Hydrogen storage and compression system

Abstract

A hydrogen storage and compression system includes a hydrogen storage and compression device and a thermal management system. The apparatus includes a housing and a plurality of storage and compression units mounted within an interior chamber of the housing. Each storage and compression unit includes a container for hydrogen storage and compression and a metal hydride contained within the container. The vessel is interconnected with the hydrogen inlet and the hydrogen outlet through a hydrogen circuit flow system for connection to a hydrogen consuming device and a hydrogen source. The thermal management system includes a hot liquid circuit system and a heat exchanger system. The circuit system includes a closed-loop hot liquid flow circuit, a hot liquid flowing within the flow circuit, and a pump for pumping the hot liquid. A flow circuit is connected to the liquid inlet and the liquid outlet of the housing for flowing a hot liquid through an interior chamber of a container surrounding the storage and compression unit for cooling or heating the storage and compression unit. The flow circuit is coupled to a first heat exchanger connected to a heating source and a second heat exchanger connected to a cooling source.

Description

[0001] Cross-reference to related applications

[0002] This application claims the benefit of and priority to European Application No. EP23189911.3 filed on August 7, 2023, the entire contents of which are incorporated herein by reference. Technical Field

[0003] The present disclosure relates to a hydrogen storage and compression system using metal hydrides. Background Art

[0004] Hydrogen storage is a key step in decarbonizing fossil fuel technologies using renewable energy.

[0005] Metal hydrides are of interest for hydrogen compression because many metals and alloys can reversibly absorb large amounts of hydrogen and can compress the hydrogen by adding heat. Molecular hydrogen dissociates on the surface of the metal hydride and is then absorbed. After desorption, the two H atoms then recombine to form H 2 The hydrogen absorption reaction in the material is generally exothermic (generating heat), while the hydrogen desorption reaction is endothermic (absorbing heat). The metal hydride compression system can be used as a unit that can desorb and supply hydrogen at the desired elevated pressure level at constant pressure and smoothly by adding the heat required for desorption.

[0006] The challenges of hydrogen compression include ensuring high heat transfer rates through a single system while maintaining a high level of safety and achieving high pressure ratios. Given the thermodynamic behavior of metal hydride materials, achieving high pressure ratios requires a high temperature range for the system, namely the absorption temperature (T 冷 ) and desorption temperature (T 热 ) is large enough.

[0007] Other challenges involve maximizing overall efficiency. Energy losses associated with transition processes (heating up and cooling down) as well as auxiliary power consumption (pumping power) should also be minimized. Summary of the invention

[0008] In view of the foregoing, an object of the present disclosure is to provide a hydrogen storage and compression system that can achieve a high pressure ratio and is energy-efficient, cost-effective, and safe.

[0009] It would be advantageous to provide a hydrogen storage and compression system that is economical to operate and maintain.

[0010] It would be advantageous to provide a reliable and compact hydrogen storage and compression system.

[0011] The object of the present disclosure is achieved by providing a system having various advantageous features of various embodiments of the present disclosure.

[0012] A hydrogen storage and compression system is disclosed herein, including a hydrogen storage and compression device and a thermal management system. The hydrogen storage and compression device includes a housing and a plurality of storage and compression units mounted in an internal chamber of the housing. Each storage and compression unit includes a container configured for hydrogen storage and compression and a metal hydride contained in the container. The plurality of storage and compression containers are interconnected with a hydrogen inlet and a hydrogen outlet through a hydrogen loop flow system for connection to a hydrogen consuming device and a hydrogen source.

[0013] The thermal management system includes a hot liquid loop system and a heat exchanger system. The hot liquid loop system includes a closed-loop hot liquid flow loop, hot liquid contained in and flowing in the hot liquid flow loop, and a hot liquid pump for pumping the hot liquid in the hot liquid flow loop. The hot liquid flow loop is connected to a hot liquid inlet and a hot liquid outlet of the shell for flowing the hot liquid through an internal chamber of a container of the shell surrounding a storage and compression unit for cooling or heating the storage and compression unit. The hot liquid flow loop is coupled to at least a first heat exchanger and a second heat exchanger, the first heat exchanger being thermally coupled to a heating source, and the second heat exchanger being thermally coupled to a cooling source.

[0014] In one embodiment, the system further comprises a control system connected to the hot liquid circuit system for controlling the flow of the hot liquid in the circuit and through the heat exchanger.

[0015] A significant advantage is that phase changes within the thermal management system are avoided.

[0016] In one embodiment, a thermal management system includes a dry cooler thermally coupled to a hot liquid flow loop.

[0017] In one embodiment, the thermal management system includes one or more additional heat exchangers thermally coupled to the hot liquid flow loop. For example, the additional heat exchangers may include heat exchangers thermally coupled to the industrial process output device for waste heat recovery and / or heat exchangers for free cooling.

[0018] In one embodiment, the hot liquid is selected from any one or more of the following: a water-glycol mixture, silicone oil, or a synthetic hydrocarbon oil.

[0019] In one embodiment, the hot liquid comprises or consists essentially of a water-glycol mixture having a ratio ranging from about 45% water:55% ethylene glycol to about 55% water:45% ethylene glycol. In another embodiment, the ratio is about 50% water:50% ethylene glycol.

[0020] In one embodiment, the metal hydride contained in the storage and compression unit is of the AB2 material class, with a typical composition of TixZryCraMnbFecNidCueVfReg. In this composition, x, y, a, b, c and d are molar ratios, Re is selected from La and Ce; 0.2≤x≤0.95; 0.05≤y≤0.45; 0.001≤a≤1; 0.3≤b≤2; 0.01≤c≤0.6; 0.005≤d≤1.5; 0≤e≤0.1; 0≤f≤0.5; 0.01≤g≤0.05; and a+b+c+d+e+f+g=1.9 to 2.3.

[0021] In one embodiment, the metal hydride contained in the storage and compression unit is of the AB5 material class, with a typical composition of LaxCeyMI(1-xy)NiaCobFecMd. In this composition, x, y, a, b, c and d are molar ratios, wherein MI is at least one element selected from Y, Ti and Zr, and M is selected from Cu and Mn; 0.15≤x≤0.95; 0.05≤y≤0.85; 0≤(1-xy)≤0.1; 3.8≤a≤4.2; 0.1≤b≤1.2; 0.01≤c≤0.3; 0≤d≤0.1; and 4.8≤(a+b+c+d)≤5.15.

[0022] In an embodiment, the housing and the hot liquid flow circuit are configured to withstand an internal pressure of at least 2 bar.

[0023] In one embodiment, a control system is connected to valves in the hydrogen loop flow system and to pressure sensors and temperature sensors connected to the hydrogen loop flow system to control the flow of hydrogen from the hydrogen source into the hydrogen storage and compression system and out of the hydrogen storage and compression system to the hydrogen consuming equipment.

[0024] In one embodiment, each storage and compression container comprises a tubular container wall having a diameter D in the range of about 1.5 cm to 10 cm. Adjacent storage and compression containers of the plurality of storage and compression containers of at least one multi-container unit are separated by a gap G having a length in the range of 0.02×D to 1×D.

[0025] In one embodiment, the diameter D of the tubular container wall of each storage and compression container is in the range of about 2 cm to 8 cm. In one example, the diameter is in the range of about 3 cm to 6 cm.

[0026] In one embodiment, the gap G between the storage and compression containers is in the range of about 0.1×D to 0.5×D.

[0027] In one embodiment, the length of the storage and compression container is in the range of about 60 cm to 200 cm. In one embodiment, the length is in the range of about 80 cm to 150 cm.

[0028] In one embodiment, the hydrogen storage and compression system is used as a near isobaric hydrogen supply system to absorb and desorb hydrogen at elevated pressures. In one embodiment, the elevated pressure is greater than 50 bar. In one embodiment, the elevated pressure is greater than 200 bar. In one embodiment, the system can desorb hydrogen at a substantially constant pressure with minimal temperature variation. In one embodiment, the temperature variation can be less than 40°C. In one embodiment, the temperature variation can be in the range of about 20°C to 30°C. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] Other objects and advantageous features of the present disclosure are apparent from the claims, detailed description and attached drawings, in which:

[0030] Figure 1 is a simplified block diagram of a hydrogen storage and compression system according to an embodiment of the present disclosure;

[0031] Figure 2 is a graph showing the relationship between pressure (bar) and storage capacity (weight percent) of a metal hydride material for a hydrogen storage and compression system according to an embodiment of the present disclosure;

[0032] Figure 3 is a block diagram schematically illustrating a control system of a hydrogen storage and compression system according to an embodiment of the present disclosure;

[0033] Figure 4a is a longitudinal cross-sectional view of a housing and a storage and compression unit of a hydrogen storage and compression system according to an embodiment of the present disclosure; and

[0034] Figure 4b is a transverse cross-sectional view of a housing and a storage and compression unit of a hydrogen storage and compression system according to an embodiment of the present disclosure. DETAILED DESCRIPTION

[0035] When a component, device, element, etc. of the present disclosure is described as having a purpose or performing an operation, function, etc., the component, device, or element should be considered herein as being "configured to" meet the purpose or perform the operation or function. Referring to the drawings, a hydrogen storage and compression system 1 includes a hydrogen storage and compression device 2 and a thermal management system 5.

[0036] The hydrogen storage and compression system 1 is connected to a hydrogen source 101 and a hydrogen consumption device 102. The hydrogen source can be, for example, an electrolytic cell, a hydrogen network connected via a pipeline, a hydrogen trailer, or a low-pressure hydrogen bottle or a high-pressure hydrogen bottle. Other possibilities include hydrogen from a steam methane reforming or biomass gasification plant. The hydrogen consumption device can be a vehicle such as a passenger car, a truck, a bus, or a ship, which uses compressed hydrogen that is usually stored in a high-pressure container and used for a fuel cell or an internal combustion engine. Hydrogen can also be used in a cogeneration cycle or other industrial processes, as a process component (such as ammonia) or for high-temperature heat generation (metal processing).

[0037] Hydrogen is at a high temperature of up to 130°C when it leaves the metal hydride compression system during the desorption process. During the hydrogenation process, the maximum possible temperature inside the high pressure storage tank must comply with certain requirements and safety standards. The hydrogen storage and compression system according to an embodiment of the present disclosure is configured to compress hydrogen at high pressure for filling the hydrogen storage tank of the hydrogen consumer. The pressure is typically greater than 350 bar and may be as high as 900 bar or more, depending on the intended consumer application.

[0038] The hydrogen storage and compression device 2 includes a shell 3 and a plurality of storage and compression units 4 installed in the shell 3. Each storage and compression unit 4 has a container 20 and a metal hydride 22 (usually in the form of powder or granules) contained in the container. The plurality of containers 20 of the plurality of storage and compression units 4 are interconnected by a gas loop flow system 24, which includes gas flow pipes and valves interconnected with a hydrogen source 101 and a hydrogen consuming device 102 via a hydrogen inlet / outlet system passing through the wall of the shell 3. The shell 3 seals and encloses the storage and compression unit 4 and the hydrogen inlet / outlet so that the liquid flowing through the internal chamber 12 of the shell is sealed and contained in the shell and is separated from the external environment around the shell.

[0039] The shell 3 and the storage and compression unit 4 may include a configuration similar to that of the shell and the storage and compression unit described in PCT Publication No. WO 2023025657, except that the shell and the storage and compression unit specifically relate to the thermal management system 5 described herein, the thermal fluid, and the thermal fluid circuit for cooling and heating the storage and compression unit 4 installed in the shell 3.

[0040] The housing 3 surrounds a housing internal chamber 12 in which the storage and compression unit 4 is mounted. The housing includes a hot liquid inlet 16 located on one end and one side of the housing, and includes a hot liquid outlet 18 located at the opposite end and opposite side of the housing 3. Therefore, when the hot liquid 28 flows from the hot liquid inlet 16 to the hot liquid outlet 18, the hot liquid flows around the outside of the container 20 of the storage and compression unit 4. The hot liquid 28 flowing around and passing the outside of the container 20 is used to cool or heat the storage container 4 according to the corresponding requirements of the hydrogen compression process stage and the hydrogen absorption process or the hydrogen desorption process.

[0041] Each storage and compression container 20 may include a tubular container wall having a diameter D in the range of about 1.5 cm to 10 cm. Adjacent storage and compression containers of the plurality of storage and compression containers of at least one multi-container unit may be separated by a gap G having a length in the range of about 0.02×D to 1×D.

[0042] In some embodiments, the diameter D of the tubular container wall of each storage and compression container is in the range of about 2 cm to 8 cm. In one embodiment, the diameter D is in the range of about 3 cm to 6 cm.

[0043] In some embodiments, the gap G between the storage and compression containers is in the range of 0.1×D to 0.5×D.

[0044] In some embodiments, the length of the storage and compression container is in the range of about 60 cm to 200 cm. In one embodiment, the length is in the range of about 80 cm to 150 cm.

[0045] The above parameters allow the hydrogen storage and compression device 2 to have good heat transfer characteristics between the metal hydride in the storage and compression unit and the hot liquid flowing through the internal chamber 12 of the shell 3. The above parameters achieve these effects while allowing the hydrogen storage and compression device 2 to be sized and configured to be easily transported by vehicles (such as trucks, ships and vessels) and easy to install and maintain.

[0046] The thermal management system 5 comprises a heat exchanger system 7 and a hot liquid loop system 6 which interconnects the hot liquid inlet 16 and the hot liquid outlet 18 of the shell 3 with the heat exchanger system 7. The hot liquid loop system 6 has a hot liquid pump 26 for pumping hot liquid through the shell chamber 12 and the heat exchanger system 7, and has a plurality of valves V for controlling the flow of hot liquid 28 through the heat exchanger system 7.

[0047] The heat exchanger system 7 includes at least a first heat exchanger 30a coupled to a heating source 8 and at least a second heat exchanger 30b coupled to a cooling source 9. The heat exchanger system 7 may include additional heat exchangers, such as a heat exchanger 30d for waste heat recovery and a heat exchanger 30e for free cooling. The heat exchange system 7 may also optionally include a dry cooler 30c. A dry cooler (also known as an air-cooled condenser or air-cooled heat exchanger) is a device used in a heat exchanger system that dissipates heat into the surrounding air or absorbs heat from the surrounding air without utilizing the evaporation of water. A dry cooler includes a fin-tube heat exchanger similar to a radiator, in which heat is exchanged between a hot fluid and ambient air.

[0048] In the present disclosure, the dry cooler provides cooling power or heating power in the transition stage of heating or cooling. Specifically, the dry cooler raises the absorption temperature to the ambient temperature and lowers the desorption temperature to the ambient temperature without the need for a cooling machine or a heating machine. Therefore, this reduces the energy consumption of the entire system.

[0049] A plurality of valves V interconnect the hot liquid loop (channel, pipe) system 6 with the corresponding heat exchangers for controlling the flow of the hot liquid through the required heat exchangers according to the process stage and demand. The first heat exchanger 30a coupled to the heating source 8 is configured to heat the hot liquid flowing in the hot liquid loop system 6 to a temperature of 105°C or higher, and in one embodiment to a temperature of 130°C or higher. The second heat exchanger 30b coupled to the cooling source 9 is configured to cool the hot liquid 28 flowing in the hot liquid loop system to a temperature of at least less than -20°C, and in one embodiment to a temperature of less than -30°C.

[0050] In one embodiment, the hot liquid loop system 6 is configured to withstand a pressure of up to 2 bar. Thus, the hot liquid 28 contained within the hot liquid loop system 6 can circulate at a pressure of up to 2 bar and remain in a liquid phase at a temperature of -35°C to +160°C. Exemplary hot liquid compositions are described in more detail below.

[0051] The thermal management system 5 comprises a control system 10 comprising a control unit connected to the hot liquid pump 26 and to the valves V to control the operation of the pump and the various valves during the hydrogen absorption process and the hydrogen desorption process. The control unit is also connected to the heat exchanger system 7 and the temperature sensor T. The control unit is optionally connected to a pressure sensor P for controlling the heating process and the cooling process of the hot liquid flowing in the hot liquid circuit system 6 and through the housing internal chamber 12.

[0052] Pressure sensors and / or temperature sensors may be coupled to the hot liquid 28 located in the housing chamber 12, and additional temperature sensors and / or pressure sensors may be positioned at different locations along the hot liquid circuit system 6. The control unit of the control system 10 is also connected to the hydrogen source 101 and the hydrogen consuming device 102, and is also connected to valves interconnecting the hydrogen storage and compression device 2 with the hydrogen source 101 and the hydrogen consuming device 102, for controlling the inflow and outflow of hydrogen between the hydrogen source 101 and the hydrogen consuming device 102 and the storage and compression unit 4 of the hydrogen storage and compression device 2.

[0053] A thermal management software module is installed in the control unit to manage the control of the pumps, valves, and heat exchanger system according to the heating demand or cooling demand, which depends on the hydrogen absorption process or the hydrogen desorption process and the inlet pressure and outlet pressure between the hydrogen storage and compression unit 4 and the hydrogen source 101 / hydrogen consumer equipment 102.

[0054] By using a hot liquid that can be maintained as a liquid single phase in the temperature range of -30°C to +130°C (typically about -20°C to about 120°C) and circulated in a closed loop that can be coupled to a separate heat exchanger for cooling and heating, the hydrogen storage and compression system is able to operate efficiently, safely, compactly and cost-effectively at high pressures greater than 350 bar and up to about 900 bar. By using a heat exchanger coupled to the closed hot liquid loop, external waste heat or free cooling from an industrial process is also advantageously coupled to allow hydrogen to be compressed in an energy-efficient manner.

[0055] Hot liquid medium

[0056] The basic requirement of the heat medium is to provide a sufficiently high heat transfer rate within the temperature range used, which for suitable materials is -30.0°C to 120°C. It is well known that fluids are more suitable for heat transfer applications than gases due to their higher heat capacity (density, heat capacity) and higher thermal conductivity. For simplicity, phase changes are also avoided. In addition, the heat medium should have a sufficiently low viscosity to be suitable for use in system pumps, and should also have low toxicity, corrosiveness and oxidation potential. When using atmospheric pressure containers, the flash point also becomes relevant, especially when the flash point is in the operating temperature range of the compressor. In this case, appropriate protective measures need to be taken to ensure that any vapor formed can be safely discharged to the atmosphere.

[0057] According to the above requirements, different heat media can be used. In one embodiment, a mixture of water and ethylene glycol mixed in equal proportions (50%:50%) at 1 bar (atmospheric) pressure (or greater) can be used, because the mixture is liquid within a given temperature and pressure range.

[0058] In another embodiment, the hot liquid may be contained in or consist of hot oil in an open housing (not a pressure vessel) at atmospheric conditions. Examples of such hot media include Therminol D-12, silicone oil, or FRAGOLTHERM 620, to name a few. Different grades of hot media may be selected depending on the desired viscosity and heat transfer characteristics. The hot media properties are summarized in the following table:

[0059]

[0060]

[0061] Metal hydride materials

[0062] In one embodiment, the metal hydride contained in the storage and compression unit 4 is of the AB2 material class, with a common composition of TixZryCraMnbFecNidCueVfReg. In this composition, x, y, a, b, c, d, e, f and g are molar ratios, Re is selected from La and Ce; 0.2≤x≤0.95; 0.05≤y≤0.45; 0.001≤a≤1; 0.3≤b≤2; 0.01≤c≤0.6; 0.005≤d≤1.5; 0≤e≤0.1; 0≤f≤0.5; 0.01≤g≤0.05; and a+b+c+d+e+f+g=1.9 to 2.3.

[0063] In another embodiment, the metal hydride contained in the storage and compression unit 4 is an AB5 material class, and its common composition is LaxCeyMI(1-xy)NiaCobFecMd. In this composition, x, y, a, b, c and d are molar ratios, wherein MI is at least one element selected from Y, Ti and Zr, and M is selected from Cu and Mn; 0.15≤x≤0.95; 0.05≤y≤0.85; 0≤(1-xy)≤0.1; 3.8≤a≤4.2; 0.1≤b≤1.2; 0.01≤c≤0.3; 0≤d≤0.1; and 4.8≤(a+b+c+d)≤5.15.

[0064] Within the scope of the present disclosure, hydrogen storage metals are not limited to AB2 materials or AB5 materials, but may also be applied to other classes of materials with similar thermochemical behaviors.

[0065] Examples of processes for industrial applications

[0066] A hydrogen storage and compression system operating in a full cycle may include the following stages in the order shown. These stages may include: (i) absorption; (ii) temperature increase; (iii) desorption; and (iv) temperature reduction. Examples of these processes are described in more detail below. The values ​​shown correspond to an embodiment in which the hot liquid consists of a water-ethylene glycol mixture mixed in equal proportions (50%:50%) at 1 bar (atmospheric) pressure.

[0067] absorb

[0068] Hydrogen is absorbed from an external source into the storage and compression unit 4 in an almost isobaric process. 2 The pressure of the source is typically in the range of 25 bar (atmosphere) to 40 bar (atmosphere), and 35 bar (atmosphere) is most common for common electrolytic cells. Since the absorption reaction is highly exothermic (causing the release of heat), the storage and compression unit 4 needs to be cooled to keep the resulting pressure below the hydrogen charging pressure. The cooling power provided is also needed to compensate for the inevitable warming caused by the environment, which will generally also increase the hydrogen pressure in the resulting storage and compression unit. This energy requirement is mainly related to the metal hydride material absorption enthalpy, which for suitable materials is 18.0 kJ / mol. H2 , the resulting energy demand is 87kWh th or about 2.7kWh th / kg H2 (Both values ​​include temperature rise compensation energy).

[0069] The time required for the absorption process depends on the H 2 source type and can vary from 1 hour to 8 hours, where the cooling power generated is 10.9kW th Up to 87kW th For suitable metal hydride materials, the compressor inlet fluid temperature is usually between -30°C and -0°C, with common values ​​of -25.0°C to -20°C. A common cooling flow rate is 7.5m 3 / h. The hot liquid flows through the cooling heat exchanger 30a and bypasses the dry cooler 30c and the heating heat exchanger 30b. It should be noted that since the exothermic reaction produces an inverse parabolic temperature characteristic distribution in the metal hydride, the inlet temperature is lower than the temperature corresponding to the absorption pressure on the material PCT (pressure-capacity-temperature) curve.

[0070]

[0071]

[0072] Desorption

[0073] During the desorption process, hydrogen is released from the hydrogen storage and compression device 2 to a hydrogen consuming device 102, such as a hydrogen-powered vehicle (i.e., a truck or bus), which requires hydrogenation at a pressure of 350 bar or greater. The desorption pressure can be adjusted by the choice of materials and the temperature of the heat medium. The time required for the vehicle to be hydrogenated determines the desorption rate of the hydrogen. The hydrogenation time can vary from a few minutes (e.g., 5 minutes to 15 minutes) to several hours (e.g., 3 hours to 8 hours). The desorption pressure of the storage and compression unit 4 is related to the final mass delivered, the desorption mass flow rate, and the temperature of the hydrogen before entering the hydrogen-powered vehicle. As an example, for a vehicle such as a vehicle with 6 kgH 2 / h slow hydrogenation application, for modern Xcient trucks (32kgH 2 ), the resulting hydrogenation time is 5 hours and 20 minutes and the temperature of the hydrogen after passing through the hydrogen cooler is -25.0°C, and the desorption pressure is 370 bar. This situation is advantageous because the cooling source of the metal hydride compressor thermal management system can be directly used for hydrogen cooling. Other flow rates are also possible by increasing the desorption pressure and / or also reducing the hydrogen temperature.

[0074] Maintain hot liquid flow at 7.5m 3 / h (as in the case of absorption) would result in a required inlet temperature of 110°C to achieve a desorption pressure of 370 bar for the given material. At a desorption enthalpy of 20.0 kJ / mol H2 In order to compensate for the cooling effect of desorption and to counteract the heat loss to the environment, the total energy requirement is 110.8 kWh. th or about 3.5kWh th / kgH 2 During this phase, the hot liquid flows through the heating heat exchanger 30b and bypasses the dry cooler 30c and the cooling heat exchanger 30a. Considering the desorption duration and the energy requirements of this phase, the heater needs to deliver 20.8 kW th of power.

[0075]

[0076] Warming up

[0077] After the absorption process is completed, the storage and compression unit 4 is heated from the absorption temperature (-25.0°C) to the desorption temperature (110°C) because the hot liquid initially flows through the dry cooler 30c and finally flows through the heating heat exchanger 30b. While heating, the internal pressure of the storage and compression unit 4 increases to 370 bar. During the initial stage of heating, the flow through the dry cooler 30c enables the temperature of the storage and compression unit 4 to be raised from the absorption temperature to the ambient temperature. This energy is essentially provided free. However, a certain amount of pumping power is required to allow the liquid to flow through the dry cooler 30c. The total energy required for heating is 5.4 kWh th / kgH 2 (172.8kWh th ), of which 1.7kWh th / kgH 2 (55.1kWh th ) is provided by the dry cooler 30c, and the remaining energy 3.7kWh th / kgH 2 (117.7kWh th ) is provided by the heating heat exchanger 30b. During the heating process, the flow rate is 7.5m 3 / h.

[0078] To simplify the system, it is assumed that the same heating heat exchanger 30b is used as for desorption. If the same electrical energy is supplied to the heating heat exchanger 30b, the thermal power will vary and depend on the coefficient of performance in this temperature range. The duration of the warm-up phase is approximately 5 hours and 20 minutes.

[0079]

[0080] Cooling

[0081] After desorption is completed, the storage and compression unit 4 is cooled from the desorption temperature (110.0°C) to the absorption temperature (-25.0°C). Similar to the warming up, all or most of the flow is initially directed through the dry cooler 30c to cool using the freely available environment. When the ambient temperature is reached, the flow is directed through the cooling heat exchanger 30a to cool again to the absorption temperature. The total energy required for the cool down is 4.7 kWh th / kgH 2 (149.2kWh th ), of which 3.2kWh th / kgH 2 (101.5kWh th ) is provided by the dry cooler 30c, and the remaining energy 1.5kWh th / kgH2 (47.7kWh th ) is provided by the cooling heat exchanger 30a. During the cooling process, the flow rate is 7.5m 3 / h.

[0082] The same cooling heat exchanger can be used for cooling, thus making the duration of this phase 2 hours and 11 minutes.

[0083]

[0084] Examples of industrial applications

[0085] In one application, the hydrogen storage and compression system can be advantageously used as a system for refueling hydrogen-powered vehicles such as trucks or buses, which requires a refueling level of 350 bar. In this application, by selectively adjusting the heating power, the outlet pressure is usually gradually increased to a pressure slightly exceeding the tank to be refueled (e.g., more than 10 bar). In this application, common desorption times can be as low as 5 minutes to 15 minutes. In other cases, the desorption time can be 60 minutes or even 180 minutes or longer. In this application, common inlet pressures are in the range of 25 bar (atmosphere) to 35 bar (atmosphere). Common cooling temperatures are in the range of -15°C to -30°C. Common heating temperatures are in the range of 90°C to 130°C.

[0086] In another application, the hydrogen storage and compression system can be advantageously used as a system for hydrogenating hydrogen-powered vehicles such as heavy vehicles or light vehicles, which requires a hydrogenation level of 700 bar. In this application, by selectively adjusting the heating power, the outlet pressure is usually gradually increased to a pressure slightly exceeding the tank to be hydrogenated (e.g., more than 10 bar). In this application, common desorption times can be as low as 5 minutes to 15 minutes. In other cases, the desorption time can be 60 minutes or even 180 minutes or longer. In this application, common inlet pressures are in the range of 150 bar (atmosphere) to 350 bar (atmosphere). Common cooling temperatures are in the range of 5°C to -30°C. Common heating temperatures are in the range of 60°C to 130°C.

[0087] In another application, the hydrogen storage and compression system can be advantageously used as a system for adding hydrogen to a trailer for transport or storage of hydrogen, which requires a hydrogenation level of 200 bar. In this application, by selectively adjusting the heating power, the outlet pressure is usually gradually increased to slightly exceed the pressure of the tank to be hydrogenated (e.g., more than 10 bar). In this application, common desorption times can be as low as 60 minutes. In other cases, the desorption time can be 180 minutes or even 300 minutes or longer. In this application, common inlet pressures are in the range of 25 bar (atmosphere) to 35 bar (atmosphere). Common cooling temperatures are in the range of -15°C to -30°C. Common heating temperatures are in the range of 90°C to 130°C.

[0088] List of reference numbers used

[0089] Hydrogen Source 101

[0090] Hydrogen consumption equipment 102

[0091] Hydrogen storage and compression systems1

[0092] Hydrogen storage and compression equipment 2

[0093] Shell 3

[0094] The inner chamber 12 of the housing

[0095] Hydrogen inlet / hydrogen outlet 14

[0096] Hot liquid inlet 16

[0097] Hot liquid outlet 18

[0098] Storage and compression unit 4

[0099] Container 20

[0100] Metal hydride 22

[0101] Gas loop flow system 24

[0102] Thermal Management System5

[0103] Hot liquid circuit system 6

[0104] Hot liquid pump 26

[0105] Hot Liquid 28

[0106] Heat exchanger system7

[0107] First heat exchanger 30a

[0108] Second heat exchanger 30b

[0109] Heating source 8

[0110] Cooling source 9

[0111] Control system 10

[0112] Pressure sensor P

[0113] Temperature sensor T

[0114] Valve V

[0115] Storage and compression container diameter D

[0116] Gap distance between adjacent containers

[0117] The length of the container is L

Claims

1. A hydrogen storage and compression system comprising: Hydrogen storage and compression equipment; Thermal management system; as well as Control systems, wherein the hydrogen storage and compression device comprises a shell and a plurality of storage and compression units installed in an internal chamber of the shell, wherein each of the storage and compression units comprises a storage and compression container configured for hydrogen storage and compression and a metal hydride contained in the storage and compression container, wherein the plurality of storage and compression containers are interconnected with a hydrogen inlet and a hydrogen outlet through a hydrogen loop flow system for respective connection to a hydrogen source and a hydrogen consuming device, Wherein, the thermal management system includes a hot liquid circuit system and a heat exchanger system, Wherein, the hot liquid circuit system comprises: - Closed hot liquid flow circuit, - a hot liquid contained and flowing within the hot liquid flow circuit; and - a hot liquid pump for pumping said hot liquid in said hot liquid flow circuit, Wherein, the hot liquid flow circuit: a hot liquid inlet and a hot liquid outlet connected to the housing for flowing the hot liquid through an internal chamber of the housing, the internal chamber of the housing surrounding the storage and compression container of the storage and compression unit, for cooling or heating the storage and compression unit, and coupled to at least a first heat exchanger and a second heat exchanger, the first heat exchanger being thermally coupled to a heating source and the second heat exchanger being thermally coupled to a cooling source, and wherein the control system is connected to the hot liquid loop system for controlling the flow of the hot liquid in the hot liquid flow loop and through the first heat exchanger and the second heat exchanger.

2. The hydrogen storage and compression system according to claim 1, wherein: The thermal management system includes a dry cooler thermally coupled to the hot liquid flow loop.

3. The hydrogen storage and compression system according to claim 1, wherein: The thermal management system includes one or more additional heat exchangers thermally coupled to the hot liquid flow loop.

4. The hydrogen storage and compression system according to claim 3, wherein: One or more of the additional heat exchangers include: A heat exchanger thermally coupled to an industrial process output device for waste heat recovery; and / or Heat exchanger for free cooling.

5. The hydrogen storage and compression system according to claim 1, wherein: The hot liquid is selected from any one or more of the following: a water-glycol mixture, silicone oil, and a synthetic hydrocarbon oil.

6. The hydrogen storage and compression system according to claim 1, wherein: The hot liquid comprises a water-ethylene glycol mixture, wherein the ratio of water to ethylene glycol is in the range of 45%:55% to 55%:45%, or 50%:50%.

7. The hydrogen storage and compression system according to claim 1, wherein: The metal hydride contained in the storage and compression unit is of the AB2 material category with a composition of TixZryCraMnbFecNidCueVfReg, wherein x, y, a, b, c, d, e, f and g are molar ratios, Re is selected from La and Ce; 0.2≤x≤0.95; 0.05≤y≤0.45; 0.001≤a≤1; 0.3≤b≤2; 0.01≤c≤0.6; 0.005≤d≤1.5; 0≤e≤0.1; 0≤f≤0.5; 0.01≤g≤0.05; and a+b+c+d+e+f+g=1.9 to 2.

3.

8. The hydrogen storage and compression system according to claim 1, wherein: The metal hydride contained in the storage and compression unit is of the AB5 material category and has a composition of LaxCeyMI(1-xy)Nia CobFecMd, wherein x, y, a, b, c and d are molar ratios, wherein MI is at least one element selected from Y, Ti and Zr, and M is selected from Cu and Mn; 0.15≤x≤0.95; 0.05≤y≤0.85; 0≤(1-xy)≤0.1; 3.8≤a≤4.2; 0.1≤b≤1.2; 0.01≤c≤0.3; 0≤d≤0.1; 4.8≤(a+b+c+d)≤5.

15.

9. The hydrogen storage and compression system according to claim 1, wherein: The housing and the hot liquid flow circuit are configured to withstand an internal pressure of at least 2 bar.

10. The hydrogen storage and compression system of claim 1, wherein: The control system is connected to valves in the hydrogen loop flow system and to pressure sensors and temperature sensors connected to the hydrogen loop flow system to control the flow of hydrogen from the hydrogen source into the hydrogen storage and compression system and out of the hydrogen storage and compression system to the hydrogen consuming equipment.

11. The hydrogen storage and compression system of claim 1, wherein: Each of the storage and compression containers comprises a tubular container wall, a diameter D of which is in the range of 1.5 cm to 10 cm, and wherein adjacent storage and compression containers among the plurality of storage and compression containers of at least one multi-container unit are separated by a gap G, a length of which is in the range of 0.02×D to 1×D.

12. The hydrogen storage and compression system of claim 11, wherein: The diameter D of the tubular container wall of each of the storage and compression containers is in the range of 2 cm to 8 cm, or in the range of 3 cm to 6 cm.

13. The hydrogen storage and compression system of claim 11, wherein: The gap G between the storage and compression containers is in the range of 0.1×D to 0.5×D.

14. The hydrogen storage and compression system of claim 11, wherein: The length of the storage and compression container is in the range of 60 cm to 200 cm or in the range of 80 cm to 150 cm.

15. A hydrogen storage and compression system according to claim 1, wherein the hydrogen storage and compression system is used as a near-isobaric hydrogen supply system to absorb and desorb hydrogen at an elevated pressure of greater than 50 bar or greater than 200 bar, and the hydrogen storage and compression system desorbs hydrogen at a substantially constant pressure with a temperature variation of less than 40°C or a temperature variation within the range of 20°C to 30°C.

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