the carbon slurry mixing feed chamber (4000) into the anode and cathode reaction chamber (3000), and the bottom of the hydroxide feeding chamber (5000) is provided with a hydroxide liquid discharge port (5500) for discharging the liquid of the hydroxide feeding chamber (5000) into the anode and cathode reaction chamber (3000), and the raw materials include hydroxide and carbon fuel; The cathode and cathode reaction chamber (3000) is a trough structure with an opening at the upper end. A vertical partition (3100) is arranged inside the cathode and cathode reaction chamber (3000) to divide the cathode and cathode reaction chamber (3000) into an anode reaction chamber (3200) and a cathode reaction chamber (3300). Current collecting screens (3400) are arranged inside the anode reaction chamber (3200) and the cathode reaction chamber (3300). The current collecting screens (3400) include an anode current collecting screen (3410) and a cathode current collecting screen (3420). A wire connection end is arranged at the upper end of the current collecting screen (3400), and the wire connection end is connected to a current collecting device outside the heat preservation oven (1000) through a wire. Before the battery is operated, a certain amount of hydroxide powder is stored in the cathode and anode reaction chambers (3000) and the hydroxide feed chamber (5000), respectively, and a carbon slurry mixture composed of a certain amount of carbon fuel and hydroxide powder mixed in proportion is stored in the carbon slurry mixing feed chamber (4000); The waste liquid storage tank (2000) is configured to receive waste liquid discharged from the anode and cathode reaction chambers (3000).

2. The hydroxide carbon fuel continuous reaction cell device according to claim 1, characterized in that: The anode reaction chamber (3200) is provided with a vertically placed anode reaction chamber baffle plate (3210) and an anode reaction chamber overflow plate (3220) in sequence from right to left. The height of the anode reaction chamber baffle plate (3210) is higher than the anode reaction chamber overflow plate (3220). There is a gap between the bottom surface of the anode reaction chamber baffle plate (3210) and the bottom wall of the anode reaction chamber (3200). The bottom surface of the anode reaction chamber overflow plate (3220) is sealed and connected to the bottom wall of the anode reaction chamber (3200).

3. The hydroxide carbon fuel continuous reaction cell device according to claim 1, characterized in that: The carbon slurry mixing feed chamber (4000) and the hydroxide feed chamber (5000) are both trough structures with an opening at the upper end, the feed port is a groove arranged on the side wall of the trough body, the groove is a structure with openings at both ends of the upper end face and the inner side face, a feeder is arranged in the groove, the feeder is a round tube, the lower end face of the round tube and the bottom face of the groove have a gap, and the top face of the round tube extends above the shell of the heat preservation oven (1000).

4. The hydroxide carbon fuel continuous reaction cell device according to claim 2, characterized in that: An anode reaction chamber drainage port (3230) is provided at the bottom of the anode reaction chamber (3200); the anode reaction chamber drainage port (3230) is a through hole penetrating the bottom wall of the anode reaction chamber (3200); the anode reaction chamber drainage port (3230) is located between the anode reaction chamber overflow plate (3220) and the left side wall of the anode reaction chamber (3200); The bottom of the anode and cathode reaction chamber (3000) is provided with a washing liquid port (3500), the washing liquid port (3500) is a through hole penetrating the bottom wall of the anode and cathode reaction chamber (3000), and the washing liquid port (3500) is provided with a plug.

5. The hydroxide carbon fuel continuous reaction cell device according to claim 1, characterized in that: A vertically placed hydroxide baffle plate (5100) and a hydroxide overflow plate (5200) are arranged in the hydroxide feed chamber (5000); a gap is provided between the bottom surface of the hydroxide baffle plate (5100) and the bottom wall of the hydroxide feed chamber (5000); the bottom surface of the hydroxide baffle plate (5100) is lower than the top surface of the hydroxide overflow plate (5200); the bottom surface of the hydroxide overflow plate (5200) is sealed to the bottom wall of the hydroxide feed chamber (5000); and the top surface of the hydroxide overflow plate (5200) is lower than the top surface of the hydroxide baffle plate (5100).

6. The hydroxide carbon fuel continuous reaction cell device according to claim 1, characterized in that: The current collecting screen (3400) is movably connected to the anode and cathode reaction chambers (3000).

7. The hydroxide carbon fuel continuous reaction cell device according to claim 1, characterized in that: A stirrer is provided in both the anode reaction chamber (3200) and the carbon slurry mixing feed chamber (4000), the stirrer comprising a stirring shaft and blades, the stirring shaft is connected to the motor (6000), and the blades of the stirrer extend to the anode reaction chamber (3200) and the carbon slurry mixing feed chamber (4000), respectively.

8. The hydroxide carbon fuel continuous reaction cell device according to claim 1, characterized in that: A sampling port (1100) is arranged on the upper surface of the outer shell of the heat preservation oven (1000), and a cover plate (1110) for sealing the sampling port and a sampler (1120) for extracting liquid through the sampling port are arranged on the sampling port (1100).

9. The hydroxide carbon fuel continuous reaction cell device according to claim 1, characterized in that: The hydroxide is selected from one or more mixtures of sodium hydroxide, potassium hydroxide, and lithium hydroxide. The carbon fuel particles have a particle size of millimeters or micrometers, a density range of 0.5-1.7g / cm³, a specific surface area of ​​5-700m² / g, and a conductivity range of 100-12900S / m.

10. A method for generating electricity, characterized in that: Using the battery device according to any one of claims 1 to 9 to generate electricity comprises the following steps: (1) adding a hydroxide raw material into the cathode and anode reaction chambers (3000) and the hydroxide feed chamber (5000), and adding a carbon slurry mixture including a carbon fuel and a hydroxide mixed in proportion into the carbon slurry mixing feed chamber (4000); (2) After the heat preservation oven is preheated to the target temperature, the carbon slurry mixture is continuously added to the carbon slurry mixing feed chamber (4000), and the molten mixed reaction liquid obtained by stirring and mixing flows into the anode reaction chamber (3200) below through the carbon slurry mixing discharge port (4300) at a suitable rate; the hydroxide is continuously added to the hydroxide feed chamber (5000), and the molten hydroxide flows into the cathode reaction chamber (3300) below through the hydroxide discharge port (5500) at a suitable rate; the carbon slurry mixture and the molten hydroxide undergo an oxidation reaction in the anode and cathode reaction chambers (3000) to lose electrons, and the electrons are conducted to the current collecting device through the current collecting screen (3400); (3) After the battery device has been running stably for a period of time, the liquid levels in the cathode and anode reaction chambers (3000) gradually rise and exceed the height of the overflow plate (3220) of the anode reaction chamber, and the reaction waste liquid is discharged into the waste liquid storage tank (2000) through the anode reaction chamber discharge port (3230); (4) After the battery device is operated, a cleaning agent is injected to clean the battery device, and the cleaning waste liquid is discharged through the cleaning liquid port (3500) at the bottom of the anode and cathode reaction chamber, thereby achieving rapid cleaning of the anode and cathode reaction chamber (3000).

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