CN116216634A - Magnesium hydride hydrolysis hydrogen production system and control method thereof - Google Patents
Magnesium hydride hydrolysis hydrogen production system and control method thereof Download PDFInfo
- Publication number
- CN116216634A CN116216634A CN202211735262.3A CN202211735262A CN116216634A CN 116216634 A CN116216634 A CN 116216634A CN 202211735262 A CN202211735262 A CN 202211735262A CN 116216634 A CN116216634 A CN 116216634A
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- reaction
- magnesium hydride
- weak acid
- controller
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000001257 hydrogen Substances 0.000 title claims abstract description 134
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 134
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 124
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 title claims abstract description 40
- 229910012375 magnesium hydride Inorganic materials 0.000 title claims abstract description 40
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 32
- 238000006460 hydrolysis reaction Methods 0.000 title claims abstract description 26
- 230000007062 hydrolysis Effects 0.000 title claims abstract description 23
- 238000000034 method Methods 0.000 title claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims abstract description 74
- 239000002253 acid Substances 0.000 claims abstract description 40
- 238000003860 storage Methods 0.000 claims abstract description 39
- 238000001816 cooling Methods 0.000 claims abstract description 33
- 239000000446 fuel Substances 0.000 claims abstract description 24
- 239000007788 liquid Substances 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims abstract description 13
- 239000000463 material Substances 0.000 claims abstract description 13
- 238000012544 monitoring process Methods 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 150000002431 hydrogen Chemical class 0.000 claims description 8
- 239000011232 storage material Substances 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 8
- 230000009123 feedback regulation Effects 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- 239000012535 impurity Substances 0.000 claims description 2
- 239000002808 molecular sieve Substances 0.000 claims description 2
- 239000000741 silica gel Substances 0.000 claims description 2
- 229910002027 silica gel Inorganic materials 0.000 claims description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 2
- 206010037660 Pyrexia Diseases 0.000 claims 1
- 238000000746 purification Methods 0.000 abstract description 3
- 238000011065 in-situ storage Methods 0.000 abstract 1
- 239000012528 membrane Substances 0.000 abstract 1
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 9
- 230000017525 heat dissipation Effects 0.000 description 4
- 230000002572 peristaltic effect Effects 0.000 description 4
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Natural products OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- PXRKCOCTEMYUEG-UHFFFAOYSA-N 5-aminoisoindole-1,3-dione Chemical compound NC1=CC=C2C(=O)NC(=O)C2=C1 PXRKCOCTEMYUEG-UHFFFAOYSA-N 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- 229910019440 Mg(OH) Inorganic materials 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 229910000103 lithium hydride Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 235000006408 oxalic acid Nutrition 0.000 description 1
- 238000002161 passivation Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 229910000033 sodium borohydride Inorganic materials 0.000 description 1
- 239000012279 sodium borohydride Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
- H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/065—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents from a hydride
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
-
- G—PHYSICS
- G01—MEASURING; TESTING
- G01D—MEASURING NOT SPECIALLY ADAPTED FOR A SPECIFIC VARIABLE; ARRANGEMENTS FOR MEASURING TWO OR MORE VARIABLES NOT COVERED IN A SINGLE OTHER SUBCLASS; TARIFF METERING APPARATUS; MEASURING OR TESTING NOT OTHERWISE PROVIDED FOR
- G01D21/00—Measuring or testing not otherwise provided for
- G01D21/02—Measuring two or more variables by means not covered by a single other subclass
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/16—Controlling the process
- C01B2203/1614—Controlling the temperature
- C01B2203/1619—Measuring the temperature
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/16—Controlling the process
- C01B2203/1614—Controlling the temperature
- C01B2203/1623—Adjusting the temperature
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/16—Controlling the process
- C01B2203/1628—Controlling the pressure
- C01B2203/1633—Measuring the pressure
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/16—Controlling the process
- C01B2203/1628—Controlling the pressure
- C01B2203/1638—Adjusting the pressure
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/16—Controlling the process
- C01B2203/1642—Controlling the product
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Physics & Mathematics (AREA)
- Health & Medical Sciences (AREA)
- Physics & Mathematics (AREA)
- General Health & Medical Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Fuel Cell (AREA)
Abstract
The invention discloses a magnesium hydride hydrolysis hydrogen production system and a control method thereof, which mainly comprise a storage system, a reaction system, a control system and a hydrogen utilization system. The material storage system comprises a weak acid material storage chamber, the weak acid material storage chamber is connected with a reaction chamber in the reaction system through a delivery pump, the reaction chamber is provided with a temperature sensor, a pressure sensor and a cooling device, a discharge hole of the reaction chamber is sequentially connected with a gas-liquid separation chamber and a hydrogen purifier in a hydrogen system, and a gas flowmeter is arranged on an outlet pipe of the hydrogen purifier; the control system includes a controller; the temperature signal of the temperature sensor, the pressure signal of the pressure sensor and the flow signal of the gas flowmeter are transmitted to the controller, and the controller controls and adjusts the conveying pump and the cooling device; the hydrogen production system is provided with the pressure and temperature monitoring and cooling device, so that the safe operation of the hydrogen production system can be ensured; the device is provided with a gas-liquid separation device and a purification device, so that the hydrogen can be prepared for use in situ; the addition of weak acid is controlled by a control system, so that the hydrogen production stop and start can be controlled, and the hydrogen production rate can be adjusted; can meet the application of proton exchange membrane fuel cell equipment.
Description
Technical Field
The invention belongs to the technical field of hydrogen preparation and supply, and particularly relates to a magnesium hydride hydrolysis hydrogen production system and a control method thereof.
Background
Due to the aggravation of environmental pollution and the exhaustion of petroleum energy, in recent years, a fuel cell is used as a clean energy conversion device, and meanwhile, the fuel cell has the advantages of high conversion efficiency, low noise, high energy density and the like, thereby attracting more and more attention of technological workers; the storage and transportation and preparation of hydrogen become key factors influencing the economic development of hydrogen energy, and the hydrogen storage technology can be roughly divided into physical hydrogen storage and chemical hydrogen storage, wherein the chemical hydrogen storage can utilize the hydrolysis reaction of active substances to prepare hydrogen, has the advantages of high hydrogen storage quantity, safe use, high hydrogen purity and the like, and can release hydrogen at normal temperature and pressure, so the hydrogen storage technology becomes a research hot spot in recent years.
The chemical hydrogen storage material mainly comprises sodium borohydride, magnesium hydride, lithium hydride, metal aluminum powder and the like; wherein MgH is 2 Among many hydrolytic hydrogen production materials, the price is relatively low, the property in the air is more stable, and the hydrogen storage density is higher; mgH (MgH) 2 Hydrolysis hydrogen production reaction principle: mgH (MgH) 2 +2H 2 O＝Mg(OH) 2 +H 2 A certain amount of heat is released during the reaction, which causes MgH 2 During the hydrolysis, a layer of Mg (OH) is formed on the surface 2 Passivation layer for preventing water from entering MgH 2 Participate in the reaction, which results in MgH alone 2 The hydrogen production amount of the reaction with water is very small, and MgH is greatly reduced 2 The hydrogen production rate of the catalyst is limited; research has shown that weak acid solutions such as citric acid,The addition of acetic acid, oxalic acid and the like can greatly improve MgH 2 Optimizing MgH 2 Is used for preparing hydrogen by hydrolysis; experiments show that magnesium hydride is mixed with water, the reaction is almost stopped after a period of time, the hydrogen production rate is extremely low, and the addition of weak acid can enable the hydrolysis reaction to be started rapidly, and the hydrogen production efficiency is greatly improved, so that the stopping and starting of the reaction and the reaction rate can be controlled by controlling the addition of weak acid; however, in the prior art, the stopping and starting of the reaction and the reaction rate are not controlled by controlling the addition of weak acid, so that the system and the method for preparing hydrogen by magnesium hydride hydrolysis have the advantages of controllable stopping and starting and adjustable hydrogen production rate.
Disclosure of Invention
In order to solve the problems in the prior art, the invention aims to provide a magnesium hydride hydrolysis hydrogen production system and a control method thereof.
In order to achieve the technical purpose, the invention adopts the following technical scheme:
in a first aspect of the present invention, there is provided a magnesium hydride hydrolysis hydrogen production system, the system comprising: the device comprises a storage system, a control system, a reaction system and a hydrogen utilization system;
the material storage system comprises a weak acid material storage chamber, the weak acid material storage chamber is connected with a reaction chamber in the reaction system through a delivery pump, the reaction chamber is provided with a temperature sensor, a pressure sensor and a cooling device, a discharge hole of the reaction chamber is sequentially connected with a gas-liquid separation chamber and a hydrogen purifier in a hydrogen system, and a gas flowmeter is arranged on an outlet pipe of the hydrogen purifier;
the control system includes a controller; the temperature signal of the temperature sensor, the pressure signal of the pressure sensor and the flow signal of the gas flowmeter are transmitted to the controller, and the controller controls and adjusts the conveying pump and the cooling device.
In a second aspect of the present invention, a control method for a magnesium hydride hydrolysis hydrogen production system is provided, which comprises the following steps:
(1) The magnesium hydride hydrogen storage material is pre-installed in the reaction chamber, the weak acid solution is pre-installed in the weak acid storage chamber, the total hydrogen amount required by the operation of the fuel cell system is firstly determined, and then the hydrogen yield of the magnesium hydride and the total amount of water and weak acid required by the hydrogen yield of the magnesium hydride are determined;
(2) Calculating and determining the flow of the conveying pump into weak acid according to the rated hydrogen flow of the fuel cell system; starting a conveying pump, and conveying the weak acid solution from the weak acid storage chamber into the reaction chamber at a set flow rate to react with the magnesium hydride hydrogen storage material in the reaction chamber and generate hydrogen;
(3) The temperature sensor is used for controlling the temperature T in the reactor during the reaction r Real-time monitoring is carried out, a temperature signal is transmitted to a controller, and the controller is used for controlling and adjusting the cooling device;
pressure sensor for pressure P inside reactor during reaction r Monitoring in real time, transmitting a pressure signal to a controller, and controlling and adjusting the conveying pump through the controller;
(4) The product after reaction in the reaction chamber is a gas-liquid mixture, and is automatically conveyed to a gas-liquid separation chamber under the influence of the air pressure in the reactor to carry out gas-liquid separation;
(5) The hydrogen purifier dries and purifies the wet hydrogen, and the purified hydrogen flows into the flowmeter;
(6) During the operation of the system, the flowmeter will measure the flow rate Q of the inflowing hydrogen i The flow rate is monitored in real time and is transmitted to the controller, the controller is used for carrying out feedback regulation on the delivery pump, and the flow rate is controlled to be within a certain range Q 1 ＜Q i ＜Q 2 Between them;
(7) The purified hydrogen enters the fuel cell system at a stable and controllable flow rate to be used as a hydrogen source.
One or more technical solutions provided in the embodiments of the present invention at least have the following technical effects or advantages:
1. the invention controls the stopping and starting of the reaction and the reaction rate by controlling the addition of the weak acid solution through the control system, monitors the flow in real time, feeds back and adjusts the flow signal, and can realize the controllable stopping and starting of hydrogen production and adjustable hydrogen production rate;
2. the invention uses chemical hydrogen storage material to supply hydrogen, has convenient storage and transportation, can convert chemical energy into electric energy, is environment-friendly, and has the characteristics of stable hydrogen release, controllable hydrogen production rate, instant hydrogen supply, high energy density and the like;
3. the cooling device and the pressure sensor are arranged, so that the working temperature and the working pressure of the system are normal, and the safety of the system is good;
4. the invention has simple and portable structure, safety and reliability, is now used for production, and is suitable for the application of multiple occasions of chemical hydrogen production fuel cell equipment.
Drawings
The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this application, illustrate embodiments of the application and together with the description serve to explain the application and do not constitute an undue limitation to the application.
FIG. 1 is a schematic diagram of the control system of the present invention;
in fig. 1: the system comprises a 1-storage system, a 2-control system, a 3-reaction system and a 4-hydrogen utilization system, wherein the 1-storage system comprises a 101-weak acid storage chamber and a 102-conveying pump; the 2-control system includes 201 a controller; the 3-reaction system comprises a 301-reaction chamber, a 302-pressure sensor, a 303-temperature sensor and a 304-cooling device; the 4-hydrogen system comprises a 401-gas-liquid separation chamber, 402-purifier, 403-gas flow meter and 404-fuel cell system.
Detailed Description
It should be noted that the following detailed description is illustrative and is intended to provide further explanation of the present application; unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments in accordance with the present application; as used herein, the singular is also intended to include the plural unless the context clearly indicates otherwise, and furthermore, it is to be understood that the terms "comprises" and/or "comprising" when used in this specification are taken to specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof.
Specifically, the invention is realized by the following technical scheme:
in a first aspect of the present invention, there is provided a magnesium hydride hydrolysis hydrogen production system, the system comprising: the device comprises a storage system, a control system, a reaction system and a hydrogen utilization system;
the material storage system comprises a weak acid material storage chamber, the weak acid material storage chamber is connected with a reaction chamber in the reaction system through a delivery pump, the reaction chamber is provided with a temperature sensor, a pressure sensor and a cooling device, a discharge hole of the reaction chamber is sequentially connected with a gas-liquid separation chamber and a hydrogen purifier in a hydrogen system, and a gas flowmeter is arranged on an outlet pipe of the hydrogen purifier;
the control system includes a controller; the temperature signal of the temperature sensor, the pressure signal of the pressure sensor and the flow signal of the gas flowmeter are transmitted to the controller, and the controller controls and adjusts the conveying pump and the cooling device.
Further, the weak acid storage chamber is provided with a feed inlet and a discharge outlet, and the discharge outlet is connected with a conveying pump.
Preferably, the conveying pump is a peristaltic pump, the flow accuracy is high, the operation, cleaning and replacement are convenient, and the problem that the cleaning and replacement are difficult due to acid-base corrosion can be avoided.
Further, the reaction chamber is provided with a feed inlet and a discharge outlet, the delivery pump is connected with the feed inlet of the reaction chamber, and the discharge outlet of the reaction chamber is connected with the gas-liquid separation chamber.
Further, a space is provided in the gas-liquid separation chamber for storing the separated liquid.
Further, the gas flow meter outlet is connected to a fuel cell system.
In a second aspect of the present invention, a control method for a magnesium hydride hydrolysis hydrogen production system is provided, which comprises the following steps:
(1) The magnesium hydride hydrogen storage material is pre-installed in the reaction chamber, the weak acid solution is pre-installed in the weak acid storage chamber, the total hydrogen amount required by the operation of the fuel cell system is firstly determined, and then the hydrogen yield of the magnesium hydride and the total amount of water and weak acid required by the hydrogen yield of the magnesium hydride are determined;
(2) Calculating and determining the flow of the conveying pump into weak acid according to the rated hydrogen flow of the fuel cell system; starting a conveying pump, and conveying the weak acid solution from the weak acid storage chamber into the reaction chamber at a set flow rate to react with the magnesium hydride hydrogen storage material in the reaction chamber and generate hydrogen;
preferably, experiments show that the magnesium hydride is mixed with water, the reaction is almost stopped after a period of time, the hydrogen production rate is extremely low, and the addition of weak acid can enable the hydrolysis reaction to be started rapidly, and the hydrogen production efficiency is greatly improved, so that the magnesium hydride and the water can be pre-mixed and then are filled into a reaction chamber; the treatment is more stable and controllable compared with the reaction of magnesium hydride directly with weak acid;
(3) The temperature sensor is used for controlling the temperature T in the reactor during the reaction r Real-time monitoring is carried out, a temperature signal is transmitted to a controller, and the controller is used for controlling and adjusting the cooling device;
pressure sensor for pressure P inside reactor during reaction r Monitoring in real time, transmitting a pressure signal to a controller, and controlling and adjusting the conveying pump through the controller;
further, the working threshold of the reactor is T 0 The operation power of the cooling device is divided into P from low to high 0 、P 1 、P 2 Three gears respectively corresponding to the temperature T from low to high 0 、T 1 、T 2 ，
When T is r ≥T 0 When in use; the cooling device is started to take a first gear P 0 Operating;
when T is 1 ≤T r ≤T 2 The cooling device is at the second gear P 1 Operating;
when T is 2 ≤T r The cooling device is in the third gear P 2 Operating;
when T is r ＜T 0 When the cooling device is in operation, the cooling device stops running;
preferably, the cooling device may be configured by assembling the fins outside the reactor by means of external air cooling, and disposing a fan facing the reactor; heat generated in the reaction process is conducted to the fins through the reactor wall, and then the heat is dissipated through the fan;
when T is r ≥T 0 The output duty cycle of the fan is 50%;
when T is 1 ≤T r ≤T 2 The output duty cycle of the fan is 75%;
when T is 2 ≤T r The output duty cycle of the fan is 100%;
when T is r ＜T 0 When the fan stops running;
further, when the pressure reaches the upper threshold P r-max When, i.e. P r ≥P r-max The conveying pump stops working;
(4) The product after reaction in the reaction chamber is a gas-liquid mixture, and is automatically conveyed to a gas-liquid separation chamber under the influence of the air pressure in the reactor to carry out gas-liquid separation;
because the densities of the hydrogen and the reaction waste liquid are different, when the liquid and the gas flow together, the liquid is subjected to the action of gravity and moves downwards, while the hydrogen moves upwards and continuously enters the hydrogen purifier under the influence of pressure;
(5) The hydrogen purifier dries and purifies the wet hydrogen, and the purified hydrogen flows into the flowmeter;
preferably, alkaline substances can be filled in the hydrogen purifier to neutralize weak acid, impurities are adsorbed through a molecular sieve, and finally wet hydrogen is dried through allochroic silica gel; the hydrogen entering the flowmeter is ensured to be dry and pure, and damage to the flowmeter and the fuel cell system can be avoided;
(6) During the operation of the system, the flowmeter will measure the flow rate Q of the inflowing hydrogen i The flow rate is monitored in real time and is transmitted to the controller, the controller is used for carrying out feedback regulation on the delivery pump, and the flow rate is controlled to be within a certain range Q 1 ＜Q i ＜Q 2 Between them;
further, Q 1 Typically not less than 95% of the rated hydrogen flow of the fuel cell system, Q 2 Typically no greater than 110% of the nominal hydrogen flow of the fuel cell system;
further, whenFlow exceeding (Q) 1 ,Q 2 ) The controller will adjust the flow rate of the delivery pump, Q i ＜Q 1 When the flow rate of the delivery pump is increased; and Q is i ＞Q 2 When the flow rate of the delivery pump is reduced; the larger the flow change of the excess part is, the larger the flow change of the delivery pump is, so that the stability of the flow is maintained;
(7) The purified hydrogen enters the fuel cell system at a stable and controllable flow rate to be used as a hydrogen source.
The technical scheme of the present application is described below by means of specific examples.
Example 1: as depicted in fig. 1, a magnesium hydride hydrolysis hydrogen production system comprising: the system comprises a storage system, a control system, a reaction system and a hydrogen utilization system, wherein the storage system comprises a weak acid storage chamber and a delivery pump; the control system comprises a controller; the reaction system comprises a reaction chamber, a pressure sensor, a temperature sensor and a cooling device; the hydrogen utilization system comprises a gas-liquid separation chamber, a purifier, a gas flowmeter and a fuel cell system; taking hydrogen supply of a fuel cell system with 100W power for 1h as an example, the required hydrogen flow is 1.8L/min, experiments prove that the required total water amount is about 0.3L, magnesium hydride is 72g, acetic acid is 0.3L, the flow of a conveying pump is adjusted to be 5.6mL/min, water and magnesium hydride are premixed in a reactor, a system is started, acetic acid solution is pumped into the reactor for reaction, at the moment, the reactor generates hydrogen with the hydrogen flow of about 1.8L/min, the generated hydrogen is subjected to gas-liquid separation and purification, and then is monitored in real time by a flowmeter, the flow is controlled in the range of (1.7L/min, 1.9L/min) by a controller, when the flow is lower than 1.7L/min, the flow of a peristaltic pump is continuously increased, when the flow is higher than 1.9L/min, the peristaltic pump flow is continuously reduced, fins and a fan are arranged outside the peristaltic pump reactor, and the heat power released by magnesium hydride hydrolysis is calculated to be 0.4KW according to theory, so that the heat dissipation power of a cooling device is determined, and the heat dissipation mode is achieved by an air cooling heat dissipation mode: the heat dissipation fins are assembled outside the reactor, a fan is arranged facing the reactor, heat generated in the reaction process is conducted to the fins through the wall of the reactor, then the heat is dissipated through the fan, and the power of the fan is increased along with the increase of the temperature; the generated hydrogen is sent into a fuel cell system for hydrogen supply at a stable flow rate after gas-liquid separation and purification.
Claims (10)
1. A system for producing hydrogen from hydrolysis of magnesium hydride, the system comprising: the device comprises a storage system, a control system, a reaction system and a hydrogen utilization system;
the material storage system comprises a weak acid material storage chamber, the weak acid material storage chamber is connected with a reaction chamber in the reaction system through a delivery pump, the reaction chamber is provided with a temperature sensor, a pressure sensor and a cooling device, a discharge hole of the reaction chamber is sequentially connected with a gas-liquid separation chamber and a hydrogen purifier in a hydrogen system, and a gas flowmeter is arranged on an outlet pipe of the hydrogen purifier;
the control system includes a controller; the temperature signal of the temperature sensor, the pressure signal of the pressure sensor and the flow signal of the gas flowmeter are transmitted to the controller, and the controller controls and adjusts the conveying pump and the cooling device.
2. A magnesium hydride hydrolysis hydrogen generation system as claimed in claim 1, characterized in that the weak acid storage chamber is provided with a feed inlet and a discharge outlet, the discharge outlet being connected to a transfer pump.
3. A magnesium hydride hydrolysis hydrogen generation system as claimed in claim 1, characterized in that the reaction chamber is provided with a feed inlet and a discharge outlet, and a transfer pump is connected to the feed inlet of the reaction chamber.
4. A magnesium hydride hydrolysis hydrogen generation system as claimed in claim 1, wherein said gas flow meter outlet is connected to a fuel cell system.
5. A control method of a magnesium hydride hydrolysis hydrogen production system is characterized by comprising the following steps:
(1) The magnesium hydride hydrogen storage material is pre-installed in the reaction chamber, the weak acid solution is pre-installed in the weak acid storage chamber, the total hydrogen amount required by the operation of the fuel cell system is firstly determined, and then the hydrogen yield of the magnesium hydride and the total amount of water and weak acid required by the hydrogen yield of the magnesium hydride are determined;
(2) Calculating and determining the flow of the conveying pump into weak acid according to the rated hydrogen flow of the fuel cell system; starting a conveying pump, and conveying the weak acid solution from the weak acid storage chamber into the reaction chamber at a set flow rate to react with the magnesium hydride hydrogen storage material in the reaction chamber and generate hydrogen;
(3) The temperature sensor is used for controlling the temperature T in the reactor during the reaction r Real-time monitoring is carried out, a temperature signal is transmitted to a controller, and the controller is used for controlling and adjusting the cooling device;
pressure sensor for pressure P inside reactor during reaction r Monitoring in real time, transmitting a pressure signal to a controller, and controlling and adjusting the conveying pump through the controller;
(4) The product after reaction in the reaction chamber is a gas-liquid mixture, and is automatically conveyed to a gas-liquid separation chamber under the influence of the air pressure in the reactor to carry out gas-liquid separation;
(5) The hydrogen purifier dries and purifies the wet hydrogen, and the purified hydrogen flows into the flowmeter;
(6) During the operation of the system, the flowmeter will measure the flow rate Q of the inflowing hydrogen i The flow rate is monitored in real time and is transmitted to the controller, the controller is used for carrying out feedback regulation on the delivery pump, and the flow rate is controlled to be within a certain range Q 1 ＜Q i ＜Q 2 Between them;
(7) The purified hydrogen enters the fuel cell system at a stable and controllable flow rate to be used as a hydrogen source.
6. The control method according to claim 5, characterized in that: in the step (2), magnesium hydride and water are mixed in advance and then are filled into a reaction chamber.
7. The control method according to claim 5, characterized in that: in the step (3), the working threshold value of the reactor is T 0 The operation power of the cooling device is divided into P from low to high 0 、P 1 、P 2 Three gears respectively corresponding to the low to highTemperature T of (2) 0 、T 1 、T 2 ，
When T is r ≥T 0 When in use; the cooling device is started to take a first gear P 0 Operating;
when T is 1 ≤T r ≤T 2 The cooling device is at the second gear P 1 Operating;
when T is 2 ≤T r The cooling device is in the third gear P 2 Operating;
when T is r ＜T 0 When the cooling device is in operation, the cooling device stops running;
preferably, the cooling device may be configured by assembling the fins outside the reactor by means of external air cooling, and disposing a fan facing the reactor; heat generated in the reaction process is conducted to the fins through the reactor wall, and then the heat is dissipated through the fan;
when T is r ≥T 0 The output duty cycle of the fan is 50%;
when T is 1 ≤T r ≤T 2 The output duty cycle of the fan is 75%;
when T is 2 ≤T r The output duty cycle of the fan is 100%;
when T is r ＜T 0 When the fan stops running;
further, when the pressure reaches the upper threshold P r-max When, i.e. P r ≥P r-max The transfer pump stops working.
8. The control method according to claim 5, characterized in that: in the step (5), alkaline substances can be filled in the hydrogen purifier to neutralize weak acid, impurities are adsorbed through a molecular sieve, and finally wet hydrogen is dried through allochroic silica gel.
9. The control method according to claim 5, characterized in that: in step (6), Q 1 Typically not less than 95% of the rated hydrogen flow of the fuel cell system, Q 2 Typically no greater than 110% of the nominal hydrogen flow of the fuel cell system;
when the flow rate isExceeding (Q) 1 ,Q 2 ) The controller will adjust the flow rate of the delivery pump, Q i ＜Q 1 When the flow rate of the delivery pump is increased; and Q is i ＞Q 2 When the flow rate of the delivery pump is reduced; the larger the flow rate variation of the excess portion is, the larger the flow rate variation of the delivery pump is so as to keep the flow rate stable.
10. Use of a magnesium hydride hydrolysis hydrogen production system according to any one of claims 1 to 4 and/or a control method of a magnesium hydride hydrolysis hydrogen production system according to any one of claims 5 to 9 for the production of hydrogen by magnesium hydride hydrolysis.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211735262.3A CN116216634B (en) | 2022-12-30 | 2022-12-30 | Magnesium hydride hydrolysis hydrogen production system and control method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211735262.3A CN116216634B (en) | 2022-12-30 | 2022-12-30 | Magnesium hydride hydrolysis hydrogen production system and control method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN116216634A true CN116216634A (en) | 2023-06-06 |
| CN116216634B CN116216634B (en) | 2024-10-18 |
Family
ID=86583547
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211735262.3A Active CN116216634B (en) | 2022-12-30 | 2022-12-30 | Magnesium hydride hydrolysis hydrogen production system and control method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116216634B (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020071102A (en) * | 2001-03-03 | 2002-09-12 | (주)에너펙텍 | A method for controlling a hydrogen and oxygen generator |
| KR20140072805A (en) * | 2012-11-30 | 2014-06-13 | 한국과학기술연구원 | Method and apparatus for simultaneous controlling of fuel concentration and temperature of liquid fuel cell by sensor-less and temperature-control based feed-back control, liquid fuel cell apparatus using the same |
| CN104555916A (en) * | 2015-01-09 | 2015-04-29 | 南京工业大学 | Continuous controllable magnesium hydride hydrolysis hydrogen production device and method for producing hydrogen by using same |
| US20150125348A1 (en) * | 2012-06-19 | 2015-05-07 | Bio Coke Lab.Co., Ltd. | Hydrogen Generation Apparatus |
| CN110002398A (en) * | 2019-04-16 | 2019-07-12 | 中国科学院嘉兴轻合金技术工程中心 | It is a kind of using magnesium hydride as the device for producing hydrogen of raw material and hydrogen production process |
| WO2019156627A1 (en) * | 2018-02-06 | 2019-08-15 | H3 Dynamics Holdings Pte. Ltd. | A portable fuel cell apparatus and system |
-
2022
- 2022-12-30 CN CN202211735262.3A patent/CN116216634B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20020071102A (en) * | 2001-03-03 | 2002-09-12 | (주)에너펙텍 | A method for controlling a hydrogen and oxygen generator |
| US20150125348A1 (en) * | 2012-06-19 | 2015-05-07 | Bio Coke Lab.Co., Ltd. | Hydrogen Generation Apparatus |
| KR20140072805A (en) * | 2012-11-30 | 2014-06-13 | 한국과학기술연구원 | Method and apparatus for simultaneous controlling of fuel concentration and temperature of liquid fuel cell by sensor-less and temperature-control based feed-back control, liquid fuel cell apparatus using the same |
| CN104555916A (en) * | 2015-01-09 | 2015-04-29 | 南京工业大学 | Continuous controllable magnesium hydride hydrolysis hydrogen production device and method for producing hydrogen by using same |
| WO2019156627A1 (en) * | 2018-02-06 | 2019-08-15 | H3 Dynamics Holdings Pte. Ltd. | A portable fuel cell apparatus and system |
| CN110002398A (en) * | 2019-04-16 | 2019-07-12 | 中国科学院嘉兴轻合金技术工程中心 | It is a kind of using magnesium hydride as the device for producing hydrogen of raw material and hydrogen production process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN116216634B (en) | 2024-10-18 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103579652B (en) | A kind of fuel cell generation of magnesium hydride hydrolyzation hydrogen supplying | |
| CN109958882B (en) | Integrated control system for hydrogen production by water electrolysis and alloy hydrogen storage | |
| CN111564884B (en) | Distributed power generation system and control method thereof | |
| CN111564647B (en) | Power supply system of methanol water hydrogen fuel cell and control method thereof | |
| CN104597409B (en) | Fuel cell testing system capable of performing circular electrolytic hydrogen production | |
| CN203617394U (en) | Portable PEMFC (proton exchange membrane fuel cell) power supply system | |
| CN103579651A (en) | Portable proton-exchange membrane fuel cell power system | |
| CN107093756A (en) | A kind of fuel cell system and its control method based on chemical hydrogen manufacturing | |
| CN107171005A (en) | A kind of hydrogen fuel cell system and its control method | |
| CN102610839B (en) | Safe and controllable portable power supply and control method | |
| CN101973520A (en) | Portable hydrogen generator based on aluminium hydrolysis reaction and control method | |
| CN108123152A (en) | It is a kind of using liquid oxygen as the fuel cell generation of oxidant | |
| CN116216634B (en) | Magnesium hydride hydrolysis hydrogen production system and control method thereof | |
| CN212655633U (en) | Comprehensive energy system based on municipal sewage treatment plant | |
| CN219117572U (en) | Energy-saving quick starting device of water electrolysis hydrogen production system | |
| CN113549954B (en) | Electrolytic hydrogen production system device and control method thereof | |
| CN212571060U (en) | Methanol-water hydrogen fuel cell power supply system | |
| CN115411315A (en) | Combined heat and power generation system of water electrolysis hydrogen production coupled metal solid hydrogen storage fuel cell | |
| CN105070928A (en) | Fuel cell oxygen supply system and oxygen supply method thereof | |
| CN114229794A (en) | Fixed type magnesium hydride hydrolysis automatic control device and method | |
| CN212085143U (en) | But continuous hydrogen power generation device | |
| CN205222681U (en) | Methanol -water reformation hydrogen manufacturing machine | |
| CN207353385U (en) | Fuel cell system thermal management control device and system | |
| CN218769638U (en) | Fuel cell power supply equipment based on hydrolysis hydrogen production unit | |
| CN201154895Y (en) | Hydrogen making system from borohydride |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant |