Continuous hydrolysis hydrogen production plant based on multi-stage screw conveyor reactor

Abstract

This invention provides a continuous water electrolysis hydrogen production device based on a multi-segment ribbon reactor. The device includes a water circulation system, a reaction system, a hydrogen purification system, and a control system. In this continuous water electrolysis hydrogen production device, the reaction zone is separated from the raw material storage zone and the product storage zone, enabling large-scale in-situ hydrogen production through continuous production with a simple system configuration. During the continuous water electrolysis hydrogen production process, this invention maintains the reaction system within a narrow temperature range between the set temperature and the boiling point of water by balancing the heat exchange of each reaction tube segment, enhancing the heat transfer process inside and outside each reaction tube segment, and utilizing the heat absorption process of excess reaction water vaporization. This maintains the stability of the hydrogen production rate of the solid hydrogen storage material.

Description

Technical Field

[0001] This utility model relates to hydrogen production technology by water electrolysis, and more particularly to a continuous hydrogen production device based on a multi-segment spiral reactor. Background Technology

[0002] Hydrogen, as the most promising zero-carbon energy source, is actively used in the production processes of various industries to achieve green transformation. However, difficulties in hydrogen storage and transportation hinder its further utilization. To address this, in-situ hydrogen production technology based on the chemical reactions between reactive metals, hydrides, and water offers an effective solution.

[0003] Hydrogen production devices employing the aforementioned in-situ hydrogen production technology often encounter problems such as system complexity, difficulty in heat extraction, and unstable hydrogen release rates when scaled up. For example, when using a container storing hydrogen production materials as a reactor, the size of the individual container must be limited to meet heat and mass transfer requirements, resulting in the hydrogen production system being broken down into multiple small units, increasing the number of devices. For example, the lack of temperature control during the mixing of hydrogen production materials and reaction water causes significant fluctuations in the reaction rate. Utility Model Content

[0004] The purpose of this invention is to address the problems of complex systems, difficult heat extraction, and unstable hydrogen release rates in existing in-situ hydrogen production devices by proposing a continuous water electrolysis hydrogen production device based on a multi-segment ribbon reactor. This device has sufficient and balanced heat extraction, stable reaction conditions, and a simple system composition, enabling safe and stable hydrogen production in scenarios with large-scale hydrogen production needs.

[0005] It should be noted that, in this utility model, unless otherwise specified, the specific meaning of "comprising" in relation to composition and description includes both open-ended meanings such as "comprising," "including," etc., and closed-ended meanings such as "composed of," "consisting of," etc., and similar meanings.

[0006] To achieve the above objectives, the technical solution adopted by this utility model is: a continuous hydrolysis hydrogen production device based on a multi-segment ribbon reactor, including a water circulation system, a reaction system, a hydrogen purification system and a control system;

[0007] The water circulation system includes an electrically heated water tank, a circulating pump, a constant temperature water tank, an electric three-way valve, a radiator, and a temperature sensor. The outlet of the electrically heated water tank is connected to the inlet of the constant temperature water tank via the circulating pump. The outlet of the constant temperature water tank is connected to both the inlet of the electrically heated water tank and the heat transfer medium inlet of the radiator via the electric three-way valve. The heat transfer medium outlet of the radiator is connected to the inlet of the electrically heated water tank. Temperature sensors are installed in both the electrically heated water tank and the constant temperature water tank.

[0008] The reaction system includes a motor, a reducer, a gear set, a hopper, a feed regulating device, reaction tubes, a ribbon stirring shaft, a water pump, a water intake pipe, a water injection pipe, and a product storage bin. Multiple reaction tubes are arranged side-by-side from top to bottom, with the discharge port of one reaction tube connected to the feed port of the next. The hopper is connected to the feed port of the uppermost reaction tube via the feed regulating device, and the discharge port of the lowermost reaction tube is connected to the product storage bin. The inlet of the water intake pipe is located in a constant temperature water tank, and the outlet of the water intake pipe is connected to the inlet of the water injection pipe via the outlet of the water pump. The outlet of the water injection pipe is connected to the reaction tube. The motor, reducer, gear set, and ribbon stirring shaft are connected sequentially. The ribbon stirring shaft is located within the reaction tubes, and the rotational speeds of the ribbon stirring shafts in different reaction tubes can be the same or different, with the rotational speeds adjusted by the gear set.

[0009] The hydrogen purification system includes a condenser and a dryer. The reaction tube (upper part) and the product storage chamber (upper part) are respectively connected to the condenser. The top outlet of the condenser is connected to the dryer. The outlet of the dryer is connected to the hydrogen-using equipment and / or hydrogen-storage equipment.

[0010] The electric heating water tank, circulating pump, electric three-way valve, motor, feed regulating device, water inlet pump and temperature sensor are all connected to the control system.

[0011] Furthermore, the feeding adjustment device is a screw feed structure or an adjustable valve.

[0012] Furthermore, a filter layer is provided at one end of the reaction tube near the condenser; more specifically, the filter layer is provided inside the reaction tube between the discharge port and the condenser.

[0013] Furthermore, the outlet of the water injection pipe is located near the inlet and outlet of the reaction pipe; preferably, the outlet of the water injection pipe is located near the inlet and outlet of the upper reaction pipe; more preferably, the outlet of the water injection pipe is located near the inlet and outlet of the uppermost reaction pipe (first-stage reaction pipe), and also near the inlet of the second reaction pipe (second-stage reaction pipe) from top to bottom.

[0014] Furthermore, a flap is provided on the spiral stirring shaft between adjacent spirals, which can improve the stirring intensity.

[0015] Furthermore, the included angle between adjacent extended surfaces of the flaps is 60-120°, preferably 90°.

[0016] Furthermore, the flap is a rectangular plate, the width of the flap is 1 / 2 to 2 / 3 of the pitch, and the height is flush with the screw ribbon.

[0017] Another objective of this utility model is to disclose a continuous hydrolysis hydrogen production method, comprising the following steps:

[0018] The water circulation system maintains the reaction system (the reaction system inside the reaction tube) within the set temperature range through preheating and heat extraction processes;

[0019] Solid hydrogen production materials are fed from the silo into the reaction tube through the feed inlet via a feed regulating device;

[0020] Water from the constant temperature water tank is injected into the reaction tube through the water intake pipe, water inlet pump, and water injection pipe;

[0021] The spiral stirring shaft inside the reaction tube rotates under the drive of the motor, stirring the solid hydrogen production material and mixing it with water. At the same time, it pushes the mixture towards the discharge port. During the process of moving towards the discharge port, the mixture undergoes a chemical reaction to generate hydrogen and release a large amount of heat.

[0022] A large amount of heat causes water to vaporize into water vapor. The vaporization process of water can carry away a large amount of heat of reaction, which helps to maintain the temperature of the reaction system. Water vapor and hydrogen flow sequentially through the filter layer, condenser and dryer to the subsequent process. The condenser realizes the condensation and separation of water vapor, and the dryer is used to absorb the residual moisture in the hydrogen.

[0023] The control unit enables the automatic operation of the continuous water electrolysis hydrogen production unit.

[0024] Furthermore, the preheating and heat extraction of the water circulation system includes the following steps:

[0025] 1) During the reaction preparation stage, the water in the electric heating water tank is heated to the set temperature, which is 70℃-90℃; then, the circulating pump injects high-temperature water into the constant temperature water tank to preheat the reaction tube.

[0026] 2) In the initial stage of the reaction, the water in the constant temperature water tank, as one of the reactants, increases the overall temperature of the reactants;

[0027] 3) During the reaction, heat exchange occurs between the constant temperature water tank and the reaction tube, which quickly removes the heat released by the reaction and regulates the temperature of the reaction system.

[0028] When the temperature sensor detects that the temperature inside the constant temperature water tank is lower than the set value (85-95℃, preferably 90℃), the circulating water flows directly back to the electric heating water tank; when it is higher than the set value (85-95℃, 90℃), the circulating water flows through the radiator to cool down and then flows back to the electric heating water tank. The change of the return flow path is controlled by an electric three-way valve.

[0029] The operating flow rate of the circulating pump is 50-70% of the maximum flow rate, preferably 60%. When the temperature in the constant temperature water tank continues to be higher than the set upper limit, the flow rate of the circulating pump is gradually increased to enhance the heat dissipation effect by increasing the amount of water flowing through the radiator, until the temperature drops back to the set range.

[0030] Furthermore, the solid hydrogen production material is magnesium hydride.

[0031] Furthermore, the feed rate of the solid hydrogen production material is determined by the target hydrogen release rate and the reaction properties of the solid hydrogen production material. Specifically, the feed rate q of the solid hydrogen production material is:

[0032] q=(V / 22.4*2) / k (Equation 1)

[0033] Where: q—feed rate of solid hydrogen production material, g / min;

[0034] V—Target hydrogen release rate, L / min;

[0035] k——hydrogen release per unit mass of solid hydrogen production material, g(H2) / g;

[0036] l — the distance the spiral agitator shaft advances per revolution, in m / r.

[0037] Furthermore, the water injection volume of the reaction tube is 2-4 times the theoretical water volume required for the hydrogen production reaction of the solid hydrogen storage material it carries.

[0038] Furthermore, the pitch and rotational speed of the ribbon stirring shaft and the length of the reaction tube determine the residence time of the mixture in the reaction tube, and the ratio of the number of teeth in the gear set is used to adjust the difference in residence time of the mixture in different reaction tubes. Specifically, the residence time T of the mixture of the solid hydrogen production material and water in the reaction tube is:

[0039] T=L / (r×l) (Equation 2)

[0040] Where: T—reaction time in the tube, min;

[0041] L—Reaction tube length, in meters;

[0042] r—Speed ​​of rotation of the ribbon agitator shaft, r / min;

[0043] l — the distance the spiral agitator shaft advances per revolution, in m / r.

[0044] Furthermore, to ensure that the amount of hydrogen released in each reaction tube is the same, the residence time of the mixture in each reaction tube is different, and the specific time is allocated according to the characteristics of the reaction process. For example, when using three reaction tubes for the hydrolysis of magnesium hydride to produce hydrogen, the residence time ratio of the mixture in the first, second, and third reaction tubes is 30:15:30.

[0045] Furthermore, due to the characteristics of the hydrolysis hydrogen production process, the conversion of the last 5% of magnesium hydride takes a long time and releases relatively little heat. Therefore, the conversion of the remaining 5% of magnesium hydride is completed in the product storage chamber.

[0046] Furthermore, the reaction tubes are connected to the feed regulating device, water injection pipe, ribbon stirring shaft, condenser, and product storage bin. The residence time in each reaction tube is determined by the hydrogen release characteristics of the solid hydrogen production material. When the total hydrogen release per unit mass of solid hydrogen production material is N liters, and the reaction tubes are divided into n tubes, with the hydrogen release of magnesium hydride in each tube remaining consistent, the cumulative hydrogen release curve is divided into n parts. The hydrogen release amount corresponding to each part is N / n liters, and the time length corresponding to this cumulative hydrogen release curve is the residence time of the solid hydrogen production material in the reaction tube. For example, if the total hydrogen release is 9L, and three reaction tubes are used, the total residence time of the reaction tubes is the time taken for three 3L hydrogen releases. Since the reaction rate is different at different times, the time taken for each reaction tube is different. Since each reaction tube has the same length but a different residence time, a different rotation speed is required, resulting in different material layer heights, i.e., different filling amounts. The filling amount of solid hydrogen production material in the reaction tube is 40%-70%.

[0047] 70% ≥ (q×T / ρ) / (L×A) ≥ 40% (Equation 3)

[0048] A = A1 - A2 (Equation 4)

[0049] Where: ρ—bulk density of solid hydrogen production material, g / m³ 3 ;

[0050] A – Available cross-sectional area of ​​the reaction tube, square meters;

[0051] A1—Cross-sectional area of ​​the reaction tube calculated based on its inner diameter, in square meters;

[0052] A2 – Cross-sectional area of ​​the spiral agitator shaft, in square meters.

[0053] The advantages of keeping the amount of hydrogen released by magnesium hydride in each reaction tube consistent are as follows: (1) The gas flow rate in each reaction tube is similar, which can avoid the gas flow rate in a certain reaction tube being too high due to the excessive concentration of hydrogen release, which would interfere with the flow state of the slurry reactants, such as being carried out of the reaction tube too fast by the high-speed gas flow; (2) The same amount of hydrogen release means that the amount of magnesium hydride participating in the reaction is the same, and the corresponding heat release is the same. This can ensure that the heat load of each reaction tube is similar, which is conducive to heat transfer and maintaining stable reaction conditions.

[0054] Another objective of this invention is to disclose the application of a continuous hydrolysis hydrogen production device based on a multi-segment ribbon reactor in the field of hydrolysis hydrogen production.

[0055] This invention relates to a continuous hydrolysis hydrogen production device based on a multi-segment ribbon reactor. Its compact structural design and precise condition control effectively solve the problems faced by large-scale in-situ hydrogen production devices. Specifically, compared with existing technologies, it has the following advantages:

[0056] 1) The system has sufficient heat extraction: The reaction tube is located in a constant temperature water tank with a large heat extraction area; the reaction tube contains a spiral rotating stirring structure to ensure sufficient heat exchange between the reactants and the wall surface; the temperature of the reaction system is maintained close to the boiling point of water, and excess heat of reaction can be removed by the latent heat of vaporization of water; therefore, the temperature of the reaction system is controlled through good heat exchange inside the reaction tube, heat exchange between the reaction tube and the water in the constant temperature water tank, and the vaporization process of the reactant water.

[0057] 2) System heat extraction balance: In the multi-stage design of the reactor, the residence time of the hydrogen storage material in each reaction zone was adjusted by changing the speed of the screw conveyor based on the reaction properties of the solid hydrogen production material, so as to ensure that the heat release of the reaction process in each reactor stage is similar.

[0058] 3) Stable reaction conditions: The reaction tube is placed in a constant temperature water tank, and the external temperature conditions are stable; the water participating in the reaction comes from the constant temperature water tank, and due to the high heat capacity of water, the overall temperature of the reactants is stable; the sufficient heat extraction conditions allow the temperature of the reaction system to be maintained within a narrow temperature range close to the boiling point of water; the above measures ensure the stability of the reaction conditions, and correspondingly, the hydrogen release rate is stabilized.

[0059] 4) Simple system composition: The reactor design separates the reaction area from the raw material storage area and the product storage area, which is suitable for large-scale hydrogen production scenarios and avoids the problem of increased equipment quantity caused by using multiple small unit combined hydrogen production schemes.

[0060] In summary, this invention, based on a multi-segment ribbon reactor, separates the reaction zone from the raw material storage zone and the product storage zone, enabling large-scale in-situ hydrogen production through a simple system configuration and continuous production. During the continuous hydrolysis hydrogen production process, this invention maintains the reaction system within a narrow temperature range between the set temperature and the boiling point of water by balancing the heat exchange of each reaction tube segment, enhancing the heat transfer process inside and outside each reaction tube segment, and utilizing the heat absorption process of excess reaction water during vaporization. This ensures the stability of the hydrogen production rate of the solid hydrogen storage material. Attached Figure Description

[0061] Figure 1 This is a schematic diagram of a continuous hydrolysis hydrogen production device with a multi-segment ribbon reactor.

[0062] Figure 2 This is a particle size distribution diagram of magnesium hydride;

[0063] Figure 3 A schematic diagram of a three-stage reactor design based on the hydrolysis reaction curve of magnesium hydride per unit mass.

[0064] Figure 4 This is a schematic diagram of the cross-sectional dimensions of the reaction tube;

[0065] Figure 5 This is a schematic diagram of the structure of the spiral ribbon stirring shaft.

[0066] Figure 6 This is a schematic diagram of the structure of the second spiral ribbon stirring shaft.

[0067] Among them, 1-electric heating water tank, 2-circulating pump, 3-constant temperature water tank, 4-electric three-way valve, 5-radiator, 6-motor, 7-reducer, 8-gear set, 9-hopper, 10-feed adjustment device, 11-reaction tube, 12-screw ribbon stirring shaft, 13-water inlet pump, 14-water intake pipe, 15-water injection pipe, 16-filter layer, 17-product storage bin, 18-condenser, 19-dryer, 20-temperature sensor, 21-control system. Detailed Implementation

[0068] This utility model of a multi-segment ribbon reactor for continuous hydrolysis hydrogen production consists of four parts: a water circulation system, a reaction system, a control system, and a hydrogen purification system. It includes an electric heating water tank, a circulation pump, a constant temperature water tank, an electric three-way valve, a radiator, a motor, a reducer, a gear set, a silo, a feed regulating device, a reaction tube, a ribbon stirring shaft, a water inlet pump, a water intake pipe, a water injection pipe, a filter layer, a product storage silo, a condenser, a radiator, a temperature sensor, and a control system, among other equipment or components.

[0069] (1) Water circulation system

[0070] The water circulation system consists of an electrically heated water tank, a circulating pump, a constant-temperature water tank, an electric three-way valve, a radiator, and a temperature sensor. The electrically heated water tank, circulating pump, constant-temperature water tank, and electric three-way valve are connected sequentially. The electric three-way valve is directly connected to the electrically heated water tank via piping, or connected to the electrically heated water tank via the radiator. Temperature sensors are installed on the electrically heated water tank and the constant-temperature water tank to monitor their temperature.

[0071] The water circulation system ensures that the reaction system is maintained within the set temperature range through preheating and heat extraction processes.

[0072] ① During the reaction preparation stage, the water in the electric heating water tank is heated to a set temperature, which is between 70℃ and 90℃. Subsequently, the circulating pump injects the high-temperature water into the constant temperature water tank to preheat the reaction tube.

[0073] ② In the initial stage of the reaction, the water in the constant temperature water tank, as one of the reactants, raises the overall temperature of the reactants.

[0074] ③ During the reaction process, heat is exchanged between the constant temperature water tank and the reaction tube, which quickly removes the heat released by the reaction and regulates the temperature of the reaction system.

[0075] When the temperature sensor detects that the temperature inside the constant temperature water tank is lower than the set value, the circulating water flows directly back to the electric heating water tank; when it is higher than the set value, the circulating water flows through the radiator back to the electric heating water tank. The switching of the return flow path is controlled by an electric three-way valve.

[0076] The circulating pump operates at 60% of its maximum flow rate. When the temperature in the constant temperature water tank is higher than the set upper limit or lower than the set lower limit, the flow rate is gradually increased until the maximum value is reached.

[0077] (2) Reaction System

[0078] The reaction system consists of a motor, reducer, gear set, silo, feed regulating device, reaction tube, ribbon stirring shaft, water pump, water intake pipe, water injection pipe, filter layer, product storage silo, etc.

[0079] The silo is connected to a feed regulating device, which can be a screw feed structure or an adjustable valve. The feed regulating device is connected to the front end of the reaction tube, feeding the solid hydrogen production material from the silo into the reaction tube. The feed rate of the solid hydrogen production material is determined by the target hydrogen release rate and the reactivity of the solid hydrogen production material.

[0080] q=(V / 22.4*2) / k (Equation 1)

[0081] Where: q—feed rate of solid hydrogen production material, g / min;

[0082] V—Target hydrogen release rate, L / min;

[0083] k——hydrogen release per unit mass of solid hydrogen production material, g(H2) / g;

[0084] l — the distance the spiral agitator shaft advances per revolution, in m / r.

[0085] The water pump is connected to the intake pipe and the injection pipe at both ends. The end of the intake pipe is located in a constant temperature water tank, and the end of the injection pipe is located near the feed inlet and discharge outlet, injecting the reactant water into the reaction tube. The water intake volume is 2-4 times the theoretical water volume required for the hydrogen production reaction of the solid hydrogen storage material.

[0086] The motor, reducer, gear set, and ribbon stirring shaft are connected in sequence, with the ribbon stirring shaft fixed inside the reaction tube. The ribbon stirring shaft stirs the solid hydrogen-producing material and water, while simultaneously propelling the mixture backward. During this backward movement, a chemical reaction occurs, generating hydrogen gas and releasing a large amount of heat.

[0087] The large amount of heat from the reaction causes water to vaporize. The water vapor and hydrogen flow through the filter layer into the condenser. The vaporization of the water vapor carries away a significant amount of heat from the reaction, which helps maintain the temperature of the reaction system.

[0088] The pitch and rotation speed of the ribbon stirring shaft, as well as the length of the reaction tube, determine the residence time of the mixture in the reaction tube. The ratio of the number of teeth in the gear set is used to adjust the difference in residence time of the mixture in different reaction tubes.

[0089] T=L / (r×l) (Equation 2)

[0090] Where: T—reaction time in the tube, min;

[0091] L—Reaction tube length, in meters;

[0092] r—Speed ​​of rotation of the ribbon agitator shaft, r / min;

[0093] l — the distance the spiral agitator shaft advances per revolution, in m / r.

[0094] The reaction tube is connected to the feed regulating device, water inlet pipe, ribbon agitator shaft, condenser, and product storage bin. The residence time in each section of the reaction tube is determined by the hydrogen release characteristics of the solid hydrogen production material. When the total hydrogen release per unit mass of solid hydrogen production material is N liters, and the reaction tube is divided into n sections, the time length corresponding to each N / n liter on the time axis of the cumulative hydrogen release curve is the residence time of the reaction tube. The material filling volume in the reaction tube should be between 40% and 70%.

[0095] 70% ≥ (q×T / ρ) / (L×A) ≥ 40% (Equation 3)

[0096] A = A1 - A2 (Equation 4)

[0097] Where: ρ—bulk density of solid hydrogen production material, g / m³ 3 ;

[0098] A – Available cross-sectional area of ​​the reaction tube, square meters;

[0099] A1—Cross-sectional area of ​​the reaction tube calculated based on its inner diameter, in square meters;

[0100] A2 – Cross-sectional area of ​​the spiral agitator shaft, in square meters.

[0101] The product storage tank is connected to the outlet of the last section of the reaction tube and the condenser, and is used to store the reaction products.

[0102] (3) Control System

[0103] The control system consists of a control unit and communication lines. The control unit is connected to the electric heating water tank, circulating pump, electric three-way valve, feed regulating device, water inlet pump, and temperature sensor via the communication lines. The control unit is used to realize the automatic operation of the continuous water electrolysis hydrogen production unit.

[0104] (4) Purification System

[0105] The purification system consists of a condenser and a dryer. The condenser inlet is connected to the reaction tube, and the dryer inlet is connected to the condenser outlet. The condenser condenses and separates water vapor, while the dryer absorbs residual moisture from the hydrogen gas.

[0106] The present invention will be further described below with reference to embodiments. The description of the technical features described below is based on representative embodiments and specific examples of the present invention, but the present invention is not limited to these embodiments and specific examples. It should be noted that:

[0107] Unless otherwise stated, all units used in this specification are international standard units, and all numerical values ​​and ranges appearing in this utility model should be understood to include systematic errors that are unavoidable in industrial production.

[0108] In this specification, the range of values ​​referred to as "value A to value B" refers to the range including the endpoint values ​​A and B.

[0109] In this specification, the numerical range indicated by "above" or "below" refers to the numerical range that includes the stated number.

[0110] In this specification, the word "may" has two meanings: to perform a certain process and not to perform a certain process.

[0111] In this specification, the terms "optional" or "optional" are used to indicate the use or omission of certain substances, components, procedures, application conditions, etc.

[0112] In this instruction manual, when "room temperature" or "room temperature" is used, the temperature can be 15-25℃.

[0113] Unless otherwise specified, all reagents or instruments used in this instruction manual are commercially available products.

[0114] Example 1

[0115] This embodiment discloses a continuous water electrolysis hydrogen production device based on a multi-segment ribbon reactor, such as... Figure 1 As shown, it includes a water circulation system, a reaction system, a hydrogen purification system, and a control system;

[0116] The water circulation system includes an electric heating water tank 1, a circulation pump 2, a constant temperature water tank 3, an electric three-way valve 4, a radiator 5, and a temperature sensor 20. The outlet of the electric heating water tank 1 is connected to the inlet of the constant temperature water tank 3 through the circulation pump 2. The outlet of the constant temperature water tank 3 is connected to the inlet of the electric heating water tank 1 and the heat medium inlet of the radiator 5 through the electric three-way valve 4. The heat medium outlet of the radiator 5 is connected to the inlet of the electric heating water tank 1. Temperature sensors 20 are installed in both the electric heating water tank 1 and the constant temperature water tank 3.

[0117] The reaction system includes a motor 6, a reducer 7, a gear set 8, a hopper 9, a feed regulating device 10, reaction tubes 11, a ribbon stirring shaft 12, a water pump 13, a water intake pipe 14, a water injection pipe 15, and a product storage bin 17. There are three reaction tubes 11 arranged side-by-side from top to bottom. The discharge port of the first reaction tube is connected to the feed inlet of the second reaction tube, and the discharge port of the second reaction tube is connected to the feed inlet of the third reaction tube. The hopper 9 is connected to the feed inlet of the first (uppermost) reaction tube 11 via the feed regulating device 10, and the discharge port of the third (lowermost) reaction tube is connected to the product storage bin 17. The feed regulating device 10 is an adjustable valve. The inlet of the water intake pipe 14 is located in the constant temperature water tank 3, and the outlet of the water intake pipe 14 is connected to the inlet of the water injection pipe 15 through the outlet of the water pump 13. The outlet of the water injection pipe 15 is located near the feed inlet and discharge outlet of the reaction pipe 11. Specifically, the water injection positions of the water injection pipe 15 are located near the feed inlet of the first stage of the reaction pipe 11, at the top of the discharge position from the first stage to the second stage of the reaction pipe 11, and at the top of the discharge position from the second stage to the third stage of the reaction pipe 11. The motor 6, reducer 7, gear set 8 and spiral ribbon stirring shaft 12 are connected in sequence, and the spiral ribbon stirring shaft 12 is arranged in the reaction pipe 11.

[0118] The ribbon stirring shaft can be adopted Figure 5 The structure shown is conventional. To improve stirring intensity, alternative methods can also be employed. Figure 6 The diagram shows a spiral stirring shaft with flaps, positioned on the spiral stirring shaft at the midpoint of adjacent spirals, with an included angle of 90° between the extended surfaces of adjacent flaps. Each flap is a rectangular plate, with a width equal to half the spiral pitch and a height flush with the spiral ribbon.

[0119] The hydrogen purification system includes a condenser 18 and a dryer 19. The reaction tube 11 and the product storage chamber 17 are respectively connected to the condenser 18. A filter layer 16 is provided inside the reaction tube 11 near the end of the condenser 18. The top outlet of the condenser 18 is connected to the dryer 19.

[0120] The electric heating water tank 1, circulating pump 2, electric three-way valve 4, motor 6, feed regulating device 10, water inlet pump 13 and temperature sensor 20 are all connected to the control system 21.

[0121] A continuous water electrolysis hydrogen production device based on a multi-stage ribbon reactor is used. The method for continuous water electrolysis hydrogen production is as follows:

[0122] Design goal: A hydrogen production system with a hydrogen supply rate of 100 L / min.

[0123] Using large-particle magnesium hydride as a solid hydrogen production material, the mass hydrogen storage density is 6.88%, the bulk density is 650 g / L, and the particle size distribution is shown in [reference needed]. Figure 2 The hydrogen desorption rate curve of magnesium hydride at 80℃ is shown in the figure. Figure 3 The hydrolysis conversion rate of magnesium hydride is 95%, and the hydrogen production per unit mass of magnesium hydride is 1.46L.

[0124] The feed rate of magnesium hydride to the reactor is:

[0125] 100L(H2) / min÷1.46L(H2) / g(MgH2)=68.5g(MgH2) / min

[0126] According to the three-stage reactor design, the hydrogen release rate of magnesium hydride must be kept consistent across the three reactor zones: the first reaction tube (first stage reactor), the second reaction tube (second stage reactor), and the third reaction tube (third stage reactor). Therefore, in Figure 3 The time points corresponding to 1 / 3, 2 / 3, and 3 / 3 of the total flow rate were selected from the cumulative flow curve as the residence time for each region. That is, the residence time in the first reactor was 30 min, the residence time in the second reactor was 15 min, and the residence time in the third reactor was 30 min. The remaining magnesium hydride was converted in the product storage chamber.

[0127] The spiral agitator shaft has an inner diameter of 20mm, an outer diameter pitch of 4cm, and a length of 1.2m. Based on the residence time requirements, the rotational speeds of the three reactor sections are 1r / min, 2r / min, and 1r / min, respectively.

[0128] The material filling volume inside the reactor is:

[0129] 30min×68.5g(MgH2) / min÷650g / L=3.2L

[0130] The stirring shaft occupies a small proportion of the space inside the reaction tube and is therefore not considered when calculating the inner cavity of the reaction tube.

[0131] Based on a filling rate of 60%, the inner diameter of the reaction tube is:

[0132]

[0133] Therefore, the thickness of the stirring shaft can be 2mm and the height can be 25mm.

[0134] See the schematic diagram of the cross-sectional dimensions of the reaction tube. Figure 4 .

[0135] The total water intake of the pump is 2-3 times the amount required for a 90% magnesium hydride reaction. As designed, the hydrogen production in the three reactor stages is equal, with a conversion rate of 30%, requiring a theoretical water flow rate of 76.4 mg / min. Therefore, the first water injection point requires 3 times the water volume (229 ml / min); the second water injection point requires 2 times the water volume (152.8 ml / min); and the third water injection point requires 2 times the water volume (152.8 ml / min).

[0136] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of this utility model, and are not intended to limit it. Although the utility model has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features therein. Such modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of this utility model.

Claims

1. A continuous hydrolysis hydrogen generation device based on a multi-stage screw conveyor reactor, characterized by, This includes a water circulation system, a reaction system, a hydrogen purification system, and a control system; The water circulation system includes an electric heating water tank (1), a circulation pump (2), a constant temperature water tank (3), an electric three-way valve (4), a radiator (5), and a temperature sensor (20). The outlet of the electric heating water tank (1) is connected to the inlet of the constant temperature water tank (3) through the circulation pump (2). The outlet of the constant temperature water tank (3) is connected to the inlet of the electric heating water tank (1) and the heat medium inlet of the radiator (5) through the electric three-way valve (4). The heat medium outlet of the radiator (5) is connected to the inlet of the electric heating water tank (1). Temperature sensors (20) are installed in both the electric heating water tank (1) and the constant temperature water tank (3). The reaction system includes a motor (6), a reducer (7), a gear set (8), a hopper (9), a feed regulating device (10), a reaction tube (11), a ribbon stirring shaft (12), a water pump (13), a water intake pipe (14), a water injection pipe (15), and a product storage hopper (17); the reaction tube (11) consists of multiple tubes arranged side by side from top to bottom, with the discharge port of one reaction tube connected to the feed inlet of the next reaction tube; the hopper (9) is connected to the uppermost reaction tube via the feed regulating device (10). The feed inlet of the reaction tube (11) is connected to the product storage chamber (17), and the discharge port of the lowest reaction tube is connected to the product storage chamber (17); the inlet of the water intake pipe (14) is located in the constant temperature water tank (3), the outlet of the water intake pipe (14) is connected to the inlet of the water injection pipe (15) through the outlet of the water pump (13), and the outlet of the water injection pipe (15) is connected to the reaction tube (11); the motor (6), reducer (7), gear set (8) and spiral ribbon stirring shaft (12) are connected in sequence, and the spiral ribbon stirring shaft (12) is set in the reaction tube (11); The hydrogen purification system includes a condenser (18) and a dryer (19). The reaction tube (11) and the product storage chamber (17) are respectively connected to the condenser (18), and the top outlet of the condenser (18) is connected to the dryer (19). The electric heating water tank (1), circulating pump (2), electric three-way valve (4), motor (6), feed regulating device (10), water pump (13) and temperature sensor (20) are all connected to the control system (21) in communication.

2. The continuous hydrolysis hydrogen production apparatus based on multi-stage screw belt reactor according to claim 1, characterized in that, The feed regulating device (10) is a screw feed structure or an adjustable valve.

3. The continuous hydrolysis hydrogen production device based on a multi-segment ribbon reactor according to claim 1, characterized in that, A filter layer (16) is provided at one end of the reaction tube (11) near the condenser (18).

4. The continuous hydrolysis hydrogen production apparatus based on multi-stage screw belt reactor according to claim 1, characterized in that, The outlet of the water injection pipe (15) is located near the inlet and outlet of the reaction pipe (11).

5. The continuous hydrolysis hydrogen production apparatus based on multi-stage screw conveyor reactor according to claim 1, wherein, A flap is provided on the spiral stirring shaft between adjacent spirals.

6. The continuous hydrolysis hydrogen production apparatus based on multi-stage screw belt reactor according to claim 5, characterized in that, The included angle between the extended surfaces of adjacent flaps is 60-120°.

7. The continuous hydrolysis based hydrogen generation apparatus using multiple zone screw conveyor reactor as claimed in claim 5 wherein, The flap is a rectangular plate, the width of which is 1 / 2 to 2 / 3 of the pitch, and the height is flush with the screw ribbon.

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