CN117468029A

CN117468029A - Hydrogen production system and method of operating the same

Info

Publication number: CN117468029A
Application number: CN202311324104.3A
Authority: CN
Inventors: 马军; 王永谋; 周长龙
Original assignee: Wuxi Longji Hydrogen Energy Technology Co ltd
Current assignee: Wuxi Longji Hydrogen Energy Technology Co ltd
Priority date: 2023-10-12
Filing date: 2023-10-12
Publication date: 2024-01-30

Abstract

The application discloses a hydrogen production system and an operation method thereof, comprising the following steps: the system comprises a power supply system, a separator, a controller, at least two electrolytic tanks, at least two alkaline pumps and a return pipeline; a power supply system for supplying electric energy to the electrolytic cell; at least two electrolytic tanks are used for electrolyzing the input alkaline electrolyte to generate target gas; at least two electrolytic tanks are arranged in parallel, and rated powers of at least two electrolytic tanks in all electrolytic tanks are different; the reflux pipeline is connected in parallel between the inlet and the outlet of each alkaline pump, and is used for adjusting the flow of alkaline electrolyte entering each electrolytic tank, and the controller is used for controlling the working state of each electrolytic tank according to the hydrogen production power and the rated power of each electrolytic tank. The hydrogen production system is favorable for selecting a proper electrolytic tank to work according to actual hydrogen production power, so that the operation load of the hydrogen production system is reduced, and the purity of gas is ensured to be in a normal range.

Description

Hydrogen production system and method of operating the same

Technical Field

The invention relates to the technical field of new energy hydrogen production, in particular to a hydrogen production system and an operation method thereof.

Background

The combination of new energy power generation and hydrogen energy is one of the important ways to achieve the goals of "carbon peak" and "carbon neutralization". However, the intermittence and uncertainty are remarkable characteristics of new energy power generation such as wind power, photovoltaic and the like, and the alkaline water electrolysis hydrogen production also has the characteristics of long cold start time and more hydrogen waste before qualified gas is produced after purification and operation. At present, the fluctuation of new energy power generation causes that the new energy power generation cannot be effectively matched with the traditional alkaline electrolytic tank under the low-load operation working condition, and the traditional multi-electrolytic tank combined hydrogen production mostly adopts the same high-power electrolytic tank for combined use, so that the whole hydrogen production system has high energy consumption and can generate the condition of unqualified gas purity.

Disclosure of Invention

In view of the foregoing drawbacks or shortcomings of the prior art, it is desirable to provide a hydrogen production system and a method of operating the same, by providing at least two electrolytic cells, which facilitate selection of appropriate electrolytic cells for operation during low load operation of the system, thereby reducing the system operating load and facilitating ensuring that the purity of the gas is in a normal range.

In a first aspect, the present invention provides a hydrogen production system comprising: the system comprises a power supply system, a separator, a controller, at least two electrolytic tanks, at least two alkaline pumps and a return pipeline;

A power supply system for supplying electric energy to the electrolytic cell;

at least two electrolytic tanks are used for electrolyzing the input alkaline electrolyte to generate target gas, and inputting the target gas into a separator;

at least two electrolytic tanks are arranged in parallel, and the rated power of the at least two electrolytic tanks is sequentially recorded as PE from small to large _n-1 ，PE _n ，PE _n+1 ,., n is greater than or equal to 1, wherein PE _n-1 >PE _n 30% of PE _n >PE _n+1 And the rated power of at least two of the cells is different from each other;

each alkaline pump is correspondingly arranged on a pipeline communicated with the inlet of each electrolytic tank, and is used for correspondingly inputting alkaline electrolyte into each electrolytic tank;

a return line is connected in parallel between the inlet and the outlet of each alkaline pump, and the return line is used for adjusting the flow rate of the alkaline electrolyte entering each electrolytic tank;

and the controller is used for acquiring the hydrogen production power provided by the power supply system and controlling the working state of each electrolytic tank according to the hydrogen production power and the rated power of each electrolytic tank.

As an alternative scheme, a first regulating valve is arranged on the return pipeline and used for regulating the return flow of the alkaline electrolyte.

As an alternative scheme, the controller is further configured to obtain an actual flow rate of the alkaline electrolyte in each electrolytic cell, and control the opening of the first regulating valve according to the actual flow rate and a preset rated flow rate of the alkaline electrolyte in each electrolytic cell.

As an alternative scheme, the controller is further configured to obtain an actual purity of the target gas, and control the opening of the first regulating valve according to the actual purity and a preset threshold.

Alternatively, the hydrogen production system further includes: and one end of the alkali liquor circulation pipeline is communicated with the liquid outlet of the separator, the other end of the alkali liquor circulation pipeline is respectively communicated with the inlets of at least two electrolytic tanks, and the alkali liquor circulation pipeline is used for collecting alkaline electrolyte which flows out along with the target gas in at least two electrolytic tanks and respectively conveying the collected alkaline electrolyte to each electrolytic tank.

Alternatively, the alkali liquor circulation pipeline is provided with a cooler, an input port of the cooler is communicated with a liquid outlet of the separator and is used for cooling part of alkaline electrolyte flowing out along with the target gas, and an output port of the cooler is communicated with a pipeline for conveying the collected alkaline electrolyte to each electrolytic tank.

As an alternative scheme, the separator comprises a hydrogen separator and an oxygen separator, wherein the inlet of the hydrogen separator is respectively communicated with the hydrogen outlet of each electrolytic tank, the alkali liquor outlet of the hydrogen separator is respectively communicated with the inlet of each electrolytic tank through an alkali liquor circulation pipeline, the inlet of the oxygen separator is respectively communicated with the oxygen outlet of each electrolytic tank, and the alkali liquor outlet of the oxygen separator is respectively communicated with the inlet of each electrolytic tank through an alkali liquor circulation pipeline.

Alternatively, the number of hydrogen separators is a plurality and the plurality of hydrogen separators are arranged in parallel or in series, and/or the number of oxygen separators is a plurality and the plurality of oxygen separators are arranged in parallel or in series.

As an alternative, a second regulating valve is installed on the cooling liquid inlet pipeline of the cooler, and the second regulating valve is used for regulating the flow rate of the cooling liquid entering the cooler;

the controller controls the opening of the second regulating valve according to the running temperature of each electrolytic tank to regulate the running temperature of each electrolytic tank to be 50-90 ℃.

As an alternative, a scrubbing apparatus is also included, the inlet of which communicates with the separated gas outlet for purifying the target gas.

In a second aspect, the present invention provides a method of operating the hydrogen production system of the first aspect, comprising the steps of:

obtaining hydrogen production power;

and controlling the working state of each electrolytic cell according to the hydrogen production power and the rated power of at least two electrolytic cells.

Alternatively, controlling the operation state of each electrolyzer according to the hydrogen production power and the rated power of at least two electrolyzers, including:

when the hydrogen production power is smaller than or equal to a preset threshold value, determining a first electrolytic cell corresponding to the first rated power as a target electrolytic cell according to the hydrogen production power and the rated powers of at least two electrolytic cells, and controlling the starting of the target electrolytic cell; wherein the first rated power is the smallest rated power;

When the hydrogen production power is greater than a preset threshold value, acquiring the current purity of the target gas according to a first preset period;

and controlling the working state of each electrolytic tank according to the hydrogen production power, the preset load distribution proportion, the current purity and the rated power.

Alternatively, the working state includes opening or closing of each electrolytic cell, and the actual working power of each electrolytic cell, and the working state of each electrolytic cell is controlled according to the hydrogen production power, the preset load distribution proportion, the current purity and the rated power, including:

when the hydrogen production power is less than 85% of the first rated power, controlling the first electrolytic tank corresponding to the first rated power to be opened or closed according to the hydrogen production power, the first threshold value and the purity of the target gas;

the following designating operation is performed, and the designating operation includes:

when the hydrogen production power is greater than or equal to 85% of the first rated power, controlling the working state of the first electrolytic tank corresponding to the first rated power or the second electrolytic tank corresponding to the second rated power according to the hydrogen production power, the second rated power, the second threshold value and the preset load distribution proportion;

the second rated power is the rated power of other electrolytic tanks except the first electrolytic tank corresponding to the first rated power, and the first rated power is smaller than the second rated power;

And updating the first rated power and the second rated power according to the rated power of at least two electrolytic cells, and executing specified operation until each electrolytic cell runs at full load.

As an alternative, the first threshold is 30% of the first rated power, and according to the hydrogen production power, the first threshold and the purity of the target gas, the opening or closing of the first electrolytic cell corresponding to the first rated power is controlled, including:

when the hydrogen production power is larger than a first threshold value, controlling the first electrolytic tank to start;

and when the hydrogen production power is smaller than or equal to a first threshold value and the purity of the target gas is larger than a preset threshold value, controlling the hydrogen production system to stop.

As an alternative, the second threshold is 30% of the second rated power, and according to the hydrogen production power, the second rated power, the second threshold and a preset load distribution ratio, the working state of the first electrolytic cell corresponding to the first rated power or the working state of the second electrolytic cell corresponding to the second rated power is controlled, including:

when the hydrogen production power is greater than a second threshold value and less than 85% of a second rated power, controlling the first electrolytic tank to start or close according to a load distribution proportion, simultaneously controlling the second electrolytic tank to start, and adjusting the actual working power of the first electrolytic tank and the second electrolytic tank;

When the hydrogen production power is smaller than or equal to a second threshold value, the first electrolytic tank and the second electrolytic tank are controlled to be started, and the actual working power of the first electrolytic tank is increased and the actual working power of the second electrolytic tank is reduced according to the load distribution proportion.

Alternatively, controlling the working state of each electrolyzer according to the hydrogen production power and the rated power of at least two electrolyzers, and further comprising:

acquiring the accumulated running time of each electrolytic tank;

and controlling the starting of the electrolytic cell with the shortest running time in the electrolytic cells with the same rated power.

Alternatively, the working state includes the actual flow of the electrolytic cells, and the working state of each electrolytic cell is controlled according to the hydrogen production power, the preset load distribution ratio and the current purity, and the method further includes:

determining the set flow of each electrolytic tank according to the hydrogen production power, the rated power of each electrolytic tank and the preset rated flow of each electrolytic tank;

acquiring the historical flow of each electrolytic tank according to a second preset period;

and controlling and adjusting the actual flow of each electrolytic tank according to the historical flow and the set flow.

As an alternative scheme, according to the hydrogen production power, the rated power of each electrolytic tank and the preset rated flow of each electrolytic tank, the set flow of each electrolytic tank is determined, and the specific formula is as follows:

F=50% fe+5fe/7 (n-30%), where F is the set flow, fe is the rated flow, and n is the ratio of hydrogen production power to rated power.

Alternatively, after controlling and adjusting the actual flow rate of each electrolytic cell according to the historical flow rate and the set flow rate, the method further comprises:

and when the current purity of the target gas is smaller than a preset threshold value, controlling to reduce the actual flow of the electrolytic cell.

As an alternative scheme, after determining that the first electrolytic cell corresponding to the first rated power is the target electrolytic cell according to the hydrogen production power and the rated powers of at least two electrolytic cells, controlling the starting of the target electrolytic cell, the method further comprises:

acquiring the operating temperature of a target electrolytic cell and the current purity of target gas;

and when the current purity of the target gas is smaller than a preset threshold value, controlling to reduce the operating temperature of the target electrolytic cell.

According to the hydrogen production system, at least two electrolytic tanks are arranged, and rated powers of at least two electrolytic tanks in all electrolytic tanks are different, so that the hydrogen production system is beneficial to selecting and controlling proper electrolytic tanks to work according to actual hydrogen production power under the working condition that the power supply load of a new energy power supply system is unstable, thereby reducing the operation load of the hydrogen production system and maintaining the continuous operation of the hydrogen production system; and through the arrangement of the alkaline pump and the return pipeline, the flow rate of the alkaline electrolyte entering each electrolytic tank can be reliably controlled and regulated, so that the flow rate of the alkaline electrolyte in each electrolytic tank can be reduced under the condition of low-load operation of a hydrogen production system, and the purity of gas can be ensured to be in a normal range.

Drawings

Other features, objects and advantages of the present application will become more apparent upon reading of the detailed description of non-limiting embodiments, made with reference to the following drawings, in which:

FIG. 1 is a schematic diagram of a hydrogen production system of the present invention;

FIG. 2 is a flow chart of a method of operating a hydrogen production system of the present invention;

FIG. 3 is a flow chart of another method of operating a hydrogen production system of the present invention;

FIG. 4 is a flow chart of a method of operation of yet another hydrogen production system of the present invention;

FIG. 5 is a flow chart of a method of operating a hydrogen production system in accordance with an embodiment of the present invention;

FIG. 6 is a schematic diagram of a hydrogen production system according to an embodiment of the present invention;

fig. 7 is a schematic structural diagram of a computer system of a terminal device according to an embodiment of the present invention.

In the drawing the view of the figure,

100. a hydrogen production system;

10. the device comprises an electrolytic tank, 20, an alkaline pump, 30, a return pipeline, 40, a first regulating valve, 50, an alkaline circulating pipeline, 70, a cooler, 71, a second regulating valve, 80, a hydrogen separator, 90, an oxygen separator, 91 and a washing device.

Detailed Description

The present application is described in further detail below with reference to the drawings and examples. It is to be understood that the specific embodiments described herein are merely illustrative of the invention and are not limiting of the invention. It should be noted that, for convenience of description, only the portions related to the invention are shown in the drawings.

It should be noted that, in the case of no conflict, the embodiments and features in the embodiments may be combined with each other. The present application will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.

In the related art, in order to maintain continuous operation of the hydrogen production system in a state that the new energy power supply system is unstable in power or low in power, the first solution is that the stopped electrolytic tank needs to be restarted for about 40 minutes to reach the rated working condition, and the second solution is that the purification system needs to be restarted for about 90 minutes to produce the gas with qualified dew point, and the unqualified gas needs to be emptied in the time to form waste of product gas. However, in low power operation, the alkaline electrolyzer has low gas yield due to its own characteristics, the diaphragm also has a certain permeability, and the presence of gas dissolved in the alkaline solution results in poor gas purity in high power electrolyzer operation at low load. Under long-time operation conditions, electric energy is wasted, and generated hydrogen is wasted.

Based on the foregoing, in a first aspect, the present invention provides a hydrogen production system 100, as shown in fig. 1, comprising: a power supply system, a separator, a controller, at least two electrolytic cells 10, at least two lye pumps 20, and a return line 30;

A power supply system for supplying electric power to the electrolytic cell 10;

at least two electrolytic tanks 10 for electrolyzing the input alkaline electrolyte to generate a target gas, and inputting the target gas into a separator;

at least two electrolytic cells 10 are arranged in parallel with each other, and rated power of the at least two electrolytic cells 10 is sequentially denoted by PE _n-1 ，PE _n ，PE _n+1 ,., n is greater than or equal to 1, wherein PE _n-1 >PE _n 30% of PE _n >PE _n+1 And the rated power of at least two cells in all cells is different;

each alkaline pump 20 is correspondingly arranged on a pipeline communicated with the inlet of each electrolytic tank 10, and each alkaline pump 20 is used for correspondingly inputting alkaline electrolyte into each electrolytic tank 10;

a return line 30 is connected in parallel between the inlet and outlet of each of the lye pumps 20, the return line 30 being used to regulate the flow of alkaline electrolyte into each of the cells 10.

And the controller is used for acquiring the hydrogen production power provided by the power supply system and controlling the working state of each electrolytic tank 10 according to the hydrogen production power and the rated power of each electrolytic tank 10.

The power supply system is mainly used for supplying electric energy to the hydrogen production system and electrolyzing alkaline electrolyte in the electrolytic tank 10; the power supply system may be electric energy provided by various new energy power systems, such as but not limited to wind energy, solar energy, lithium battery pack or various new energy batteries, and the embodiment of the present application is not limited thereto.

It can be understood that the electrolytic tank 10 is used for containing alkaline electrolyte and electrolyzing the alkaline electrolyte to generate target gas, the number of the electrolytic tanks 10 can be two or more, and in practical application, the number of the electrolytic tanks 10 can be determined according to the actually required hydrogen production amount and the provided electric energy power of the power supply system; each electrolytic tank 10 is arranged in parallel, and each electrolytic tank 10 can work independently, so that the working efficiency of generating target gas of the hydrogen production system is improved, the operation load of the whole hydrogen production system is reduced, and the energy consumption is saved.

Wherein the rated power of at least two electrolytic cells 10 is denoted PE in turn _n-1 ，PE _n ，PE _n+1 ,., n is greater than or equal to 1, wherein PE _n-1 >PE _n 30% of PE _n >PE _n+1 30% of the total amount of the electrolyte is determined according to the operation condition of each electrolytic tank; the rated powers of at least two electrolytic tanks in all the electrolytic tanks 10 are different, so that when the hydrogen production system operates under the working condition of low load, the electrolytic tanks 10 with proper rated powers can be selected to work, the load of the whole hydrogen production system is reduced, and the purity of the generated target gas is ensured.

In a specific embodiment, four electrolytic cells are arranged in PE from small to large power _n-1 、PE _n 、PE _n+1 ......，PE _n Greater than PE _n+1 30% of PE _n-1 Greater than PE _n 30% of (C), wherein the maximum power is set to 3000Nm ³ /h, minimum power of 500Nm ³ Per h, the combination of the cells 10 may be 500Nm ³ /h，1000Nm ³ /h，2000Nm ³ /h，2000Nm ³ Four powers per h; can also be 500Nm ³ /h，1000Nm ³ /h，2000Nm ³ /h，3000Nm ³ /h; can also be 500Nm ³ /h，1000Nm ³ /h，1000Nm ³ /h，1000Nm ³ /h。

It will be appreciated that the use of the alkaline pump 20 for the corresponding input of alkaline electrolyte into each cell 10 is advantageous in ensuring that an appropriate amount of alkaline electrolyte is maintained throughout each cell 10.

Since the inlet pressure of the alkaline pump 30 is generally lower than the outlet pressure, alkaline liquor reflux is generally formed during operation of the alkaline pump, and the flow rate of the alkaline electrolyte entering the electrolytic tank 10 is accurately and automatically controlled by arranging a reflux pipeline 30 to regulate the flow rate of the alkaline pump reflux.

The controller can be used for acquiring the hydrogen production power provided by the power supply system, acquiring the running temperature of the electrolytic cells and the flow of the alkaline electrolyte of each electrolytic cell, judging whether the hydrogen production power is within the preset range of the rated power or not according to the comparison between the hydrogen production power and the rated power of each electrolytic cell 10, and further controlling the working state of each electrolytic cell 10; the operation state of the electrolytic cell 10 may be the start or stop of the electrolytic cell 10, or may be the actual operation power of the electrolytic cell 10, the actual flow rate of the alkaline electrolyte of the electrolytic cell 10, the operation temperature of the electrolytic cell 10, etc., which is not particularly limited in the embodiment of the present application.

According to the embodiment of the application, the problems that in the prior art, under the working condition of low-load operation of a hydrogen production system, an electrolytic tank with proper power cannot be matched, so that the whole hydrogen production system is high in energy consumption and unqualified in gas purity are solved. According to the embodiment of the application, the at least two electrolytic tanks are arranged, and rated powers of the at least two electrolytic tanks in all the electrolytic tanks are different, so that the hydrogen production system can be controlled to work according to the actual hydrogen production power under the working condition that the power supply load of the new energy power supply system is unstable, and the controller can control the proper electrolytic tanks to work, so that the operation load of the hydrogen production system is reduced, and the continuous operation of the hydrogen production system is maintained; and through the arrangement of the alkaline pump and the return pipeline, the flow rate of the alkaline electrolyte entering each electrolytic tank can be reliably controlled and regulated, so that the flow rate of the alkaline electrolyte in each electrolytic tank can be reduced under the condition of low-load operation of a hydrogen production system, and the purity of gas can be ensured to be in a normal range.

As an achievable way, the return line 30 is provided with a first regulating valve 40, the first regulating valve 40 being used for regulating the return flow of the alkaline electrolyte.

In this embodiment, the parallel connection and the matching of the first adjusting valve 40 and the alkaline pump 20 are beneficial to adjusting the flow of the return line 30 of the alkaline pump 20 through the first adjusting valve 40, so as to accurately and automatically control the flow of the alkaline electrolyte entering the electrolytic tank 10, increase the opening degree of the first adjusting valve 40, effectively reduce the flow of the alkaline electrolyte entering the electrolytic tank 10 from the separator, increase the residence time of the alkaline electrolyte in the separator, and increase the gas precipitation time, thereby reducing the solubility of the target gas in the alkaline electrolyte and further improving the purity of the target gas.

Further, in some embodiments, the controller is configured to obtain an actual flow rate of the alkaline electrolyte in each electrolytic cell 10, and control the opening of the first regulating valve 40 according to the actual flow rate and a preset rated flow rate of the alkaline electrolyte in each electrolytic cell.

The embodiment is beneficial to improving the purity of the target gas when the hydrogen production system runs under low load.

Further, in some embodiments, the controller is further configured to obtain an actual purity of the target gas, and control the opening of the first regulating valve according to the actual purity and a preset threshold.

The preset threshold value is a purity range preset in the controller according to actual production requirements, the controller compares the acquired actual purity of the target gas with the preset threshold value, if the actual purity is not in the preset threshold value range, the opening of the first regulating valve needs to be increased, the flow rate of the alkaline electrolyte entering the electrolytic tank 10 is reduced, the alkaline electrolyte stays in the separator for a longer time, and the separation purity of the target gas is improved.

As an achievable approach, hydrogen production system 100 further includes: and one end of the alkali liquor circulation pipeline 50 is communicated with a liquid outlet of the separator, the other end of the alkali liquor circulation pipeline 50 is respectively communicated with inlets of at least two electrolytic tanks 10, and the alkali liquor circulation pipeline 50 is used for collecting alkaline electrolyte, which flows out along with target gas, in at least two electrolytic tanks 10 and respectively conveying the collected alkaline electrolyte to each electrolytic tank 10.

The method is beneficial to recycling alkaline electrolyte, saving raw materials and improving the purity of target gas.

As a practical way, a cooler 70 is installed on the alkali liquor circulation line 50, the inlet of the cooler 70 is communicated with the liquid outlet of the separator for cooling the alkaline electrolyte partially flowing out with the target gas, and the outlet of the cooler 70 is communicated with the line for conveying the collected alkaline electrolyte to each electrolytic cell.

Wherein the cooling fluid of the cooler 70 may be water or other cooling medium.

The cooler 70 in the present embodiment cools the alkaline electrolyte flowing out with the target gas by means of heat exchange to facilitate recycling of the alkaline electrolyte.

In some embodiments, the separators include a hydrogen separator 80 and an oxygen separator 90, the inlet of the hydrogen separator 80 is respectively connected to the hydrogen outlet of each of the electrolytic cells 10, the lye outlet of the hydrogen separator 80 is respectively connected to the inlet of each of the electrolytic cells 10 through the lye circulation line 50, the inlet of the oxygen separator 90 is respectively connected to the oxygen outlet of each of the electrolytic cells 10, and the lye outlet of the oxygen separator 90 is respectively connected to the inlet of each of the electrolytic cells 10 through the lye circulation line 50.

Further, in other embodiments, the number of hydrogen separators 80 is multiple and the plurality of hydrogen separators 80 are arranged in parallel or in series, and/or the number of oxygen separators 90 is multiple and the plurality of oxygen separators 90 are arranged in parallel or in series.

Wherein, the plurality refers to two or more than two;

the present embodiment is advantageous in improving the separation efficiency and purity of the target gas.

As an achievable way, a second regulating valve 71, the second regulating valve 71 being mounted on the cooling liquid inlet line of the cooler 90, the second regulating valve 71 being for regulating the flow rate of the cooling liquid into the cooler 70;

the controller controls the opening of the second regulating valve 71 according to the operation temperature of each electrolytic cell 10 to adjust the operation temperature of each electrolytic cell 10 to be 50-90 ℃.

In the present embodiment, the second regulating valve 71 may be provided to regulate the temperature of the alkaline electrolyte entering the electrolytic cell 10, and thus the operating temperature of the electrolytic cell 10. Further, in other embodiments, by increasing the opening of the second regulating valve 71, the temperature of the alkaline electrolyte may be further reduced to reduce the operating temperature of each electrolytic cell 10, for example, the operating temperature of each electrolytic cell 10 may be adjusted to be 50-70 ℃, thereby reducing the activity of the gas, avoiding dissolution of the gas, and so on, which is beneficial to improving the purity of the target gas.

As an achievable way, the hydrogen production system 100 further comprises a scrubbing device 91, the inlet of the scrubbing device 91 being in communication with the separated gas outlet for purifying the target gas.

In summary, in the hydrogen production system according to the embodiment of the present application, by providing at least two electrolytic tanks, and the rated powers of at least two electrolytic tanks in all the electrolytic tanks are different, the controller is favorable to selectively control the operation of the appropriate electrolytic tank according to the actual hydrogen production power under the working condition that the power supply load of the new energy power supply system is unstable, so as to reduce the operation load of the hydrogen production system and maintain the continuous operation of the hydrogen production system; the arrangement of the alkaline pump and the return pipeline is beneficial to reliably controlling and adjusting the flow of the alkaline electrolyte entering each electrolytic tank, so that the flow of the alkaline electrolyte in each electrolytic tank is reduced and the purity of the gas is ensured to be in a normal range under the condition of low-load operation of a hydrogen production system;

and by arranging the first regulating valve and the second regulating valve, the flow and the temperature of the alkaline electrolyte entering the electrolytic tank can be controlled, and the purity of the target gas can be improved.

In a second aspect, embodiments of the present application provide a method of operating the hydrogen production system of the first aspect, as shown in fig. 2, comprising the steps of:

S10, obtaining hydrogen production power;

s20, controlling the working state of each electrolytic cell according to the hydrogen production power and the rated power of at least two electrolytic cells.

It should be noted that, the operation method of the hydrogen production system in the embodiment of the present application is executed by the controller;

in step S10, the hydrogen production power may be understood as the power provided by the power supply system, and the controller may obtain the power of the power supply system sent in real time by the power supply system or sent according to a certain period;

in step S20, the hydrogen production power and the rated power of the electrolytic tank are matched to work in accordance with the electrolytic tank of the hydrogen production power, which is beneficial to saving the power consumption of the whole hydrogen production system and improving the working efficiency of the hydrogen production system and the purity of the target gas.

Specifically, when the hydrogen production power is low, that is, the hydrogen production system is in the process of low-load operation, one electrolytic tank with low rated power is selected to work or a plurality of electrolytic tanks work together according to the comparison of the hydrogen production power and the rated power, so long as the load requirement of the whole hydrogen production system is met and the actual working power of each electrolytic tank meets the minimum load requirement of each electrolytic tank;

When the hydrogen production power is higher, in the process that the hydrogen production system is in high-load operation, one electrolytic tank with higher power or a plurality of electrolytic tanks are selected to work together according to the comparison of the hydrogen production power and rated power, so long as the load requirement of the whole hydrogen production system is met, and the actual working power of each electrolytic tank is within the optimal load range of each electrolytic tank.

Further, in some embodiments, step S20, controlling the operation state of each electrolyzer according to the hydrogen production power and the rated power of at least two electrolyzers, as shown in fig. 3, includes:

s21, when the hydrogen production power is smaller than or equal to a preset threshold value, determining a first electrolytic cell corresponding to the first rated power as a target electrolytic cell according to the hydrogen production power and the rated powers of at least two electrolytic cells, and controlling the starting of the target electrolytic cell; wherein the first rated power is the smallest rated power;

it should be noted that, the predetermined threshold is determined according to the working condition of the actual power supply system, and is preset in the controller, for example, the predetermined threshold may be 85% of the minimum rated power of the electrolytic cell;

when the hydrogen production power is smaller than a preset threshold value, determining that the hydrogen production system is in a low-load operation condition, and directly determining an electrolytic cell corresponding to the minimum rated power as a target electrolytic cell by the controller to control the starting work of the electrolytic cell; when the number of the electrolytic cells corresponding to the minimum rated power is 2 or more, the controller can control the electrolytic cell with the shortest accumulated running time to start by acquiring the accumulated running time of each electrolytic cell.

S22, when the hydrogen production power is greater than a preset threshold value, acquiring the current purity of the target gas according to a first preset period;

it is appreciated that when the hydrogen production power is greater than the predetermined threshold, then determining that the hydrogen production system is not in a low load operating condition; the first preset period is determined according to actual production requirements and preset in the controller.

S23, controlling the working state of each electrolytic tank according to the hydrogen production power, the preset load distribution proportion, the current purity and the rated power.

The preset load distribution proportion refers to the actual working power distribution proportion of each electrolytic tank, and the preset load distribution proportion is determined in advance according to the optimal working load of each electrolytic tank; for example, 500Nm ³ The full load of the cell per h is 2.5MW, a 2000Nm ³ The full load of the electrolyzer per hour is 10MW and can be allocated to 500Nm when the hydrogen production power is 10MW ³ The/h cell was 2MW, allocated to 2000Nm ³ The cell per h was 8MW.

And under the working condition that the hydrogen production system is not in low-load operation, the hydrogen production power, the preset load distribution proportion, the current purity and the rated power of the electrolytic cells are synthesized, the working state of each electrolytic cell is controlled, the operation of each electrolytic cell under the optimal working load is ensured, the working efficiency of the whole hydrogen production system is improved, and the purity of target gas is ensured to meet the requirements.

Further, in some embodiments, the operation state of the electrolytic cells includes opening or closing of each electrolytic cell, and actual operation power of each electrolytic cell, S23, controlling the operation state of each electrolytic cell according to hydrogen production power, preset load distribution ratio, current purity and rated power, including:

it should be noted that, the first rated power is the minimum rated power in all the electrolytic cells, so when the hydrogen production power is less than 85% of the first rated power, the hydrogen production system is already in a low-load running state, and therefore, only the start-up or the shut-down of the electrolytic cell corresponding to the first rated power is required to be controlled, and other electrolytic cells are not required to be considered; since each electrolyzer has the lowest work load, for example, the lowest work load of the electrolyzer with the rated power can be 30%, if the hydrogen production power is lower than the lowest work load of the electrolyzer with the smallest rated power, the current power supply system provides very small hydrogen production power, and the electrolyzer with the small rated power needs to be controlled to work, however, in order to ensure the work efficiency of the hydrogen production system, whether to start the electrolyzer with the smallest rated power needs to be further judged by combining the current purity of the target gas.

it will be appreciated that when the hydrogen production power is greater than or equal to 85% of the first rated power, it is indicated that the hydrogen production system is not in a low load operating condition, and therefore, it is necessary to combine the integrated judgment of the rated powers of the other electrolytic tanks than the first electrolytic tank.

it will be appreciated that the second power rating may be one value or may be two or more values.

In practical application, according to the rated power of at least two electrolytic cells, the first rated power and the second rated power are continuously updated, and specified operation is executed until each electrolytic cell runs at full load.

When the power of the other electrolytic cells except the first electrolytic cell is not equal, the first rated power is updated to the minimum rated power of the other electrolytic cells, and the second rated power is updated to the rated power of the other electrolytic cells which is larger than the updated first rated power.

Example 1 the electrolyzer combination of the hydrogen production system may be 500Nm ³ /h，1000Nm ³ /h，1000Nm ³ /h，1000Nm ³ And/h, the first rated power at this time is 500Nm ³ And/h, a second rated power of 1000Nm ³ /h；

Example 2 the electrolyzer combination of the hydrogen production system may be 500Nm ³ /h，1000Nm ³ /h，2000Nm ³ /h，2000Nm ³ And/h, the first rated power at this time is 500Nm ³ And/h, a second rated power of 1000Nm ³ And/h, the updated first rated power is 1000Nm ³ And/h, the updated second rated power is 2000Nm ³ /h；

Example 3 the electrolyzer combination of the hydrogen production system may be 500Nm ³ /h，1000Nm ³ /h，2000Nm ³ /h，3000Nm ³ And/h, the first rated power at this time is 500Nm ³ And/h, a second rated power of 1000Nm ³ And/h, the first rated power after the first update is 1000Nm ³ And/h, the updated second rated power is 2000Nm ³ And/h, the first rated power after the second update is 2000Nm ³ And/h, the updated second rated power is 2000Nm ³ /h。

The first rated power and the second rated power, and the updated first rated power and the updated second rated power are judged in no sequence, and the judgment is directly carried out according to the rated power of the electrolytic cell in practice.

Further, in some embodiments, the first threshold is 30% of the first rated power, and controlling the first electrolytic cell to be opened or closed corresponding to the first rated power according to the hydrogen production power, the first threshold and the purity of the target gas includes:

it is understood that the first threshold value refers to the lowest work load of the first electrolytic tank corresponding to the minimum rated power, the hydrogen production power is more than 30% and less than 85% of the first rated power, and the load requirement of the electrolytic tank corresponding to the first rated power is met, so that the first electrolytic tank is controlled to start.

And when the hydrogen production power is smaller than or equal to a first threshold value and the purity of the target gas is smaller than a preset threshold value, controlling the hydrogen production system to stop.

The preset threshold is preset according to actual needs, and the preset threshold refers to the purity of the target gas, for example, the hydrogen in oxygen is more than 1.5%;

the hydrogen production power is lower than the lowest work load of the electrolytic tank with the smallest rated power, which means that the hydrogen production power provided by the current power supply system is very small, and the electrolytic tank with the small rated power needs to be controlled to work, however, in order to ensure the work efficiency of the hydrogen production system, whether the electrolytic tank with the smallest rated power is started needs to be further judged by combining the current purity of the target gas, if the purity of the target gas is higher than a preset threshold value, the current system cannot meet the production requirement, the whole hydrogen production system is controlled to stop, and when the purity of the target gas is lower than or equal to the preset threshold value, the current system can meet the production requirement under the lowest work load of the first electrolytic tank, and the first electrolytic tank is controlled to start to work.

Further, the second threshold is 30% of the second rated power, and according to the hydrogen production power, the second rated power, the second threshold and the preset load distribution ratio, the working state of the first electrolytic cell corresponding to the first rated power or the working state of the second electrolytic cell corresponding to the second rated power is controlled, including:

when the hydrogen production power is larger than a second threshold value and smaller than 85% of the second rated power, the first electrolytic tank is controlled to be started or closed according to the load distribution proportion, the second electrolytic tank is controlled to be started at the same time, and the actual working power of the first electrolytic tank and the second electrolytic tank is adjusted; the method comprises the steps of carrying out a first treatment on the surface of the

When the hydrogen production power is smaller than or equal to a second threshold value, the second electrolytic tank is controlled to be started or closed according to the load distribution proportion, the first electrolytic tank is controlled to be started at the same time, and the actual working power of the first electrolytic tank and the second electrolytic tank is adjusted.

When a value greater than the second rated power exists in the rated power of the electrolytic cell, the value is determined as the second rated power.

The load distribution ratio determines the actual load of each electrolytic cell, so that when the hydrogen production power is greater than the second threshold value and less than 85% of the second rated power, only the second electrolytic cell can be started, and the first electrolytic cell and the second electrolytic cell can be started at the same time, so that the load of the first electrolytic cell is transferred to the second electrolytic cell according to the load ratio (namely, the actual working power of the second electrolytic cell is increased, and the actual working power of the first electrolytic cell is reduced). Similarly, when the hydrogen production power is smaller than or equal to the second threshold value, only the first electrolytic tank can be started, and of course, the first electrolytic tank and the second electrolytic tank can also be started at the same time, and the load of the second electrolytic tank is transferred to the first electrolytic tank according to the load proportion (namely, the actual working power of the first electrolytic tank is increased, and the actual working power of the second electrolytic tank is reduced).

Further, in a preferred embodiment, step S23, controlling the working state of each electrolytic cell according to the hydrogen production power and the rated power of the at least two electrolytic cells, further includes:

acquiring the accumulated running time of each electrolytic tank;

It can be understood that the number of the electrolytic cells with the same rated power can be one, two or more than two, and the controller starts the electrolytic cell with the shortest accumulated running time each time, thereby being beneficial to improving the production efficiency.

In other embodiments, the operating state includes an actual flow of the electrolyzer, S23, controlling the operating state of each electrolyzer according to the hydrogen production power, the preset load distribution ratio, the current purity and the rated power, and further includes:

wherein the nominal flow of the electrolyzer is pre-adapted to the nominal power, e.g1000m ³ The rated flow of alkaline solution of the electrolytic tank is 80m ³ /h; the set flow rate is the working flow rate which accords with the current hydrogen production power and the target gas purity, and is determined according to the load distributed by each electrolytic tank, namely the actual working power, and the controller continuously updates the set flow rate according to the change of the hydrogen production power;

wherein, the historical flow refers to the flow of each electrolytic cell at any time before the current time;

Because the hydrogen production power fluctuates and changes, the set flow is changed, and the actual flow of the electrolytic tank is controlled according to the difference value of the historical flow and the set flow, thereby being beneficial to ensuring that the purity of the target is in a normal range.

Specifically, according to the hydrogen production power, the rated power of each electrolytic cell and the preset rated flow of each electrolytic cell, the set flow of each electrolytic cell is determined, and the specific formula is as follows:

In a preferred embodiment, after controlling and adjusting the actual flow rate of each electrolytic cell according to the historical flow rate and the set flow rate, the method further comprises:

It can be understood that the change of the flow of the alkaline electrolyte in the electrolytic tank can affect the purity of the target gas, so that after the actual flow of the electrolytic tank is adjusted, the actual flow of the electrolytic tank is adjusted according to the purity of the target gas, which is beneficial to ensuring the working efficiency of the hydrogen production system and ensuring that the purity of the target gas meets the requirements.

In other embodiments, as shown in fig. 4, in step S21, according to the hydrogen production power and the rated powers of at least two electrolytic tanks, determining a first electrolytic tank corresponding to the first rated power as a target electrolytic tank, and after controlling the start of the target electrolytic tank, further includes:

s31, acquiring the operation temperature of the target electrolytic tank and the current purity of the target gas;

s32, when the current purity of the target gas is larger than a preset threshold value, controlling to reduce the operating temperature of the target electrolytic tank.

It can be understood that when the hydrogen production system is operated under the low-load working condition, when the purity of the target gas is smaller than the preset threshold value (hydrogen in oxygen is more than 1.5%), the operation temperature of the electrolytic tank is reduced, the activity of newly generated gas of the electrolytic tank is reduced, the permeability of the gas is correspondingly reduced, and the purity of the target gas is protected and ensured to be in a normal range.

The method is characterized in that according to practical application, the temperature is reduced, and meanwhile, the heat preservation requirement of the hydrogen production system in low-load operation is met, and the hot start requirement of the system is met.

The following describes, by way of one specific example, the method of operation of the hydrogen production system of embodiments of the present application.

500Nm is adopted ³ /h，1000Nm ³ /h，2000Nm ³ /h，2000Nm ³ Four power electrolytic cell combinations/h, wherein the rated power corresponding to each electrolytic cell is PE ₁ 、PE ₂ 、PE ₃ 、PE ₃ At the time of low load of the new energy power supply system, one 500Nm is adopted ³ The cell/h is operated at 0.75KW (500 Nm) ³ The load of the electrolyzer at/h is about 2.5MW and 30% of the load), the minimum load requirement is met, qualified gas is produced, the system can also be ensured to rapidly respond to the power generation characteristic (hot start) of new energy, and the maximum power configuration of 32.5MW and the minimum power configuration of 0.75MW can be realized according to the configuration.

Acquiring actual hydrogen production power P according to the system load of the new energy power supply system, judging the hydrogen production power and the rated power of the electrolytic tank, and automatically selecting the electrolytic tank to operate;

as shown in figures 5 and 6 of the drawings,

(1) When P is more than or equal to 85 percent PE ₁ And 30% PE ₂ <P<85％PE ₂ At the time of direct start up 1000Nm ³ A/h (i.e., 2# in FIG. 1) electrolyzer;

(2) According to the load distribution of the control system to the electrolytic tank and the set flow F of the alkaline electrolyte of the electrolytic tank _Lye The actual flow of alkaline electrolyte of the corresponding electrolytic cell is matched. Wherein 1000Nm ³ The rated flow rate of alkali liquor of the/h electrolytic tank is 80m ³ And/h, setting the lowest alkali liquor flow to be 50%, namely setting the flow F=50% Fe+5Fe/7 (n-30%) (Fe is the rated flow and n is the ratio of hydrogen production power to rated power), wherein during the operation in the load range, the gas production of the electrolytic tank is reduced when the load is in a lower load, the heating value is correspondingly reduced, and the alkali liquor flow can be reduced. By changing the flow of the alkali liquor, the time of the alkali liquor in the separator is increased, the gas is ensured to be separated out for a sufficient time, and the purity of the gas is improved. In addition, by properly reducing the temperature of the alkaline solution, the activity of newly generated gas of the electrolytic tank is reduced, and the permeability of the gas is correspondingly reduced.

The method comprises the following steps: the controller acquires the historical flow F of the electrolytic tank branch in real time through a No. 2 flowmeter _Pv The method comprises the steps of carrying out a first treatment on the surface of the The controller sets the flow rate F by comparison _Lye And historical flow F _Pv Through PID control algorithm, an adjusting value is given, through electrical conversion, a 1# adjusting valve adjusting signal is given, an appropriate opening degree is given to the adjusting valve, the alkaline liquid flow is controlled to ensure that the gas purity is detected by sampling analysis of the electrolytic tank in the operation process of the electrolytic tank, and when a certain purity value is poor (for example, hydrogen in oxygen is more than 1.5%), the gas purity of the electrolytic tank is improved by reducing the alkaline liquid flow of the electrolytic tank through feedback of the purity. No matter what way is adopted to reduce the flow rate of the electrolyte of the water electrolysis hydrogen production system, the lower the flow rate of the electrolyte is, the more thoroughly the hydrogen is separated in the hydrogen separator, the more thoroughly the oxygen is separated in the oxygen separator, and the better the purity of the hydrogen and the oxygen is; therefore, in the reduction process, once the detected gas purity meets the preset requirement, the reduction process can be stopped in practical application, namely, the hydrogen purity can be detected to meet the corresponding requirement, and the hydrogen electrolysis hydrogen production system can output the hydrogen with the purity meeting the corresponding requirementTo avoid too low electrolyte flow. Too low an electrolyte flow rate may result in a cell outlet temperature less than the cell temperature linkage value.

The determination of the reduction of the electrolyte flow rate and the gas purity may be performed periodically, and the determination of whether the gas purity satisfies a preset requirement and whether the electrolyte flow rate falls to a preset flow rate lower limit is performed; after a certain period of time, one cycle is completed. The length of the period may depend on the particular application environment; the step length of each period may be the same or different, and is not particularly limited. Or, the judgment of the reduction of the flow rate of the electrolyte and the gas purity can be continuously performed without interruption, namely, the flow rate of the electrolyte is continuously reduced, and then, the judgment of whether the gas purity meets the preset requirement and whether the flow rate of the electrolyte is reduced to the lower limit of the preset flow rate is performed in real time.

(3) When 30% PE ₁ <P<85％PE ₁ Power transfer is performed to 1000Nm ³ The power of the/h electrolyzer was transferred to 500Nm ³ And (3) comparing the power of the system again according to the actual detected power at intervals of 1 minute, wherein the minimum running power of the system is as low as 0.75MW and the maximum running power of the system is 32.5MW. In the process of the load range operation, the purity is monitored in real time, and the alkali liquor flow is finely regulated by adopting the same method as the method (2).

(4) When P is more than or equal to 85 percent PE ₂ Power transfer is performed to 1000Nm ³ The power of the/h electrolyzer was transferred to 2000Nm ³ And (3) comparing again according to the actually detected power at intervals of 1 minute in the electrolyzer, regulating the flow of alkali liquor according to the purity of the target gas, and when P is less than 30% PE ₃ Power transfer to 1000Nm ³ And/h, simultaneously executing the step (2); and so on until all cells are operating at full capacity.

(5)P≤30％PE ₁ And when the hydrogen content in the oxygen is more than 1.5%, the machine is stopped directly.

In addition, each electrolytic cell corresponds to one alkali pump, and the No. 1 alkali pump provides 20-60m ³ /h (corresponding to 500 Nm) ³ An electrolyzer of/h), 2# alkaline pump provides 40-100m ³ /h (corresponding to 1000 Nm) ³ An electrolyzer of/h), 3# alkaline pump provides 80-200m ³ /h (corresponding to 2000 Nm) ³ An electrolyzer of/h), the 4# alkaline pump provides 80-200m ³ /h (corresponding to 2000 Nm) ³ An electrolysis cell of/h). The reflux flow is controlled through the first regulating valve, so that the flow of alkali liquor is accurately regulated, the purity of gas generated by the electrolytic tank is improved, and the damage to the alkali pump caused by a conventional pressure-holding regulation mode is avoided.

When the system enters a low-load operation condition, the activity of newly generated gas of the electrolytic tank is reduced by properly reducing the temperature of alkali liquor, and the permeability of the gas is correspondingly reduced. The reduced temperature is according to practical application, and the heat preservation requirement during the low-load operation of the system is met while the temperature is reduced, so that the purpose of hot start of the system is met.

In a third aspect, embodiments of the present application provide an operating apparatus for a hydrogen production system, comprising:

the acquisition module is used for acquiring hydrogen production power;

and the determining module is used for controlling the working state of each electrolytic cell according to the hydrogen production power and the rated powers of at least two electrolytic cells.

The principle and effect of the operation device of the present embodiment are the same as those of the operation method described above, and will not be described here again.

Referring now to FIG. 7, a schematic diagram of a computer system 600 suitable for use in implementing the terminal device of an embodiment of the present application is shown.

As shown in fig. 7, the computer system 600 includes a Central Processing Unit (CPU) 601, which can perform various appropriate actions and processes according to a program stored in a Read Only Memory (ROM) 602 or a program loaded from a storage section 608 into a Random Access Memory (RAM) 603. In the RAM 603, various programs and data required for the operation of the system 600 are also stored. The CPU 601, ROM 602, and RAM 603 are connected to each other through a bus 604. An input/output (I/O) interface 605 is also connected to bus 604.

The following components are connected to the I/O interface 605: an input portion 606 including a keyboard, mouse, etc.; an output portion 607 including a Cathode Ray Tube (CRT), a Liquid Crystal Display (LCD), and the like, a speaker, and the like; a storage section 608 including a hard disk and the like; and a communication section 609 including a network interface card such as a LAN card, a modem, or the like. The communication section 609 performs communication processing via a network such as the internet. The drive 610 is also connected to the I/O interface 505 as needed. Removable media 611 such as a magnetic disk, an optical disk, a magneto-optical disk, a semiconductor memory, or the like is installed as needed on drive 610 so that a computer program read therefrom is installed as needed into storage section 608.

In particular, according to embodiments of the present application, the process described above with reference to any of fig. 2-4 may be implemented as a computer software program. For example, embodiments of the present application include a computer program product comprising a computer program tangibly embodied on a machine-readable medium, the computer program comprising program code for performing the method of any of fig. 2-4. In such an embodiment, the computer program may be downloaded and installed from a network through the communication portion 609, and/or installed from the removable medium 611.

It should be noted that the computer readable medium shown in the present application may be a computer readable signal medium or a computer readable storage medium, or any combination of the two. The computer readable storage medium can be, for example, but not limited to, an electronic, magnetic, optical, electromagnetic, infrared, or semiconductor system, apparatus, or device, or a combination of any of the foregoing. More specific examples of the computer-readable storage medium may include, but are not limited to: an electrical connection having one or more wires, a portable computer diskette, a hard disk, a Random Access Memory (RAM), a read-only memory (ROM), an erasable programmable read-only memory (EPROM or flash memory), an optical fiber, a portable compact disc read-only memory (CD-ROM), an optical storage device, a magnetic storage device, or any suitable combination of the foregoing. In the context of this document, a computer readable storage medium may be any tangible medium that can contain, or store a program for use by or in connection with an instruction execution system, apparatus, or device. In the present application, however, a computer-readable signal medium may include a data signal propagated in baseband or as part of a carrier wave, with computer-readable program code embodied therein. Such a propagated data signal may take any of a variety of forms, including, but not limited to, electro-magnetic, optical, or any suitable combination of the foregoing. A computer readable signal medium may also be any computer readable medium that is not a computer readable storage medium and that can communicate, propagate, or transport a program for use by or in connection with an instruction execution system, apparatus, or device. Program code embodied on a computer readable medium may be transmitted using any appropriate medium, including but not limited to: wireless, wire, fiber optic cable, RF, etc., or any suitable combination of the foregoing.

The flowcharts and block diagrams in the figures illustrate the architecture, functionality, and operation of possible implementations of systems, methods and computer program products according to various embodiments of the present invention. In this regard, each block in the flowchart or block diagrams may represent a module, segment, or portion of code, which comprises one or more executable instructions for implementing the specified logical function(s). It should also be noted that, in some alternative implementations, the functions noted in the block may occur out of the order noted in the figures. For example, two blocks shown in succession may, in fact, be executed substantially concurrently, or the blocks may sometimes be executed in the reverse order, depending upon the functionality involved. It will also be noted that each block of the block diagrams and/or flowchart illustration, and combinations of blocks in the block diagrams and/or flowchart illustration, can be implemented by special purpose hardware-based systems which perform the specified functions or acts, or combinations of special purpose hardware and computer instructions.

The units or modules described in the embodiments of the present application may be implemented by software, or may be implemented by hardware. The described units or modules may also be provided in a processor, for example, as: a processor includes an acquisition module and a determination module. The names of these units or modules do not constitute a limitation on the unit or module itself in some cases, and for example, the determination module may also be described as "a module that controls the operation state of each electrolyzer in accordance with the hydrogen production power and the rated power of at least two electrolyzers".

As another aspect, the present application also provides a computer-readable storage medium, which may be a computer-readable storage medium contained in the foregoing apparatus in the foregoing embodiment; or may be a computer-readable storage medium, alone, that is not assembled into a device. The computer readable storage medium stores one or more programs for use by one or more processors in performing the methods of operating the hydrogen production system described herein.

It is to be understood that the above references to the terms "center", "longitudinal", "transverse", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc., are for convenience in describing the present invention and simplifying the description only, and do not indicate or imply that the apparatus or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus are not to be construed as limiting the present invention. Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include one or more such feature. In the description of the present invention, unless otherwise indicated, the meaning of "a plurality" is two or more.

The foregoing description is only of the preferred embodiments of the present application and is presented as a description of the principles of the technology being utilized. It will be appreciated by persons skilled in the art that the scope of the invention referred to in this application is not limited to the specific combinations of features described above, but it is intended to cover other embodiments in which any combination of features described above or equivalents thereof is possible without departing from the spirit of the invention. Such as the above-described features and technical features having similar functions (but not limited to) disclosed in the present application are replaced with each other.

Claims

1. A hydrogen production system, comprising: the system comprises a power supply system, a separator, a controller, at least two electrolytic tanks, at least two alkaline pumps and a return pipeline;

the power supply system is used for providing electric energy for the electrolytic tank;

the at least two electrolytic tanks are used for electrolyzing the input alkaline electrolyte to generate target gas, and inputting the target gas into the separator;

the at least two electrolytic tanks are arranged in parallel, and rated power of the at least two electrolytic tanks is sequentially recorded as PE from small to large _n-1 ，PE _n ，PE _n+1 ,., n is greater than or equal to 1, wherein PE _n-1 >PE _n 30% of PE _n >PE _n+1 And the rated power of at least two of the cells is different;

each alkaline pump is correspondingly arranged on a pipeline communicated with the inlet of each electrolytic cell, and is used for correspondingly inputting the alkaline electrolyte into each electrolytic cell;

the return line is connected in parallel between the inlet and the outlet of each alkaline pump and is used for regulating the flow rate of alkaline electrolyte entering each electrolytic tank;

the controller is used for acquiring the hydrogen production power provided by the power supply system and controlling the working state of each electrolytic cell according to the hydrogen production power and the rated power of each electrolytic cell.

2. The hydrogen production system of claim 1, wherein the return line is provided with a first regulating valve for regulating the return amount of alkaline electrolyte.

3. The hydrogen production system of claim 2, wherein said controller is further configured to obtain an actual flow rate of alkaline electrolyte in each of said electrolytic cells, and control an opening of said first regulator valve based on said actual flow rate and a preset rated flow rate of alkaline electrolyte in each of said electrolytic cells.

4. The hydrogen production system of claim 2, wherein the controller is further configured to obtain an actual purity of the target gas, and control the opening of the first regulator valve based on the actual purity and a preset threshold.

5. The hydrogen production system of any of claims 1-4, further comprising: the alkaline solution circulating pipeline is used for collecting alkaline electrolyte flowing out along with the target gas in at least two electrolytic tanks and conveying the collected alkaline electrolyte to each electrolytic tank respectively.

6. The hydrogen production system of claim 5 wherein a cooler is mounted on said lye circulation line, an inlet of said cooler being in communication with a liquid outlet of said separator for cooling a portion of alkaline electrolyte flowing outwardly with said target gas, an outlet of said cooler being in communication with a line delivering collected alkaline electrolyte to each of said cells.

7. The hydrogen production system of claim 5 wherein said separator comprises a hydrogen separator and an oxygen separator, said hydrogen separator inlet being in communication with each of said electrolyzer hydrogen outlets, respectively, said hydrogen separator lye outlet being in communication with each of said electrolyzer inlets through said lye circulation line, said oxygen separator inlet being in communication with each of said electrolyzer oxygen outlets, respectively, said oxygen separator lye outlet being in communication with each of said electrolyzer inlets through said lye circulation line.

8. The hydrogen production system of claim 7, wherein the number of hydrogen separators is a plurality and a plurality of the hydrogen separators are arranged in series or parallel, and/or the number of oxygen separators is a plurality and a plurality of the oxygen separators are arranged in series or parallel.

9. The hydrogen production system of claim 6, further comprising: a second regulating valve installed on a coolant inlet line of the cooler, the second regulating valve for regulating a flow rate of coolant entering the cooler;

the controller controls the opening of the second regulating valve according to the running temperature of each electrolytic tank so as to regulate the running temperature of each electrolytic tank to be 50-90 ℃.

10. The hydrogen production system of any of claims 1-4, further comprising a scrubbing apparatus having an inlet in communication with the separated gas outlet for purifying the target gas.

11. A method of operating a hydrogen production system as claimed in any one of claims 1 to 10, comprising the steps of:

obtaining hydrogen production power;

and controlling the working state of each electrolytic tank according to the hydrogen production power and the rated power of at least two electrolytic tanks.

12. The method of claim 11, wherein controlling each of the electrolyzer operating conditions based on the hydrogen production power and the rated power of the at least two electrolyzers comprises:

when the hydrogen production power is smaller than or equal to a preset threshold value, determining a first electrolytic cell corresponding to a first rated power as a target electrolytic cell according to the hydrogen production power and the rated powers of the at least two electrolytic cells, and controlling the starting of the target electrolytic cell; wherein the first rated power is the smallest rated power;

when the hydrogen production power is greater than a preset threshold value, acquiring the current purity of the target gas according to the first preset period;

13. The method of claim 12, wherein the operating conditions include opening or closing of each electrolyzer, and actual operating power of each electrolyzer, and controlling the operating conditions of each electrolyzer based on the hydrogen production power, a preset load distribution ratio, the current purity, and the rated power comprises:

when the hydrogen production power is less than 85% of the first rated power, controlling the first electrolytic tank corresponding to the first rated power to be opened or closed according to the hydrogen production power, a first threshold value and the purity of the target gas;

the following specified operations are performed, including:

when the hydrogen production power is greater than or equal to 85% of the first rated power, controlling the working state of a first electrolytic cell corresponding to the first rated power or a second electrolytic cell corresponding to the second rated power according to the hydrogen production power, the second rated power, a second threshold value and the preset load distribution proportion;

And updating the first rated power and the second rated power according to the rated power of the at least two electrolytic cells, and executing the specified operation until each electrolytic cell runs at full load.

14. The method of claim 13, wherein the first threshold is 30% of the first rated power, and controlling the opening or closing of the first electrolyzer corresponding to the first rated power based on the hydrogen production power, the first threshold, and the purity of the target gas comprises:

when the hydrogen production power is larger than the first threshold value, controlling the first electrolytic tank to start;

and when the hydrogen production power is smaller than or equal to the first threshold value and the purity of the target gas is larger than a preset threshold value, controlling the hydrogen production system to stop.

15. The method of claim 13, wherein the second threshold is 30% of the second rated power, and controlling the operating state of the first electrolytic cell corresponding to the first rated power or the second electrolytic cell corresponding to the second rated power according to the hydrogen production power, the second rated power, the second threshold, and the preset load distribution ratio comprises:

When the hydrogen production power is greater than the second threshold value and less than 85% of the second rated power, controlling the first electrolytic tank to start or stop according to the load distribution proportion, simultaneously controlling the second electrolytic tank to start, and adjusting the actual working power of the first electrolytic tank and the second electrolytic tank;

when the hydrogen production power is smaller than or equal to the second threshold value, the second electrolytic tank is controlled to be started or closed according to the load distribution proportion, the first electrolytic tank is controlled to be started at the same time, and the actual working power of the first electrolytic tank and the actual working power of the second electrolytic tank are adjusted.

16. The method of claim 12, wherein controlling each of the electrolyzer operating conditions based on the hydrogen production power and the rated power of the at least two electrolyzers further comprises:

acquiring the accumulated running time of each electrolytic tank;

and controlling the starting of the electrolytic cells with the shortest running time in the electrolytic cells with the same rated power.

17. The method of claim 12, wherein the operating conditions include an actual flow rate of the electrolyzer, and controlling the operating conditions of each of the electrolyzer based on the hydrogen production power, a preset load distribution ratio, the current purity, and the rated power comprises:

18. The method of claim 17, wherein the set flow rate for each cell is determined based on the hydrogen production power, the rated power for each cell, and a preset rated flow rate for each cell, in particular according to the formula:

19. The method of claim 17, further comprising, after controlling and adjusting the actual flow rate of each electrolytic cell based on the historical flow rate and the set flow rate:

and when the current purity of the target gas is smaller than a preset threshold value, controlling to reduce the actual flow of the electrolytic tank.

20. The method of claim 12, wherein after determining a first cell corresponding to a first rated power as a target cell based on the hydrogen production power and the rated powers of the at least two cells, controlling start-up of the target cell further comprises:

Acquiring the operating temperature of the target electrolytic tank and the current purity of target gas;

and controlling to reduce the operating temperature of the target electrolytic tank when the current purity of the target gas is smaller than a preset threshold value.