Stable supply system of clean energy hydrogen and control method thereof

Abstract

The present application relates to hydrogen production technology field, especially to a kind of clean energy hydrogen production stable supply system and control method thereof, stable supply system includes: raw material mixing unit, including to be mixed to methanol vapor and desalted water vapor to form mixed gas gas mixing chamber and the heat preservation chamber for the heat preservation of gas mixing chamber by the hydrogen gas mixed gas output from reaction chamber is set outside gas mixing chamber;Reaction hydrogen production unit, which is connected with the raw material mixing unit, is used to provide the chemical reaction conditions of the mixed gas to generate hydrogen gas and hydrogen gas mixed gas of carbon dioxide;Gas separation unit is used to separate the hydrogen gas mixed gas to output pure hydrogen gas;Detection unit is used to detect the internal gas pressure of gas mixing chamber, the gas pressure of the gas inlet of reaction chamber, the gas pressure of the gas outlet of reaction chamber and the vibration frequency of gas mixing chamber respectively;The present application improves the stability of hydrogen production.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of hydrogen production, in particular to a stable supply system for clean energy hydrogen production and a control method thereof. BACKGROUND

[0002] Traditional hydrogen production technologies such as fossil fuel hydrogen production produce a large amount of carbon dioxide, and water point hydrogen production has high energy consumption and is also more dependent on the stability of the power grid. If connected to new energy power supply, the stability of the power supply is insufficient, so methanol as a clean energy for hydrogen production has special advantages, but the process of methanol hydrogen production is complex, and the generated mixed gas is easy to interfere with the normal reaction process.

[0003] Chinese Patent Publication No. CN117658069A discloses a methanol hydrogen production system and a methanol hydrogen production process. The methanol hydrogen production system includes a vaporization unit, a reforming hydrogen production unit, a mixed gas separation unit, and a carbon sequestration agent regeneration unit. The vaporization unit is connected to the tube side of the heat exchanger of the reforming hydrogen production unit to input the steam of the methanol solution into the tube side of the heat exchanger to react with the methanol reforming catalyst. The tube side discharge end of the heat exchanger is connected to the shell side, which is filled with calcium oxide. The mixed gas of the reforming product enters the shell side of the heat exchanger, and the mixed gas reacts exothermically with calcium oxide. The released heat can exchange with the tube side of the heat exchanger to provide heat for the continuous reforming reaction, effectively reducing the energy consumption required for the reforming reaction. The shell side discharge end of the heat exchanger is connected to the mixed gas separation unit. Hydrogen and impurity gas are separated by the mixed gas separation unit. The impurity gas can be input from the mixed gas separation unit to the carbon sequestration agent regeneration unit as fuel to realize the recycling of the carbon sequestration agent. It can be seen that the methanol hydrogen production system and the methanol hydrogen production process have the problem that the high-temperature mixed gas of hydrogen and carbon dioxide causes the circulation pipeline to vibrate, so that when the vibration frequency is high, the original methanol vapor and desalted water vapor in the gas mixing chamber will cause the micro-droplets in the mixed gas to gather, causing the mixed gas containing droplets to instantaneously vaporize in the high-temperature environment when entering the reaction chamber, resulting in an instantaneous increase in gas pressure, and thus the impact on the catalyst becomes larger. SUMMARY

[0004] Therefore, the present application provides a stable supply system for clean energy hydrogen production and a control method thereof to overcome the problem in the prior art that the high-temperature mixed gas of hydrogen and carbon dioxide causes the circulation pipeline to vibrate, so that when the vibration frequency is high, the original methanol vapor and desalted water vapor in the gas mixing chamber will cause the micro-droplets in the mixed gas to gather, causing the mixed gas containing droplets to instantaneously vaporize in the high-temperature environment when entering the reaction chamber, resulting in an instantaneous increase in gas pressure, and thus the impact on the catalyst becomes larger.

[0005] To achieve the above objectives, the present invention provides a stable supply system for clean energy hydrogen production, comprising:

[0006] The raw material mixing unit includes a gas mixing chamber for mixing methanol vapor and demineralized water vapor to form a mixed gas, and an insulation chamber located outside the gas mixing chamber for heat preservation of the gas mixing chamber by hydrogen mixed gas output through the reaction chamber.

[0007] A reaction hydrogen production unit, connected to the raw material mixing unit, is used to provide chemical reaction conditions for the mixed gas to generate a hydrogen-carbon dioxide mixture, including a reaction chamber, a catalytic reaction bed disposed inside the reaction chamber to provide a catalyst reaction position, and a heating component for heating the mixed gas inside the reaction chamber.

[0008] A gas separation unit, which is connected to the raw material mixing unit, is used to separate the hydrogen gas mixture to output pure hydrogen.

[0009] The detection unit is connected to the raw material mixing unit and the reaction hydrogen production unit respectively, and is used to detect the internal gas pressure of the gas mixing chamber, the gas pressure at the inlet of the reaction chamber, the gas pressure at the outlet of the reaction chamber, and the vibration frequency of the gas mixing chamber respectively.

[0010] A control unit, connected to the raw material mixing unit, the reaction hydrogen production unit, the gas separation unit, and the detection unit, is used to determine the gas flow rate entering the insulation chamber based on the decrease in internal gas pressure and vibration frequency of the gas mixing chamber; to determine the gas inlet velocity of the reaction chamber based on the switching frequency of droplet aggregation state; and to determine the trigger frequency of the breathing mode of the reaction chamber based on the pressure difference between the inlet and outlet of the reaction chamber after operating at the gas inlet velocity of the reaction chamber.

[0011] The breathing method of the reaction chamber involves simultaneously adjusting the inlet temperature and the air intake speed of the reaction chamber within a preset time period.

[0012] Furthermore, the detection unit includes:

[0013] A first pressure sensor is disposed on the inner wall of the gas mixing chamber to detect the internal pressure of the gas mixing chamber;

[0014] The second pressure sensor is installed in the air inlet pipe of the reaction chamber to detect the air pressure at the air inlet of the reaction chamber.

[0015] The third pressure sensor is installed in the gas outlet pipe of the reaction chamber to detect the gas pressure at the gas outlet of the reaction chamber.

[0016] A vibration sensor, connected to the gas mixing chamber, is used to detect the vibration frequency of the gas mixing chamber.

[0017] Further, the control unit is connected with the first air pressure sensor and the vibration sensor respectively, to determine that the liquid droplet aggregation state is not qualified according to that the internal air pressure reduction is greater than a preset air pressure reduction, and the vibration frequency of the gas mixing chamber is greater than a preset vibration frequency, and reduce the gas flow into the holding chamber.

[0018] Further, the gas flow into the holding chamber is in a negative correlation with the internal air pressure reduction.

[0019] Further, the control unit determines that the impact risk of the mixed gas on the catalyst is not qualified according to that the switching frequency of the aggregation state is greater than a preset switching frequency, and reduces the gas inlet speed of the reaction chamber, wherein,

[0020] The gas inlet speed of the reaction chamber is in a negative correlation with the switching frequency of the aggregation state.

[0021] Further, the switching frequency of the aggregation state is the number of times of triggering that the liquid droplet aggregation state is not qualified in a monitoring period and the length of the monitoring period.

[0022] Further, the control unit determines that the corrosion degree of the catalytic reaction bed is not qualified according to that the inlet and outlet pressure difference of the reaction chamber is less than a preset pressure difference, and increases the triggering frequency of the breathing mode of the reaction chamber.

[0023] Further, the inlet and outlet pressure difference of the reaction chamber is the difference between the air pressure of the gas inlet of the reaction chamber and the air pressure of the gas outlet of the reaction chamber.

[0024] Further, the triggering frequency of the coefficient mode of the reaction chamber is in a negative correlation with the inlet and outlet pressure difference of the reaction chamber.

[0025] The application also provides a control method of a stable supply system of clean energy hydrogen production, comprising:

[0026] Respectively acquire the internal air pressure of the gas mixing chamber and the vibration frequency of the gas mixing chamber;

[0027] Determine the liquid droplet aggregation state according to the internal air pressure reduction and the vibration frequency, to determine the gas flow into the holding chamber;

[0028] Collect the switching frequency of the liquid droplet aggregation state;

[0029] Determine the gas inlet speed of the reaction chamber according to the switching frequency;

[0030] Acquire the air pressure of the gas inlet of the reaction chamber and the air pressure of the gas outlet of the reaction chamber after the reaction chamber is operated according to the gas inlet speed of the reaction chamber;

[0031] The inlet and outlet pressure difference of the reaction chamber is calculated according to the gas pressure of the gas inlet of the reaction chamber and the gas pressure of the gas outlet of the reaction chamber.

[0032] The triggering frequency of the breathing mode of the reaction chamber is determined according to the inlet and outlet pressure difference of the reaction chamber.

[0033] Compared with the prior art, the beneficial effects of the present application are that the present application determines the liquid droplet aggregation state of the mixed gas according to the decrease amount of the internal gas pressure and the vibration frequency of the gas mixing chamber, and reduces the gas flow entering the heat preservation chamber when the liquid droplet aggregation state does not meet the requirements, thereby reducing the fact that when there is a trace amount or a small amount of liquid droplets in the gas mixing chamber, the high-temperature mixed gas of hydrogen and carbon dioxide output by the reaction chamber vibrates the circulation pipeline during the process of being transported to the gas mixing chamber through the circulation pipeline, so that when the vibration frequency is high, the trace liquid droplets in the mixed gas of methanol vapor and desalted water vapor in the gas mixing chamber will aggregate, so that the mixed gas entering the reaction chamber contains liquid droplets, the liquid droplets vaporize instantaneously in the high-temperature environment in the reaction chamber, thereby causing an instantaneous increase in gas pressure, and the impact of the entering mixed gas on the catalyst becomes larger, therefore, by reducing the gas flow of the mixed gas of hydrogen and carbon dioxide entering the heat preservation chamber, the aggregation degree of the liquid droplets is reduced, thereby improving the impact effect on the catalyst, and the stability and completeness of the hydrogen production reaction are improved.

[0034] Further, the present application reduces the gas inlet speed of the reaction chamber according to the switching frequency of the aggregation state, and when the switching frequency between the state that the liquid droplet aggregation state does not meet the requirements and the state that the liquid droplet aggregation state meets the requirements exceeds a certain range, the impact on the catalyst will become serious, because the greater the switching frequency, the different the movement ability and impact strength of the mixed gas input into the reaction chamber each time, and if they are different, the structure of the catalyst will be subjected to different intensity impacts, thereby weakening the structural strength, so that the catalyst is more likely to break or the risk of breaking increases, thereby increasing the amount of the catalyst converted into a powder form, thereby making the reaction process of the methanol mixed gas incomplete, thereby affecting the amount of hydrogen production, by reducing the gas inlet speed of the reaction chamber, the impact strength is reduced, thereby reducing the influence of the impact on the catalyst on the integrity of the catalyst, and improving the stability of hydrogen production.

[0035] Further, the present application determines the triggering frequency of the breathing mode of the reaction chamber according to the pressure difference between the inlet and outlet of the reaction chamber after the reaction chamber is operated at a certain gas inlet speed, so as to reduce the corrosion of trace chlorine ions to the catalytic reaction bed, for example, the reaction of the chlorine ions with the catalyst carrier aluminum oxide to generate volatile aluminum chloride, so that the generated aluminum chloride migrates and re-deposits in the bed, thereby destroying the pore structure of the catalytic reaction bed and making the structural strength poor, so that the contact integrity of the mixed gas and the catalyst is reduced, and thus by increasing the inlet temperature of the reaction chamber and reducing the gas inlet speed of the reaction chamber, the chlorine ions and other toxic substances adsorbed on the catalyst can be taken out of the reaction chamber at a higher temperature and a lower flow rate, and the reaction completeness of the catalyst is improved through deep breathing adjustment of the catalyst. BRIEF DESCRIPTION OF DRAWINGS

[0036] Figure 1 The overall structure block diagram of the stable supply system for clean energy hydrogen production of the embodiment of the present application;

[0037] Figure 2 The structure block diagram of the raw material mixing unit of the stable supply system for clean energy hydrogen production of the embodiment of the present application

[0038] Figure 3 The overall structure schematic diagram of the stable supply system for clean energy hydrogen production of the embodiment of the present application;

[0039] Figure 4 The overall flowchart of the control method of the stable supply system for clean energy hydrogen production of the embodiment of the present application;

[0040] The reference signs are explained as follows: 1-hydrogen PSA device, 2-circulation pipeline, 3-third gas pressure sensor, 4-vibration sensor, 5-gas inlet valve, 6-heat preservation chamber, 7-first conveying pipeline, 8-second conveying pipeline, 9-first gas pressure sensor, 10-gas mixing chamber, 11-gas outlet pipeline, 12-conducting oil heating furnace, 13-conveying pump, 14-first gas outlet valve, 15-heat exchange cavity, 16-second gas outlet valve, 17-water cooler, 18-gas inlet pipeline, 19-second gas pressure sensor. DETAILED DESCRIPTION

[0041] In order to make the purpose and advantages of the present application more clear and explicit, the present application is further described below in combination with embodiments; it should be understood that the specific embodiments described herein are only used to explain the present application, and are not used to limit the present application.

[0042] The preferred embodiments of the present application are described below with reference to the accompanying drawings. Those skilled in the art should understand that these embodiments are only used to explain the technical principles of the present application, and are not used to limit the protection scope of the present application.

[0043] It should be noted that in the description of the present application, the terms "upper", "lower", "left", "right", "inner", "outer" and the like indicate the direction or positional relationship of the terms based on the direction or positional relationship shown in the drawings, which is only for the convenience of description, and does not indicate or imply that the device or element must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as a limitation on the present application.

[0044] In addition, it should be noted that in the description of the present application, unless otherwise explicitly specified and limited, the terms "mounting", "connecting", "connecting" should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or integrally connected; it can be mechanically connected, or it can be electrically connected; it can be directly connected, or it can be indirectly connected through an intermediate medium, and it can be the communication inside two elements. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances.

[0045] Please refer to Figure 1 and Figure 2 The overall structure block diagram of the stable supply system for hydrogen production by clean energy, the structure block diagram of the raw material mixing unit, the overall structure diagram and the overall flow chart of the control method of the stable supply system for hydrogen production by clean energy are shown in the drawings. The stable supply system for hydrogen production by clean energy of the present application comprises:

[0046] The raw material mixing unit comprises a gas mixing chamber 10 for mixing methanol vapor and desalted water vapor to form a mixed gas, and a heat preservation chamber 6 arranged outside the gas mixing chamber 10 and outputting the hydrogen mixed gas from the reaction chamber to heat the gas mixing chamber 10;

[0047] The reaction hydrogen production unit is connected with the raw material mixing unit, and is used to provide a chemical reaction condition for the mixed gas to generate hydrogen mixed gas of hydrogen and carbon dioxide, and comprises a reaction chamber 20, a catalytic reaction bed arranged inside the reaction chamber to provide a catalyst reaction position, and a heating assembly for heating the mixed gas inside the reaction chamber;

[0048] The gas separation unit is connected with the raw material mixing unit, and is used to separate the hydrogen mixed gas to output pure hydrogen;

[0049] The detection unit is connected with the raw material mixing unit and the reaction hydrogen production unit respectively, and is used to detect the internal gas pressure of the gas mixing chamber 10, the gas pressure of the gas inlet of the reaction chamber, the gas pressure of the gas outlet of the reaction chamber and the vibration frequency of the gas mixing chamber 10 respectively;

[0050] a control unit connected to the raw material mixing unit, the reaction hydrogen production unit, the gas separation unit, and the detection unit, respectively, to determine the gas flow into the holding chamber 6 according to the decrease in the internal gas pressure of the gas mixing chamber 10 and the vibration frequency, to determine the gas inlet speed of the reaction chamber according to the switching frequency of the liquid droplet aggregation state, and to determine the triggering frequency of the breathing mode of the reaction chamber according to the pressure difference between the inlet and outlet of the reaction chamber after the reaction chamber is operated at the gas inlet speed,

[0051] The breathing mode of the reaction chamber is to adjust the inlet temperature of the reaction chamber and the gas inlet speed of the reaction chamber simultaneously within a preset time period.

[0052] Specifically, the adjustment of the inlet temperature of the reaction chamber is achieved by adjusting the heating temperature of the device for heating methanol and the device for heating desalted water; the adjustment of the gas inlet speed of the reaction chamber is achieved by changing the opening size of the gas inlet valve.

[0053] Specifically, in the breathing mode of the reaction chamber, the adjustment of the inlet temperature of the reaction chamber is an increase adjustment, the adjustment of the gas inlet speed of the reaction chamber is a decrease adjustment, the preferred embodiment of the duration of the preset time period is 2 hours, the optional range of the increase amplitude of the inlet temperature of the reaction chamber is [6℃, 12℃], and the preferred embodiment of the increase amplitude of the inlet temperature of the reaction chamber is 9℃; the optional range of the decrease amplitude of the gas inlet speed of the reaction chamber is [20%, 40%], and the preferred embodiment of the decrease amplitude of the gas inlet speed of the reaction chamber is 30%.

[0054] Those skilled in the art can understand that those skilled in the art can adaptively adjust the adjustment amplitudes of the inlet temperature of the reaction chamber and the gas inlet speed of the reaction chamber according to actual conditions, which will not be described here.

[0055] Specifically, when the breathing mode of the reaction chamber is triggered, the decrease amplitude of the gas inlet speed of the reaction chamber is calculated in percentage, which means that the designed gas inlet speed of the reaction chamber is decreased by a corresponding proportion.

[0056] Specifically, the gas separation unit includes a water cooler 17 and a hydrogen PSA pressure swing adsorption device 1.

[0057] Specifically, the heating assembly includes:

[0058] A heat exchange cavity 15 is arranged inside the reaction chamber to transfer heat to the inside of the reaction chamber.

[0059] A heat conducting oil heating furnace 12 is connected to the heat exchange cavity 15 through a delivery pump 13 to deliver heated heat conducting oil into the heat exchange cavity 15.

[0060] Specifically, the raw material mixing unit further includes:

[0061] a first conveying pipe 7 connected with the gas mixing chamber 10 for conveying methanol vapor to the gas mixing chamber 10;

[0062] a second conveying pipe 8 connected with the gas mixing chamber 10 through the first conveying pipe 7 for conveying desalted water vapor to the gas mixing chamber 10.

[0063] Specifically, the gas mixing chamber 10 and the reaction chamber are further provided with an inlet valve 5 for controlling the feed air speed.

[0064] Specifically, the reaction hydrogen production unit further comprises:

[0065] an outlet pipe 11 connected with the reaction chamber for conveying part of the hydrogen mixed gas outputted by the reaction chamber to the heat preservation chamber 6;

[0066] a first outlet valve 14 arranged on the outlet pipe 11 for controlling the gas flow entering the heat preservation chamber 6;

[0067] a second outlet valve 16 arranged between the reaction chamber and a water cooler 17 for controlling the flow of hydrogen mixed gas entering the water cooler 17.

[0068] Specifically, the heat preservation chamber 6 and the water cooler 17 are further provided with a circulating pipe 2 for conveying the hydrogen mixed gas after passing through the heat preservation chamber 6 to the water cooler 17.

[0069] Specifically, the detection unit comprises:

[0070] a first air pressure sensor 9 arranged on the inner wall of the gas mixing chamber 10 for detecting the internal air pressure of the gas mixing chamber 10;

[0071] a second air pressure sensor 19 arranged in the inlet pipe 18 of the reaction chamber for detecting the air pressure of the inlet of the reaction chamber;

[0072] a third air pressure sensor 3 arranged in the outlet pipe 11 of the reaction chamber for detecting the air pressure of the outlet of the reaction chamber;

[0073] a vibration sensor 4 connected with the gas mixing chamber 10 for detecting the vibration frequency of the gas mixing chamber 10.

[0074] Specifically, the control unit is connected with the first air pressure sensor 9 and the vibration sensor 4 respectively, so as to determine that the liquid droplet aggregation state of the mixed gas does not meet the requirements and reduce the gas flow entering the heat preservation chamber 6 when the reduction of the internal air pressure is greater than a preset air pressure reduction and the vibration frequency of the gas mixing chamber 10 is greater than a preset vibration frequency.

[0075] Specifically, the gas flow into the holding chamber 6 is negatively correlated with the decrease of the internal pressure.

[0076] Optionally, when the internal pressure of the gas mixing chamber 10 is 0.1 MPa, the optional range of the preset pressure decrease is [50 Pa, 100 Pa], and the preferred embodiment of the preset pressure decrease is 80 Pa.

[0077] Optionally, when the rotating speed of the methanol feeding pump is 800 r / min, the optional range of the preset vibration frequency is [80 Hz, 100 Hz], and the preferred embodiment of the preset vibration frequency is 90 Hz.

[0078] In the implementation, when the decrease of the internal pressure exceeds the value of the preset pressure decrease by 20 Pa or less, the gas flow into the holding chamber 6 is reduced to 95% of the current gas flow into the holding chamber 6; when the decrease of the internal pressure exceeds the value of the preset pressure decrease by more than 20 Pa, the current gas flow into the holding chamber 6 is reduced by 1 m³ / h for each 1 Pa of excess, in a possible embodiment, the current gas flow into the holding chamber 6 is 150 m³ / h, the decrease of the internal pressure is 110 Pa, and then the reduced gas flow into the holding chamber 6 is 150 m³ / h x 95% - (110 Pa - 80 Pa - 20 Pa) / 1 Pa x 1 m³ / h = 132.5 m³ / h.

[0079] In the implementation, the present application determines the liquid droplet aggregation state of the mixed gas according to the decrease of the internal pressure and the vibration frequency of the gas mixing chamber 10, and reduces the gas flow into the holding chamber 6 when the liquid droplet aggregation state does not meet the requirements, thereby reducing the vibration of the circulating pipeline caused by the high-temperature mixed gas of hydrogen and carbon dioxide output from the reaction chamber when there are trace or small amounts of liquid droplets in the gas mixing chamber 10, and thereby reducing the aggregation of the trace liquid droplets in the mixed gas of methanol vapor and desalted water vapor in the gas mixing chamber 10 when the vibration frequency is high, so that the mixed gas entering the reaction chamber contains liquid droplets, the liquid droplets instantaneously vaporize in the high-temperature environment of the reaction chamber, causing an instantaneous increase in the gas pressure, and the impact of the entering mixed gas on the catalyst is increased, therefore, by reducing the gas flow of the mixed gas of hydrogen and carbon dioxide into the holding chamber 6, the aggregation degree of the liquid droplets is reduced, the impact on the catalyst is improved, and the stability and completeness of the hydrogen production reaction are improved.

[0080] Specifically, the control unit determines that the risk of the mixed gas impacting the catalyst does not meet the requirement according to the switching frequency of the aggregation state being greater than a preset switching frequency, and reduces the intake air speed of the reaction chamber, wherein,

[0081] The intake air speed of the reaction chamber is in a negative correlation with the switching frequency of the aggregation state.

[0082] Optionally, the optional range of the preset switching frequency is [2 times / hour, 4 times / hour], and the preferred embodiment of the preset switching frequency is 3 times / hour.

[0083] In implementation, under the production capacity of 5Nm³ / h, when the switching frequency of the aggregation state exceeds the value of the preset switching frequency within 2 times / hour, the intake air speed of the reaction chamber is reduced to 0.9 times of the current intake air speed of the reaction chamber; when the switching frequency of the aggregation state exceeds the value of the preset switching frequency by more than 2 times / hour, the current intake air speed of the reaction chamber is reduced by 0.1m³ / h for each excess of 1 time / hour. In a possible embodiment, the switching frequency of the aggregation state is 6 times / hour, and the current intake air speed of the reaction chamber is 8.2m³ / h, so the reduced intake air speed of the reaction chamber is 8.2m³ / h*0.9-(6 times / hour-3 times / hour) / 1 time / hour*0.1m³ / h=7.08m³ / h.

[0084] In implementation, the application reduces the intake air speed of the reaction chamber according to the switching frequency of the aggregation state. When the switching frequency exceeds a certain range, the impact on the catalyst becomes serious. The reason is that the movement ability and impact strength of the mixed gas input into the reaction chamber are different each time when the switching frequency is greater. The different impact strengths weaken the structure of the catalyst, which increases the risk of the catalyst breaking and the amount of the catalyst converted into powder, and thus affects the reaction process of the methanol mixed gas, which affects the amount of hydrogen produced. By reducing the intake air speed of the reaction chamber, the impact strength is reduced, which reduces the influence of the impact on the catalyst on the integrity of the catalyst and improves the stability of hydrogen production.

[0085] Specifically, the switching frequency of the aggregation state is the number of times of triggering the liquid droplet aggregation state not meeting the requirement within the monitoring period and the length of the monitoring period.

[0086] Specifically, the control unit determines that the corrosion degree of the catalyst reaction bed does not meet the requirement according to the pressure difference between the inlet and outlet of the reaction chamber being less than a preset pressure difference, and increases the triggering frequency of the breathing mode of the reaction chamber.

[0087] Specifically, the pressure difference between the inlet and outlet of the reaction chamber is the difference between the air pressure at the inlet of the reaction chamber and the air pressure at the outlet of the reaction chamber.

[0088] Specifically, the triggering frequency of the breathing mode in the reaction chamber is negatively correlated with the pressure difference between the inlet and outlet of the reaction chamber.

[0089] Optionally, the preset pressure difference can be selected within the range of [0.05MPa, 0.07MPa], and the preferred embodiment of the preset pressure difference is 0.06MPa.

[0090] In implementation, when the difference between the preset pressure difference and the inlet / outlet pressure difference of the reaction chamber is within 0.01 MPa, the trigger frequency of the breathing mode in the reaction chamber is increased to 1.5 times the current trigger frequency. When the difference between the preset pressure difference and the inlet / outlet pressure difference of the reaction chamber exceeds 0.01 MPa, the trigger frequency of the breathing mode in the reaction chamber is increased by 1 time / month for every 0.001 MPa exceeding the current value. In one embodiment, the inlet / outlet pressure difference of the reaction chamber is 0.045 MPa, and the current trigger frequency of the breathing mode in the reaction chamber is 8 times / h. Therefore, the increased trigger frequency of the breathing mode in the reaction chamber is 4 times / month × 1.5 + (0.06 MPa - 0.045 MPa - 0.01 MPa) / 0.001 MPa × 1 time / month = 11 times / month.

[0091] In practice, this invention determines the trigger frequency of the reaction chamber's breathing mode by adjusting the inlet and outlet pressure difference of the reaction chamber after it operates according to the inlet gas velocity. This reduces the corrosion of the catalytic reaction bed by trace amounts of chloride ions, such as the reaction with the catalyst support alumina to generate volatile aluminum chloride. The generated aluminum chloride migrates and redeposits within the bed, thereby damaging the pore structure of the catalytic reaction bed and weakening its structural strength. Consequently, the integrity of the contact between the mixed gas and the catalyst decreases. Therefore, by increasing the inlet temperature of the reaction chamber and decreasing the inlet gas velocity, toxic substances such as chloride ions adsorbed on the catalyst can be carried out of the reaction chamber at a higher temperature and lower flow rate. By adjusting the deep breathing of the catalyst, the completeness of the catalyst's reaction is improved.

[0092] This invention also provides a method for controlling a stable supply system for clean energy hydrogen production, comprising:

[0093] The internal air pressure and vibration frequency of the gas mixing chamber 10 are obtained respectively.

[0094] The droplet aggregation state is determined based on the decrease in internal air pressure and the vibration frequency, so as to determine the gas flow rate entering the insulation chamber 6;

[0095] The switching frequency of the droplet aggregation state is collected;

[0096] determining the intake velocity of the reaction chamber according to the switching frequency;

[0097] obtaining the air pressure at the intake port of the reaction chamber and the air pressure at the outlet port of the reaction chamber after the reaction chamber is operated according to the intake velocity of the reaction chamber;

[0098] calculating the pressure difference between the inlet and outlet of the reaction chamber according to the air pressure at the intake port of the reaction chamber and the air pressure at the outlet port of the reaction chamber;

[0099] determining the triggering frequency of the breathing mode of the reaction chamber according to the pressure difference between the inlet and outlet of the reaction chamber.

[0100] So far, the technical solutions of the present application have been described in combination with the preferred embodiments shown in the drawings, but it is easy for those skilled in the art to understand that the protection scope of the present application is obviously not limited to these specific embodiments. Those skilled in the art can make equivalent changes or replacements to the related technical features without departing from the principles of the present application, and the technical solutions after these changes or replacements will all fall within the protection scope of the present application.

Claims

1. A stable supply system of clean energy hydrogen production, characterized by, The application relates to a hydrogen production device, comprising: a raw material mixing unit, comprising a gas mixing chamber for mixing methanol vapor and desalted water vapor to form a mixed gas, and a heat preservation chamber arranged outside the gas mixing chamber and outputting a hydrogen mixed gas through a reaction chamber to heat preserve the gas mixing chamber; a reaction hydrogen production unit connected with the raw material mixing unit, for providing a chemical reaction condition of the mixed gas to produce hydrogen and carbon dioxide, comprising a reaction chamber, a catalytic reaction bed arranged inside the reaction chamber to provide a catalytic reaction position, and a heating assembly for heating the mixed gas inside the reaction chamber; a gas separation unit connected with the raw material mixing unit, for separating the hydrogen mixed gas to output pure hydrogen; a detection unit connected with the raw material mixing unit and the reaction hydrogen production unit respectively, for detecting an internal gas pressure of the gas mixing chamber, a gas pressure of an air inlet of the reaction chamber, a gas pressure of an air outlet of the reaction chamber, and a vibration frequency of the gas mixing chamber respectively; a control unit connected with the raw material mixing unit, the reaction hydrogen production unit, the gas separation unit and the detection unit respectively, for determining a gas flow entering the heat preservation chamber according to a reduction amount of the internal gas pressure and the vibration frequency of the gas mixing chamber, determining an air inlet speed of the reaction chamber according to a switching frequency of a liquid drop aggregation state, and determining a triggering frequency of a breathing mode of the reaction chamber according to a pressure difference between the air inlet and the air outlet of the reaction chamber after the reaction chamber is operated at the air inlet speed, wherein the breathing mode of the reaction chamber is to simultaneously adjust the inlet temperature of the reaction chamber and the air inlet speed of the reaction chamber for a preset time period.

2. The stable supply system of clean energy hydrogen production according to claim 1, characterized in that, The detection unit comprises: a first gas pressure sensor arranged on an inner wall of the gas mixing chamber, for detecting the internal gas pressure of the gas mixing chamber; a second gas pressure sensor arranged in an air inlet pipeline of the reaction chamber, for detecting the gas pressure of the air inlet of the reaction chamber; a third gas pressure sensor arranged in an air outlet pipeline of the reaction chamber, for detecting the gas pressure of the air outlet of the reaction chamber; a vibration sensor connected with the gas mixing chamber, for detecting the vibration frequency of the gas mixing chamber.

3. The stable supply system of clean energy hydrogen production according to claim 2, characterized in that, The control unit is connected with the first gas pressure sensor and the vibration sensor respectively, for determining that the liquid drop aggregation state of the mixed gas does not meet the requirement when the reduction amount of the internal gas pressure is greater than a preset gas pressure reduction amount, and the vibration frequency of the gas mixing chamber is greater than a preset vibration frequency, and reducing the gas flow entering the heat preservation chamber.

4. The stable supply system of clean energy hydrogen production according to claim 3, characterized in that, The gas flow entering the heat preservation chamber is in a negative correlation with the reduction amount of the internal gas pressure.

5. The stable supply system of clean energy hydrogen production according to claim 4, characterized in that, The control unit determines that the impact risk of the mixed gas on the catalyst does not meet the requirement when the switching frequency of the aggregation state is greater than a preset switching frequency, and reduces the air inlet speed of the reaction chamber, wherein the air inlet speed of the reaction chamber is in a negative correlation with the switching frequency of the aggregation state. The switching frequency of the aggregation state is a number of times of triggering that the liquid drop aggregation state does not meet the requirement in a monitoring period and a length of the monitoring period.

6. The stable supply system of clean energy hydrogen production according to claim 5, characterized in that, ​ 7. The stable supply system of clean energy hydrogen production according to claim 6, characterized in that, The control unit determines that the corrosion degree of the catalytic reaction bed does not meet the requirement according to the fact that the inlet-outlet pressure difference of the reaction chamber is less than a preset pressure difference, and increases the triggering frequency of the breathing mode of the reaction chamber.

8. The stable supply system of clean energy hydrogen production according to claim 7, characterized in that, The inlet-outlet pressure difference of the reaction chamber is the difference between the gas pressure of the gas inlet of the reaction chamber and the gas pressure of the gas outlet of the reaction chamber.

9. The stable supply system of clean energy hydrogen production according to claim 8, characterized in that, The triggering frequency of the coefficient mode of the reaction chamber is in a negative correlation with the inlet-outlet pressure difference of the reaction chamber.

10. A control method applied to the stable supply system of hydrogen produced from clean energy according to any one of claims 1-9, characterized in that, The method comprises the following steps: respectively acquiring the internal gas pressure of the gas mixing chamber and the vibration frequency of the gas mixing chamber; determining the liquid drop aggregation state according to the decrease of the internal gas pressure and the vibration frequency, so as to determine the gas flow rate into the heat preservation chamber; acquiring the switching frequency of the liquid drop aggregation state; determining the gas inlet speed of the reaction chamber according to the switching frequency; acquiring the gas pressure of the gas inlet of the reaction chamber and the gas pressure of the gas outlet of the reaction chamber after the reaction chamber is operated according to the gas inlet speed of the reaction chamber; calculating the inlet-outlet pressure difference of the reaction chamber according to the gas pressure of the gas inlet of the reaction chamber and the gas pressure of the gas outlet of the reaction chamber; determining the triggering frequency of the breathing mode of the reaction chamber according to the inlet-outlet pressure difference of the reaction chamber.

Images