CN213483781U - Catalyst in-situ preparation device for flow battery - Google Patents
Catalyst in-situ preparation device for flow battery Download PDFInfo
- Publication number
- CN213483781U CN213483781U CN202022137396.8U CN202022137396U CN213483781U CN 213483781 U CN213483781 U CN 213483781U CN 202022137396 U CN202022137396 U CN 202022137396U CN 213483781 U CN213483781 U CN 213483781U
- Authority
- CN
- China
- Prior art keywords
- negative
- electroplating
- catalyst
- electrolyte
- positive
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
Landscapes
- Hybrid Cells (AREA)
Abstract
The utility model discloses a catalyst in-situ preparation device for a flow battery, which comprises a negative porous electrode, a diaphragm, a positive porous electrode, a negative current collector, a positive electrolyte storage tank, a positive side pipeline, a positive side drive pump, a negative electrolyte storage tank, a negative side drive pump, a negative side pipeline, an electroplating liquid storage tank, an electroplating side pipeline, a negative electrolyte valve, an electroplating bypass valve and a negative electrolyte valve, through the arranged electroplating bypass, the electroplating liquid storage tank and the electroplating liquid, the ion concentration of catalyst precursor ions in the electroplating liquid is improved, the catalyst is more uniformly distributed on the cathode of the flow battery, meanwhile, intermittent electroplating can be adopted, so that catalyst particles are smaller, the particle density and uniformity are higher, and the problem that the existing catalyst is unevenly distributed and blocks a porous electrode is solved.
Description
Technical Field
The invention belongs to the field of large-scale energy storage, and particularly relates to a device for in-situ preparation of a flow battery catalyst.
Background
The flow battery is an advanced electrochemical electricity storage technology, and can be divided into the following active substances according to the adopted positive and negative electrode active substances: all-vanadium, all-lead, sulfur bromine, zinc bromine, iron chromium flow batteries and the like. For the preparation problem of the flow battery catalyst, a common method is to add precursor ions of the catalyst, such as bismuth ions, into the electrolyte after the battery is assembled, and then directly electroplate the catalyst metal bismuth to the negative electrode of the flow battery by an online in-situ electroplating method. Compared with the traditional scheme of loading the catalyst on the electrode in advance, the scheme of plating the catalyst in situ has the advantage of simple operation, and if the catalyst is damaged or has performance decay, the catalyst can be prepared in situ again.
For the in-situ electroplating process, the quality of the electroplating process directly influences whether the catalyst can be uniformly distributed on the flow battery electrode. The flow battery is generally applied to a continuous discharge scene for hours, and the volume of electrolyte stored in the liquid storage tank is often larger. The loading requirement of the catalyst on the electrode is often certain (too high loading also can block the porous electrode), so the ion concentration formed by dissolving the precursor salt of the catalyst in the electrolyte is often very low (generally less than 0.3mM), and the electrodeposited metal particles are easy to agglomerate. If the catalyst is mainly accumulated in the inlet region or the upstream region after plating, there is a possibility that the flow of the electrolyte in the porous electrode is directly blocked, resulting in deterioration of the battery performance. How to uniformly distribute the catalyst in the porous electrode is an important issue for improving the flow battery. However, the in situ plating process is currently under very rare investigation. The invention provides an electroplating device, which can uniformly distribute a catalyst on an electrode and greatly improve the performance of a flow battery.
Disclosure of Invention
The invention mainly overcomes the defects in the prior art, and aims to provide a device for in-situ preparation of a flow battery catalyst, so that the catalyst is uniformly distributed on an electrode, and the performance of the flow battery is greatly improved.
In order to achieve the technical purpose, the invention adopts the following technical scheme:
an in-situ preparation device for a catalyst for a flow battery, the in-situ preparation device for the catalyst for the flow battery comprising: the battery comprises a negative porous electrode, a diaphragm, a positive porous electrode, a negative current collector, a positive electrolyte storage tank, a positive side pipeline, a positive side driving pump, a negative electrolyte storage tank, a negative side driving pump, a negative side pipeline, an electroplating liquid storage tank, an electroplating by-pass pipeline, a negative side pipeline, a negative electrolyte upper valve, an electroplating by-pass valve and a negative electrolyte lower valve, wherein the diaphragm divides the battery into a positive side and a negative side which are mutually independent, the negative porous electrode is connected with the negative current collector, the positive porous electrode is connected with the positive current collector, the positive side and the positive electrolyte storage tank form a closed loop, the positive electrolyte circularly flows through the positive porous electrode through the positive side pipeline under the action of the positive side driving pump to participate in chemical reaction to form a positive half battery, and the negative side and the negative electrolyte storage tank form a closed loop, the negative electrode electrolyte circularly flows through the negative electrode porous electrode under the action of the negative electrode side drive pump through the negative electrode upper side pipeline and the negative electrode lower side pipeline, and participates in chemical reaction under the state that the negative electrode electrolyte upper valve and the negative electrode electrolyte lower valve are opened to form a negative electrode half cell, the electroplating liquid storage tank is filled with electroplating liquid, the electroplating liquid contains catalyst precursor salt, when the negative electrode electrolyte upper valve and the negative electrode electrolyte lower valve are closed, the electroplating bypass valve is opened, the electroplating liquid passes through the negative electrode upper side pipeline and the electroplating bypass pipeline, and forms a closed loop through the negative electrode porous electrode under the action of the negative electrode side drive pump to form electroplating bypass circulation, the positive electrode half cell, the negative electrode half cell and the electroplating bypass circulation jointly form a catalyst in-situ preparation device for the flow battery, and the catalyst in-situ preparation for the flow battery is completed through the, and after the electroplating is finished, closing the electroplating bypass valve, and opening the cathode electrolyte upper valve and the cathode electrolyte lower valve to switch the battery cathode to the cathode upper side pipeline and the cathode lower side pipeline to perform normal charge-discharge circulation.
Preferably, the area of the single cell of the flow battery is (30-60) × (50-100) cm2。
Preferably, the capacities of the positive electrolyte storage tank (6) and the negative electrolyte storage tank (9) are 50L-2500L.
Preferably, the capacity of the electroplating liquid storage tank (12) is 0.2L-20L.
Preferably, the electroplating liquid storage tank (12) is cylindrical in shape.
Preferably, the shape of the electroplating liquid storage tank (12) is square.
Preferably, the negative electrolyte upper valve (15), the negative electrolyte lower valve (17) and the electroplating bypass valve (16) are electromagnetic valves.
This application is through electroplating bypass and electroplating liquid storage pot and plating solution that sets up in negative pole half cell one side, because electroplating the liquid storage pot is less, plating solution wherein is less, under the condition of catalyst loading capacity on given electrode, catalyst precursor salt can form higher concentration in the plating solution, this kind of plating solution that contains catalyst precursor salt of higher concentration, can be so that the electroplating in-process, the catalyst is in porous electrode's upstream district and all even distribution in downstream district, improve the homogeneity of catalyst distribution by a wide margin, the problem that the catalyst blockked up electrolyte flow in upstream district has greatly been avoided, reduce flow resistance effectively, improve battery output performance.
The device that this application provided can also accomplish the preparation of catalyst with the electroplating scheme of high current intermittent type electroplating, and the intermittent type electroplates the principle as follows, and when electroplating was opened, catalyst precursor concentration reduces gradually, especially in electrode downstream district, and precursor salt concentration consumption can appear even and be zero, leads to the downstream district not to have the catalyst and distributes. At a suitable time when the catalyst precursor salt in the downstream region is about to be depleted, the electroplating process is suspended, and the electroplating is in a 'rest' state. At the moment, the electroplating is suspended, the catalyst precursor salt is not continuously consumed, the pump continuously conveys new electroplating solution into the porous electrode to increase the concentration of the catalyst precursor salt in the porous electrode, and when the concentration of the catalyst precursor is recovered to a proper time, the electroplating process is started again to perform intermittent electroplating in cycles, so that the catalyst can be uniformly distributed in the upstream and downstream regions of the porous electrode. The intermittent current is adopted for electroplating, so that the distribution of the catalyst can be further improved, and the catalyst particles are smaller and the distribution is more dispersed.
Has the advantages that:
1. through the electroplating bypass and the electroplating liquid storage tank that set up in negative pole half cell one side, because electroplating the liquid storage tank is less, electroplating solution wherein is less, under the condition of catalyst loading capacity on given electrode, catalyst precursor salt can form higher concentration in the electroplating solution, this kind of electroplating solution that contains catalyst precursor salt of higher concentration, can be so that the electroplating in-process, the catalyst is at the upstream district of porous electrode and the homogeneous distribution of downstream district, improve the homogeneity of catalyst distribution by a wide margin, the problem that the local reunion of catalyst in upstream district blockked up the electrolyte and flow has reduced the flow resistance effectively, improve battery output performance.
2. Traditional catalyst electroplating uses constant current to carry out, and under given catalyst precursor salt concentration, the too high constant current also can lead to the catalyst to take place local reunion in electrode upstream area, and the device that this application provided can adopt the electroplating scheme of high current intermittent type electroplating to accomplish the preparation of catalyst, and the intermittent type electroplating principle is as follows, and when electroplating was opened, catalyst precursor concentration reduces gradually, especially in electrode downstream area, and precursor salt concentration consumption can even appear zero, leads to the downstream area not to have the catalyst to distribute. At a suitable time when the catalyst precursor salt in the downstream region is about to be depleted, the electroplating process is suspended, and the electroplating is in a 'rest' state. At the moment, the electroplating is suspended, the catalyst precursor salt is not continuously consumed, the pump continuously conveys new electroplating solution into the porous electrode to increase the concentration of the catalyst precursor salt in the porous electrode, and when the concentration of the catalyst precursor is recovered to a proper time, the electroplating process is started again to perform intermittent electroplating in cycles, so that the catalyst can be uniformly distributed in the upstream and downstream regions of the porous electrode. The intermittent current is adopted for electroplating, so that the distribution of the catalyst can be further improved, and the catalyst particles are smaller and the distribution is more dispersed.
3. According to the catalyst in-situ preparation device for the flow battery, the electroplating bypass, the electroplating liquid storage tank and the electroplating liquid are arranged on one side of the negative electrode half battery, so that in-situ electroplating of the catalyst can be performed before the flow battery is charged and discharged, and the in-situ electroplating process can be performed again after the appearance of the catalyst is changed after the flow battery is charged and discharged for a certain time.
Drawings
Fig. 1 is a schematic view of an in-situ preparation apparatus for a catalyst for a flow battery according to an embodiment of the present invention.
Wherein, 1 is a negative porous electrode, 2 is a diaphragm, 3 is a positive porous electrode, 4 is a negative current collector, 5 is a positive current collector, 6 is a positive electrolyte storage tank, 7 is a positive side pipeline, 8 is a positive side drive pump, 9 is a negative electrolyte storage tank, 10 is a negative side drive pump, 11 is a negative side pipeline, 12 is an electroplating storage tank, 13 is an electroplating bypass pipeline, 14 is a negative side pipeline, 15 is a negative electrolyte upper valve, 16 is an electroplating bypass valve, and 17 is a negative electrolyte lower valve.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail with reference to the following embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Example methods
The application discloses a catalyst normal position preparation facilities for flow battery, the subassembly includes: the battery comprises a negative porous electrode (1), a diaphragm (2), a positive porous electrode (3), a negative current collector (4), a positive current collector (5), a positive electrolyte liquid storage tank (6), a positive side pipeline (7), a positive side drive pump (8), a negative electrolyte liquid storage tank (9), a negative side drive pump (10), a negative side upper pipeline (11), an electroplating liquid storage tank (12), an electroplating by-pass pipeline (13), a negative side pipeline (14), a negative electrolyte upper valve (15), an electroplating by-pass valve (16) and a negative electrolyte lower valve (17), wherein the diaphragm (2) separates the battery into a positive side and a negative side which are mutually independent, the negative porous electrode (1) is connected with the negative current collector (4), the positive porous electrode (3) is connected with the positive current collector (5), and the positive side and the positive electrolyte liquid storage tank (6) form a closed loop, the positive electrolyte circularly flows through the positive porous electrode (3) through the positive pipeline (7) under the action of the positive side drive pump (8) to participate in chemical reaction to form a positive half cell, the negative side and the negative electrolyte storage tank (9) form a closed loop, the negative electrolyte circularly flows through the negative porous electrode (1) under the action of the negative side drive pump (10) to participate in chemical reaction to form a negative half cell through the negative upper pipeline (11) and the negative lower pipeline (14) under the state that the negative electrolyte upper valve (15) and the negative electrolyte lower valve (17) are opened, the electroplating bypass valve (16) is opened when the negative electrolyte upper valve (15) and the negative electrolyte lower valve (17) are closed, the electroplating liquid is stored in the negative porous electrode storage tank (11) and the electroplating bypass pipeline (13), under the action of a negative electrode side driving pump (10), a closed loop is formed by flowing through a negative electrode porous electrode (1), an electroplating bypass circulation is formed, a positive electrode half cell, a negative electrode half cell and the electroplating bypass circulation jointly form a catalyst in-situ preparation device for the flow battery, the catalyst in-situ preparation for the flow battery is completed through the electroplating bypass circulation, after the electroplating is completed, an electroplating bypass valve (16) is closed, a negative electrode electrolyte upper valve (15) and a negative electrode electrolyte lower valve (17) are opened, and the negative electrode of the battery is switched to a negative electrode upper side pipeline (11) and a negative electrode lower side pipeline (14) to perform normal charging and discharging circulation.
The concrete mode is as follows:
1) when a constant current plating scheme is employed
The concentration of catalyst precursor salt contained in electroplating solution contained in an electroplating solution storage tank in the catalyst in-situ preparation method is 2-100mmol, and the catalyst is uniformly plated on a negative porous electrodeThe specific loading amount of the preparation is 0.2-10mg/cm2。
Through the electroplating bypass and the electroplating liquid storage tank that set up in negative pole half cell one side, because electroplating the liquid storage tank is less, electroplating solution wherein is less, under the condition of catalyst loading capacity on given electrode, catalyst precursor salt can form higher concentration in the electroplating solution, this kind of electroplating solution that contains catalyst precursor salt of higher concentration, can be so that the electroplating in-process, the catalyst is at the upstream district of porous electrode and the homogeneous distribution of downstream district, improve the homogeneity of catalyst distribution by a wide margin, the problem that the local reunion of catalyst in upstream district blockked up the electrolyte and flow has reduced the flow resistance effectively, improve battery output performance.
2) When an intermittent electroplating scheme is adopted
A. The opening time interval of the electroplating current of the intermittent current method is 0.1-5 seconds, and the electroplating current density is 5-50 mA cm-2The plating current was turned off for a time interval of 1 to 10 seconds, and the plating was continued in this intermittent manner until the catalyst precursor salt in the plating solution was completely consumed.
B. After the intermittent current method is repeated for a plurality of periods of electroplating, when the concentration of the catalyst precursor salt in the electroplating solution is reduced to 30-80% of the initial concentration, the electroplating is changed into constant current electroplating, and the current intensity of the constant current electroplating is 2-30 mA cm-2And electroplating at constant current until the catalyst precursor salt in the electroplating solution is completely consumed.
Example 1
As shown in FIG. 1, the area of the all-vanadium redox flow battery cell is 30x50cm2150L of electrolyte is respectively stored in the positive and negative liquid storage tanks, wherein the concentration of vanadium ions is 1.5M/L. The bypass plating solution storage tank is only 1.0L, wherein the concentration of bismuth chloride is 8 mM/L. And during electroplating, an electroplating bypass valve (16) is opened, a negative electrolyte upper valve (15) and a negative electrolyte lower valve (17) are closed, and the negative electrode of the vanadium battery is switched to the electroplating bypass. During electroplating, the flow rate is 3L/min, and the adopted electroplating current density is 10mA cm-2The electroplating process is carried out for 1 second, the rest is carried out for 2 seconds, the period is 60 periods, and then the constant current is 3mA cm-2Electroplating until bismuth is separatedThe seed is completely consumed. After the electroplating is finished, the electroplating bypass valve (16) is closed, the negative electrolyte upper valve (15) and the negative electrolyte lower valve (17) are opened, and the battery is charged and discharged normally. Under constant current conditions, the voltage drop across the cell remains constant. 140mAcm-2Under the constant-current charging and discharging condition, the energy efficiency of the battery reaches 82%.
Example 2
As shown in figure 1, the all-vanadium redox flow battery pile is formed by connecting 3 layers of single cells in series, and the area of each single cell is 30x50cm2250L of electrolyte is respectively stored in the positive and negative liquid storage tanks, wherein the concentration of vanadium ions is 1.5M/L. The bypass plating solution storage tank is only 1.5L, wherein the concentration of bismuth chloride is 14 mM/L. And during electroplating, an electroplating bypass valve (16) is opened, a negative electrolyte upper valve (15) and a negative electrolyte lower valve (17) are closed, and the negative electrode of the vanadium battery is switched to the electroplating bypass. During electroplating, the flow rate is 8L/min, and the adopted electroplating current density is 8mA cm-2The electroplating process is carried out for 0.5 second, the operation is carried out for 1 second, the operation is carried out for 100 cycles by taking the operation as a cycle, and then the constant current is carried out for 2mA cm-2Electroplating is carried out until bismuth ions are completely consumed. After the electroplating is finished, the electroplating bypass valve (16) is closed, the negative electrolyte upper valve (15) and the negative electrolyte lower valve (17) are opened, and the battery is charged and discharged normally. Under constant current conditions, the voltage drop across the cell remains constant. 150mAcm-2Under the condition of constant current charging and discharging, the energy efficiency of the battery reaches 80 percent.
Example 3
As shown in figure 1, the all-vanadium redox flow battery pile is formed by connecting 3 layers of single cells in series, and the area of each single cell is 30x50cm2250L of electrolyte is respectively stored in the positive and negative liquid storage tanks, wherein the concentration of vanadium ions is 1.5M/L. The bypass plating solution storage tank is only 1.5L, wherein the concentration of bismuth chloride is 2 mM/L. And during electroplating, an electroplating bypass valve (16) is opened, a negative electrolyte upper valve (15) and a negative electrolyte lower valve (17) are closed, and the negative electrode of the vanadium battery is switched to the electroplating bypass. During electroplating, the flow rate is 8L/min, and the adopted electroplating current density is 5mA cm-2The electroplating process is carried out for 0.1 second, the rest is carried out for 1 second, the period is taken as 100 periods, and then the electroplating is carried out by constant current of 2mA cm-2 until the bismuth ions are completely consumed. Electric powerAfter the plating is finished, the plating bypass valve (16) is closed, the negative electrolyte upper valve (15) and the negative electrolyte lower valve (17) are opened, and the battery is charged and discharged normally. Under constant current conditions, the voltage drop across the cell remains constant. 120mAcm-2Under the condition of constant current charging and discharging, the energy efficiency of the battery reaches 80 percent.
Example 4
As shown in figure 1, the all-vanadium redox flow battery pile is formed by connecting 3 layers of single cells in series, and the area of each single cell is 30x50cm2250L of electrolyte is respectively stored in the positive and negative liquid storage tanks, wherein the concentration of vanadium ions is 1.5M/L. The bypass plating solution storage tank is only 0.3L, wherein the concentration of bismuth chloride is 50 mM/L. And during electroplating, an electroplating bypass valve (16) is opened, a negative electrolyte upper valve (15) and a negative electrolyte lower valve (17) are closed, and the negative electrode of the vanadium battery is switched to the electroplating bypass. During electroplating, the flow rate is 8L/min, and the adopted electroplating current density is 50mA cm-2The electroplating process is carried out for 0.1 second, the rest is carried out for 10 seconds, 70 cycles are carried out by taking the rest as the cycle, and then the electroplating is carried out by constant current of 20mA cm & lt-2 & gt until the bismuth ions are completely consumed. After the electroplating is finished, the electroplating bypass valve (16) is closed, the negative electrolyte upper valve (15) and the negative electrolyte lower valve (17) are opened, and the battery is charged and discharged normally. Under constant current conditions, the voltage drop across the cell remains constant. 110mAcm-2Under the constant-current charging and discharging condition, the energy efficiency of the battery reaches 82%.
Comparative example 1
The all-vanadium redox flow battery pile is formed by connecting 3 layers of single cells in series, wherein the area of each single cell is 30x50cm250L of electrolyte is respectively stored in the positive and negative liquid storage tanks, wherein the concentration of vanadium ions is 1.5M/L, and the concentration of bismuth chloride is 0.4 mM/L. During electroplating, the flow rate is 8L/min, and the adopted electroplating current density is 2mA cm-2And (4) carrying out electroplating by constant current until bismuth ions are completely consumed. After completion of the plating, it was found that the stack voltage dropped by 80%, the electrolyte flow characteristics deteriorated, and the battery performance deteriorated. 80mAcm-2Under the constant current charging and discharging condition, the energy efficiency of the battery is only 70%.
The device that this application provided adopts the electroplating scheme of high current intermittent type electroplating to accomplish the preparation of catalyst, and the intermittent type electroplates the principle as follows, and when electroplating was opened, catalyst precursor concentration reduces gradually, especially in electrode downstream district, and precursor salt concentration consumption can appear even and be zero, leads to the downstream district not to have the catalyst and distributes. At a suitable time when the downstream region catalyst precursor salt is about to be depleted, the electroplating process is halted, leaving the electroplating in a "rest" state. At the moment, the electroplating is suspended, the catalyst precursor salt is not continuously consumed, the pump continuously conveys new electroplating solution into the porous electrode to increase the concentration of the catalyst precursor salt in the porous electrode, and when the concentration of the catalyst precursor is recovered to a proper time, the electroplating process is started again to perform intermittent electroplating in cycles, so that the catalyst can be uniformly distributed in the upstream and downstream regions of the porous electrode. The intermittent current is adopted for electroplating, so that the distribution of the catalyst can be further improved, and the catalyst particles are smaller and the distribution is more dispersed.
The preparation of the catalyst for the redox flow battery can be in-situ electroplating of the catalyst before the charging and discharging of the redox flow battery, or can be in-situ electroplating process again after the morphology of the catalyst is changed after the redox flow battery is subjected to charging and discharging operation for a certain time, wherein the in-situ electroplating method of the redox flow battery after the charging and discharging operation for the certain time is as follows: the redox flow battery is completely discharged, at the moment, the charge state of the electrolyte is 0%, then the cathode electrolyte valve is closed, the electroplating bypass valve is opened, at the moment, the cathode electroplating solution flows through the cathode porous electrode under the action of the cathode side driving pump through the cathode side pipeline and the electroplating bypass pipeline, then, the redox flow battery is further discharged, the catalyst is oxidized and dissolved, and after the catalyst is completely dissolved, the in-situ electroplating process can be carried out again.
Although the present invention has been described with reference to the above embodiments, it should be understood that the present invention is not limited to the above embodiments, and those skilled in the art can make various changes and modifications without departing from the scope of the present invention.
Claims (7)
1. An in-situ preparation device for a catalyst for a flow battery, the in-situ preparation device for the catalyst for the flow battery comprising: the battery comprises a negative porous electrode (1), a diaphragm (2), a positive porous electrode (3), a negative current collector (4), a positive current collector (5), a positive electrolyte liquid storage tank (6), a positive side pipeline (7), a positive side drive pump (8), a negative electrolyte liquid storage tank (9), a negative side drive pump (10), a negative side upper pipeline (11), an electroplating liquid storage tank (12), an electroplating by-pass pipeline (13), a negative side pipeline (14), a negative electrolyte upper valve (15), an electroplating by-pass valve (16) and a negative electrolyte lower valve (17), wherein the diaphragm (2) separates the battery into a positive side and a negative side which are mutually independent, the negative porous electrode (1) is connected with the negative current collector (4), the positive porous electrode (3) is connected with the positive current collector (5), and the positive side and the positive electrolyte liquid storage tank (6) form a closed loop, the positive electrolyte circularly flows through the positive porous electrode (3) through the positive pipeline (7) under the action of the positive side drive pump (8) to participate in chemical reaction to form a positive half cell, the negative side and the negative electrolyte storage tank (9) form a closed loop, the negative electrolyte circularly flows through the negative porous electrode (1) under the action of the negative side drive pump (10) to participate in chemical reaction to form a negative half cell through the negative upper pipeline (11) and the negative lower pipeline (14) under the state that the negative electrolyte upper valve (15) and the negative electrolyte lower valve (17) are opened, the electroplating bypass valve (16) is opened when the negative electrolyte upper valve (15) and the negative electrolyte lower valve (17) are closed, the electroplating liquid is stored in the negative porous electrode storage tank (11) and the electroplating bypass pipeline (13), under the action of a negative electrode side driving pump (10), a closed loop is formed by flowing through a negative electrode porous electrode (1), an electroplating bypass circulation is formed, a positive electrode half cell, a negative electrode half cell and the electroplating bypass circulation jointly form a catalyst in-situ preparation device for the flow battery, the catalyst in-situ preparation for the flow battery is completed through the electroplating bypass circulation, after the electroplating is finished, an electroplating bypass valve (16) is closed, a negative electrode electrolyte upper valve (15) and a negative electrode electrolyte lower valve (17) are opened, and a battery negative electrode is switched to a negative electrode upper side pipeline (11) and a negative electrode lower side pipeline (14) to perform normal charging and discharging circulation.
2. The in-situ preparation device of catalyst for flow battery according to claim 1, wherein the electrode area of single cell of the flow battery is (30-60) × (50-100) cm2。
3. The in-situ preparation device of the catalyst for the flow battery, according to claim 1, wherein the capacities of the positive electrolyte storage tank (6) and the negative electrolyte storage tank (9) are 50L-2500L.
4. The in-situ preparation device of the catalyst for the flow battery, according to claim 1, wherein the capacity of the electroplating liquid storage tank (12) is 0.2L-20L.
5. The in-situ preparation device of the catalyst for the flow battery, according to claim 1, wherein the electroplating liquid storage tank (12) is cylindrical in shape.
6. The in-situ preparation device of the catalyst for the flow battery, according to claim 1, wherein the electroplating liquid storage tank (12) is square in shape.
7. The in-situ preparation device of the catalyst for the flow battery, according to claim 1, wherein the negative electrolyte upper valve (15), the negative electrolyte lower valve (17) and the plating bypass valve (16) are solenoid valves.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022137396.8U CN213483781U (en) | 2020-09-25 | 2020-09-25 | Catalyst in-situ preparation device for flow battery |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022137396.8U CN213483781U (en) | 2020-09-25 | 2020-09-25 | Catalyst in-situ preparation device for flow battery |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN213483781U true CN213483781U (en) | 2021-06-18 |
Family
ID=76362979
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022137396.8U Active CN213483781U (en) | 2020-09-25 | 2020-09-25 | Catalyst in-situ preparation device for flow battery |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN213483781U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112164805A (en) * | 2020-09-25 | 2021-01-01 | 西南交通大学 | In-situ preparation device and method of catalyst for flow battery |
-
2020
- 2020-09-25 CN CN202022137396.8U patent/CN213483781U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112164805A (en) * | 2020-09-25 | 2021-01-01 | 西南交通大学 | In-situ preparation device and method of catalyst for flow battery |
| CN112164805B (en) * | 2020-09-25 | 2024-07-16 | 西南交通大学 | In-situ preparation device and preparation method of catalyst for flow battery |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103137986B (en) | A kind of zinc bromine single flow battery | |
| CN102201590B (en) | Acidic zinc single liquid flow energy storage battery | |
| CN109509901B (en) | Alkaline zinc-iron flow battery | |
| Pan et al. | Preliminary study of alkaline single flowing Zn–O2 battery | |
| CN113270624B (en) | Flow battery subsystem with catalyst management and electrolyte capacity rebalancing | |
| CN106549189A (en) | Battery, set of cells and uninterrupted power source | |
| CN213483781U (en) | Catalyst in-situ preparation device for flow battery | |
| CN113678218B (en) | Water system mixed super capacitor | |
| CN112164805B (en) | In-situ preparation device and preparation method of catalyst for flow battery | |
| CN109728314B (en) | Flow battery structure with magnetic particle attached electrode of external magnetic field and method | |
| CN110224157B (en) | Non-circulating flow battery | |
| JPH0324022B2 (en) | ||
| CN116454341A (en) | Iron-chromium flow battery pile system | |
| CN107845826A (en) | A kind of zinc bromine single flow battery | |
| CN104300169A (en) | Alkaline zinc vanadium flow battery | |
| CN114388859B (en) | Negative electrode electrolyte for all-iron flow battery | |
| KR20160064545A (en) | Zn-Br Redox Flow Battery System | |
| CN116231021A (en) | Recovery method of zinc-bromine flow battery electrolyte | |
| CN108134123A (en) | A kind of pile of redox flow batteries | |
| CN104409691B (en) | Method using rare earth for modification of lead storage battery negative electrode plate | |
| CN114171766A (en) | High-efficiency zinc-iodine adsorption auxiliary flow battery with low-cost film | |
| CN114551935B (en) | Performance recovery method of zinc-bromine single flow battery | |
| CN215265953U (en) | Electrochemical energy storage device with water-based zinc electrode | |
| CN219647779U (en) | Lithium battery slurry automatic circulation demagnetizing system | |
| CN114497644B (en) | Zinc-based single flow battery operation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |