KR20220128567A - On-site Hydrogen filling station - Google Patents

Abstract

The present invention relates to an ammonia-based on-site hydrogen filling station and, more specifically, to an ammonia-based on-site hydrogen filling station capable of producing hydrogen by using liquefied ammonia and supplying hydrogen to a place requiring hydrogen. The ammonia-based on-site hydrogen filling station comprises: an ammonia storage tank unit (100) storing liquid ammonia; a hydrogen production unit (200) producing hydrogen by using liquid ammonia supplied from the ammonia storage tank unit (100); a hydrogen storage unit (300) storing hydrogen produced by the hydrogen production unit (200); and a dispenser unit (400) connected to external equipment requiring hydrogen filling to supply hydrogen stored in the hydrogen storage unit (300) to the external equipment.

Description

Ammonia-based On-site Hydrogen filling station

The present invention relates to an ammonia-based on-site hydrogen charging station, and more particularly, to an ammonia-based on-site hydrogen charging station that can produce hydrogen using liquefied ammonia and supply it to a required place.

Recently, the problem of global warming due to the indiscriminate use of fossil fuels is emerging. Accordingly, various studies on the production and utilization of hydrogen (H2) as a clean energy source are being actively conducted.

When a fuel cell is operated using hydrogen, energy conversion efficiency can be expected to be two to three times higher than that of an existing internal combustion engine. is becoming

On the other hand, hydrogen production technology is representative of fossil fuel-based byproduct hydrogen, extracted hydrogen, and renewable energy-based water electrolysis hydrogen.

As a facility for transporting hydrogen as energy to general life infrastructure, hydrogen charging stations can be largely divided into two types, off-site type and on-site type, depending on the method of supplying hydrogen.

First, the off-site hydrogen charging station is a method of transporting hydrogen produced in other regions to the hydrogen charging station and supplying it.

Off-site hydrogen charging stations are divided into pipeline supply type hydrogen charging stations and tube trailer supply type hydrogen charging stations according to the transport method.

Currently, the most common hydrogen refueling station is a tube trailer supply method, which incurs transportation costs, but has the advantage of not incurring equipment investment costs for transportation infrastructure, but requires a lot of space, and the hydrogen storage capacity is 200kg to 400kg. Since there is a limit to charging only 80 hydrogen vehicles per day, the hydrogen tank needs to be replaced frequently, which has a problem in that the operating cost of hydrogen transportation and replacement is high.

On the other hand, the on-site hydrogen refueling station produces and supplies hydrogen directly from the hydrogen refueling station.

On-site hydrogen refueling stations are divided into natural gas extraction (reforming) hydrogen refueling stations and water electrolysis hydrogen refueling stations according to the production method of hydrogen. In the case of a natural gas extraction hydrogen charging station, hydrogen can be produced using the established natural gas supply line, so the transportation and storage cost of hydrogen is low. There is a problem in that ancillary costs are high to create a high-temperature environment, and since fossil fuels (natural gas) are used, CO2 is generated (safety costs and explosion risks exist as explosive gases).

An object of the present invention is to provide an ammonia-based on-site hydrogen charging station capable of producing hydrogen using ammonia and supplying it to a necessary place in order to solve the above problems.

The present invention was created to achieve the object of the present invention as described above, and an ammonia storage tank unit 100 for storing liquid ammonia, and hydrogen produced by using the liquid ammonia supplied from the ammonia storage tank unit 100 The hydrogen production unit 200, the hydrogen storage unit 300 for storing the hydrogen produced by the hydrogen production unit 200, and the hydrogen stored in the hydrogen storage unit 300 are connected to external equipment that requires hydrogen charging. Disclosed is an ammonia-based on-site hydrogen charging station comprising a dispenser unit 400 for supplying external equipment.

The ammonia storage tank unit 100 may be installed in an underground space (B) separated from the ground by being surrounded by a protective wall (2) on all sides below the ground.

The ammonia storage tank unit 100 communicates with the storage tank 110 in which the liquid ammonia located in the underground space B is stored, and the liquid ammonia supply unit 10, and supplies the liquid ammonia to the storage tank 110. It may include a liquid ammonia inlet pipe 120 for introducing the liquid ammonia, and a liquid ammonia outlet pipe 130 communicating with the hydrogen production unit 200 and discharging the liquid ammonia from the storage tank 110 .

The ammonia storage tank unit 100 includes a leak detection unit 140 for detecting whether the storage tank 110 is leaking, and vapor phase ammonia to the underground space B when a leak occurs in the storage tank 110 . It may further include a solvent spraying unit 150 for spraying the solvent 23 that can be dissolved.

The ammonia storage tank unit 100 may further include at least one sensor 160 for measuring at least one of a temperature and a pressure inside the storage tank 110 .

The ammonia storage tank unit 100 may further include a temperature control unit 170 installed outside the storage tank 110 to control the temperature of the liquid ammonia.

The hydrogen production unit 200 includes a vaporizer 210 that receives liquid ammonia stored in the ammonia storage tank unit 100 and vaporizes it into vapor phase ammonia, and decomposes vapor phase ammonia vaporized in the vaporizer 210 into nitrogen and hydrogen. a reactor 220, an adsorber 230 for adsorbing unreacted ammonia among the mixed gas passing through the reactor 220, and a separator 240 for separating hydrogen from the mixed gas passing through the adsorber 230. may include

The hydrogen production unit 200 is installed between a heating unit 250 for heating the gaseous ammonia in the reactor 220 and the reactor 220 and the adsorber 230 to recover the heat of the mixed gas. A heat exchanger 260 may be further included.

The hydrogen production unit 200 includes an ammonia distributor 270 for distributing at least a portion of the vapor phase ammonia that has passed through the vaporizer 210 to the heating unit 250 and the reactor 220, respectively, and the separator 240 ) may further include a hydrogen distributor 280 for distributing at least a portion of the separated hydrogen to the heating unit 250 and the hydrogen storage unit 300 , respectively.

The hydrogen production unit 200, the ammonia and hydrogen supplied to the heating unit 250 through the ammonia distributor 270 and the hydrogen distributor 280 is burned, and then the generated exhaust gas is the heat source of the separator 240 . It may further include an exhaust gas transport line 292 for use as.

The vaporizer 210 includes a first flow path P1 through which a fluid exchanging heat with liquid ammonia passing through the vaporizer 210 flows, and the heat exchanger 260 passes through the heat exchanger 260 . A second flow path P2 through which a fluid exchanging heat with the mixed gas flows may be included.

The hydrogen production unit 200, a fluid circulation line 294 for circulating communication between the first flow path P1 and the second flow path P2, and the fluid circulation line 294 to circulate the fluid along the fluid circulation line 294 A circulation pump 296 installed in the line 294 may be further included.

In the present invention, the ammonia-based on-site hydrogen charging station uses ammonia to produce and supply hydrogen without CO ₂ generation, thereby minimizing the transportation and storage cost of hydrogen and has the advantage of producing and supplying eco-friendly hydrogen.

1 is a block diagram showing an ammonia-based on-site hydrogen charging station according to the present invention.
FIG. 2 is a conceptual view showing an ammonia storage tank unit of the hydrogen filling station of FIG. 1 .
3 is a block diagram showing a hydrogen production unit of the hydrogen charging station of FIG. 1 .
4 to 6 are conceptual views illustrating a part of the configuration of FIG. 3 .
7 is a conceptual diagram showing a hydrogen storage unit and a dispenser unit of the hydrogen charging station of FIG. 1 .

Hereinafter, an ammonia-based on-site hydrogen charging station according to the present invention will be described in detail with reference to the accompanying drawings.

The ammonia-based on-site hydrogen charging station according to the present invention, as shown in FIGS. 1 to 7 , includes an ammonia storage tank unit 100 for storing liquid ammonia, and the ammonia storage tank unit 100 supplied from A hydrogen production unit 200 for producing hydrogen using liquid ammonia, a hydrogen storage unit 300 for storing the hydrogen produced by the hydrogen production unit 200, and external equipment requiring hydrogen charging are connected to the hydrogen storage unit ( 300) and a dispenser unit 400 for supplying the hydrogen stored in the external equipment.

The ammonia storage tank unit 100 is configured to store liquid ammonia, and various configurations are possible.

Ammonia is toxic and is a substance that can have a fatal effect on the human body when leaked, so it is necessary to have a safety device for storing and handling liquid ammonia.

Accordingly, the ammonia storage tank unit 100 may be installed in an underground space (B) separated from the ground by being surrounded by a protective wall (2) on all sides below the ground (G) in order to safely store liquid ammonia, which is a liquid dangerous substance. have.

More specifically, the ammonia storage tank unit 100 communicates with the storage tank 110 for storing liquid ammonia located in the underground space B, and the liquid ammonia supply unit 10, and the storage tank 110. It may include a liquid ammonia inlet pipe 120 for introducing liquid ammonia into the furnace, and a liquid ammonia outlet pipe 130 communicating with the hydrogen production unit 200 and draining the liquid ammonia from the storage tank 110 .

The storage tank 110, a tank for storing liquid ammonia, is located in the underground space B surrounded by the protective wall 2 and may be configured in various shapes and sizes according to specifications.

The storage tank 110 may be configured as a double jacket type for installing a temperature control unit 170 to be described later.

The liquid ammonia inlet pipe 120 is a pipe for supplying liquid ammonia to the storage tank 110 , and may communicate with the liquid ammonia supply unit 10 on the ground.

The liquid ammonia supply unit 10 is a facility for supplying liquid ammonia to the storage tank 110 , and as shown in FIG. 1 , may be configured as a transport vehicle using a tank lorry container.

At this time, the liquid ammonia supply unit 10 is moved to the liquid ammonia supply position set on the ground above the underground space (B) where the storage tank 110 is installed, and the liquid ammonia inlet pipe 120 of the storage tank 110 is located. ) and then to provide liquid ammonia to the storage tank 110 .

One or more valves 12 for controlling the supply of liquid ammonia may be installed in the liquid ammonia inlet pipe 120 between the liquid ammonia supply 10 and the storage tank 110 .

The liquid ammonia outlet pipe 130 is a pipe for supplying the liquid ammonia stored in the storage tank 110 to the hydrogen production unit 200 to be described later. Various configurations are possible, and the liquid ammonia supply to the hydrogen production unit 200 is provided. One or more valves 132 for regulating may be installed.

In addition, the ammonia storage tank unit 100 has a leak detection unit 140 for detecting whether the storage tank 110 is leaking, and when a leak occurs in the storage tank 110, the vapor rises to the underground space (B). It may further include a solvent spraying unit 150 for spraying a solvent capable of dissolving ammonia.

The leak detection unit 140 is configured to detect whether the storage tank 110 is leaking, and various configurations are possible.

For example, the leak detection unit 140 may be an ammonia detector installed in the underground space (B) to detect the concentration of ammonia in the underground space (B). At this time, when the ammonia concentration detected by the leak detection unit 140 exceeds a preset standard, a leak occurs in the storage tank 110 and it may be determined that ammonia has leaked.

The solvent spraying unit 150 is configured to spray the solvent 23 capable of dissolving vapor phase ammonia into the underground space (B) when a leak occurs in the storage tank 110 , and various configurations are possible.

The solvent injection unit 150 includes a solvent storage unit 20 for storing the solvent 23 to be sprayed into the underground space B, and a flow path through which the solvent 23 flows, which is installed on the upper side of the underground space B. It may include a solvent flow path 152 to be formed, and one or more injection ports 154 provided in the solvent flow path 152 and through which a flow path flowing along the solvent flow path 152 is injected.

The solvent storage unit 20 is a storage unit in which the solvent 23 is stored, and various configurations are possible and may be installed on the ground.

The solvent flow path 152 is a flow path through which the solvent 23 communicates with the solvent storage unit 20 and the connection pipe 156, and can have various shapes and is installed in various patterns on the upper side of the underground space (B). can be

One or more valves 22 for controlling the flow of the solvent 23 may be installed between the solvent storage unit 20 and the solvent flow path 152 .

The injection holes 154 are preferably formed in a plurality of solvent passages 152 along the solvent passages 152 . In addition, a nozzle for smoothly spraying the solvent 23 may be installed in the injection hole 154 .

Here, the solvent 23 is a material for dissolving gaseous ammonia in the underground space B, and may be composed of various materials such as water or a neutralizing agent.

When the solvent 23 is injected through the injection hole 154, the gaseous ammonia in the underground space B is dissolved, so that the ammonia concentration in the underground space B is reduced below the standard, thereby ensuring safety.

In addition, the ammonia storage tank unit 100 may further include at least one sensor 160 for measuring at least one of temperature and pressure inside the storage tank 110 .

More preferably, the ammonia storage tank unit 100 may include a sensor 160 for measuring the internal temperature of the storage tank 110 and a sensor 160 for measuring the internal pressure, respectively.

Through the sensor 160, it is possible to maintain the environment in the storage tank 110 so that the temperature and pressure inside the storage tank 110 are maintained in an appropriate state, thereby stably operating the facility, risk can be minimized.

To this end, the ammonia storage tank unit 100 may further include a temperature control unit 170 installed outside the storage tank 110 to control the temperature of the liquid ammonia.

The temperature control unit 170 is configured to control the temperature of the storage tank 110, and various configurations are possible.

For example, the temperature control unit 170 may be a refrigerant passage that is installed in various shapes and patterns on the outer surface of the storage tank 110 and a refrigerant flows therein.

The temperature control unit 170 may be installed on the outer wall of the storage tank 110 when the storage tank 110 has a double jacket structure. The temperature control unit 170 may allow ammonia to be stored in a liquid state at normal pressure through refrigerant circulation.

At this time, the temperature control unit 170 may be installed on the ground and coupled with the refrigerant circulation device 30 for refrigerant circulation.

The refrigerant circulation device 30 communicates with the temperature control unit 170 so that the refrigerant circulates along the temperature control unit 170 and includes a pair of circulation passages 34 through which the refrigerant flows in and out. One or more valves 31 for controlling the circulation of the refrigerant may be provided in each of the circulation passages 34 .

The hydrogen production unit 200 is configured to produce hydrogen using the liquid ammonia supplied from the ammonia storage tank unit 100, and various configurations are possible.

The hydrogen production unit 200 may be installed on the ground, and between the hydrogen production unit 200 and the ammonia storage tank unit 100 is connected to the liquid ammonia outlet pipe 130 to store the liquid ammonia in the storage tank 110. An ammonia transport pump 60 for transporting to the production unit 200 may be installed.

At least one valve 62 for controlling the transfer of liquid ammonia may be installed at at least one before and after the ammonia transfer pump 62 .

The hydrogen production unit 200 includes a vaporizer 210 that receives liquid ammonia stored in the ammonia storage tank unit 100 and vaporizes it into vapor phase ammonia, and a reactor that decomposes vapor phase ammonia vaporized in the vaporizer 210 into nitrogen and hydrogen. 220 , an adsorber 230 for adsorbing unreacted ammonia among the mixed gas passing through the reactor 220 , and a separator 240 for separating hydrogen from the mixed gas passing through the adsorber 230 . .

The vaporizer 210 may be configured in various configurations to vaporize the liquid ammonia transferred from the storage tank 110 into gaseous ammonia.

The liquid ammonia flowing into the vaporizer 210 may be vaporized into vapor phase ammonia by heating the liquid ammonia in the vaporizer 210 at a low temperature of 0°C to 3°C.

Liquid ammonia heating in the vaporizer 210 can be utilized in various ways, for example, the vaporizer 210, the vaporizer 210, the first flow path (P1) through which the fluid that exchanges heat with the liquid ammonia passing through the vaporizer 210 flows. ) may be included.

In this case, the high-temperature fluid may move along the first flow path P1 to vaporize the liquid ammonia in the vaporizer 210 .

Gas-phase ammonia vaporized through the vaporizer 210 may be injected into the reactor 220 .

The reactor 220 is configured to decompose gaseous ammonia vaporized in the vaporizer 210 into nitrogen and hydrogen, and various configurations are possible if hydrogen can be produced through ammonia.

For example, the reactor 220 may include an ammonia decomposition catalyst layer 222 that decomposes ammonia into nitrogen and hydrogen.

The ammonia decomposition catalyst layer 222 may include both a metal and a non-metal catalyst, and is not limited to a specific material.

On the other hand, the ammonia decomposition through the ammonia decomposition catalyst layer 222 is preferably performed in a rather high temperature environment.

Accordingly, the hydrogen production unit 200 may further include a heating unit 250 for heating the vapor phase ammonia in the reactor 220 .

The heating unit 250, various heat sources may be applied as long as the gaseous ammonia in the reactor 220 can be heated, and for example, may be configured as a combustor that generates heat by burning a raw material.

The heating unit 250 may be a combustor that is combusted using hydrogen as a raw material, but more specifically, may be a combustor using a gas in which hydrogen and ammonia are mixed for stable heat generation.

A fuel supply method to the heating unit 250 will be described later.

Through the reactor 220 , a mixed gas including nitrogen and oxygen in which ammonia is decomposed and unreacted ammonia that does not react with the ammonia decomposition catalyst layer 222 may be generated.

The mixed gas including nitrogen, oxygen, and unreacted ammonia that has passed through the reactor 220 may be injected into the adsorber 230 .

The adsorber 230 is configured to adsorb unreacted ammonia among the mixed gas that has passed through the reactor 220 , and various configurations are possible.

However, the mixed gas that has passed through the reactor 220 is in a high temperature state, but adsorption of unreacted ammonia through the adsorber 230 is not performed well in a high temperature environment.

Accordingly, the hydrogen production unit 200 is installed between the reactor 220 and the adsorber 230 to lower the temperature of the mixed gas that has passed through the reactor 220 to a temperature suitable for adsorption of unreacted ammonia. It may further include a heat exchanger 260 to recover the.

At this time, the mixed gas including nitrogen, oxygen, and unreacted ammonia that has passed through the reactor 220 is not directly injected into the adsorber 230 , but is injected into the heat exchanger 260 to complete heat exchange and then the adsorber 230 . ) is injected.

The heat exchanger 260 may use various heat exchange methods as long as the heat of the mixed gas can be recovered.

For example, the heat exchanger 260 may include a second flow path P2 through which a fluid that exchanges heat with the mixed gas passing through the heat exchanger 260 flows.

In this case, the relatively low temperature fluid moves along the second flow path P2 , and heat of the mixed gas in the heat exchanger 260 may be recovered.

At this time, the hydrogen production unit 200 includes a fluid circulation line 294 and a fluid circulation line 294 for circulating communication between the first flow path P1 of the vaporizer 210 and the second flow path P2 of the heat exchanger 260 . ) may further include a circulation pump 296 installed in the fluid circulation line 294 to circulate the fluid along.

Through this, the high-temperature fluid (eg, steam) flowing along the second flow path P2 and recovering the heat of the mixed gas is transferred to the first flow path P1 along the fluid circulation line 294 and the vaporizer 210 of liquid ammonia can be heated. The fluid from which heat is recovered to liquid ammonia through the vaporizer 210 (eg, a state in which steam is deprived of heat and liquefied) is again transferred to the second flow path P2 along the fluid circulation line 294 and is a mixed gas of high temperature. of heat can be recovered.

The mixed gas (eg, 25° C. or less) from which heat is recovered by passing through the heat exchanger 260 may be injected into the above-described adsorber 230 .

The adsorber 230 may include two or more adsorption modules 230a and 230b connected in parallel to each other, as shown in FIG. 5 .

For example, the adsorber 230 includes a first adsorption module 230a , a second adsorption module 230b connected in parallel, and a plurality of valves for controlling the flow direction of the mixed gas in the adsorber 230 . (V1, V2, V3, V4, V5, V6, V7, V8).

In this case, the first adsorption module 230a and the second adsorption module 230b may be used alternately for continuous ammonia adsorption.

That is, while the first adsorption module 230a among the adsorption modules 230a and 230b adsorbs unreacted ammonia in the mixed gas, the other second adsorption module 230b is prepared for adsorption of unreacted ammonia. can be regenerated (or replaced) as

For example, while the first adsorption module 230a adsorbs unreacted ammonia, the first valve V1, the third valve V3, the fourth valve V4, and the sixth valve V6 are opened to open the first The mixed gas passing through the adsorption module 230a may be injected into a separator 240 to be described later.

In this case, the second valve V2, the fifth valve V5, the seventh valve V7, and the eighth valve V8 may maintain a closed state.

As unreacted ammonia adsorption proceeds in the first adsorption module 230a, when the first adsorption module 230a is saturated after a certain time has elapsed, the second valve V2, the fifth valve V5, The seventh valve V7 and the eighth valve V8 may be opened to inject the mixed gas into the second adsorption module 230b.

At this time, the first valve V1, the third valve V3, the fourth valve V4, and the sixth valve V6 are closed, so that regeneration (or replacement) of the first adsorption module 230a may be performed.

That is, it is possible to continuously adsorb unreacted ammonia through the first adsorption module 230a and the second adsorption module 230b without interruption.

In the case of FIG. 5 , the adsorber 230 has been described focusing on an embodiment including two adsorption modules 230a and 230b connected in parallel to each other, but the adsorber 230 includes a single adsorption module or system capacity. Of course, an embodiment including three or more adsorption modules connected in various ways, such as series and parallel, is also possible.

The mixed gas (including nitrogen and hydrogen) passing through the first adsorption module 230a or the second adsorption module 230b may be injected into the separator 240 .

At this time, between the adsorber 230 and the separator 240, a first compressor 70 for compressing the mixed gas passing through the adsorber 230 to a high pressure so that hydrogen separation through the separator 240 can be performed more efficiently. can

The mixed gas passing through the adsorber 230 may be compressed to a high pressure (eg, 20 bar) through the first compressor 70 and then injected into the separator 240 .

On the other hand, in the present invention, in order to prevent ammonia that has not been adsorbed in the adsorber 230 from being injected into the separator 240, it is installed in front of the separator 240, more specifically, in front of the first compressor 70, the separator It may further include an ammonia concentration sensor 92 for detecting the ammonia concentration in the mixed gas injected into the 240.

The ammonia concentration sensor 92 may check in real time whether or not the ammonia concentration in the mixed gas passing through deviates from a preset standard (eg, about 0.1 to 1 ppm) to check whether the facility operates normally.

The separator 240 is configured to separate hydrogen from the mixed gas that has passed through the adsorber 230 , and various configurations are possible.

For example, the separator 240 may be a pressure swing absorption (PSA) or hydrogen separation membrane for nitrogen and hydrogen separation.

6 is an embodiment showing a case in which the separator 240 is formed of a PSA. Here, the separator 240 may be configured to separate hydrogen from the mixed gas by adsorbing nitrogen from the mixed gas injected under specific conditions (eg, 20 bar, 0° C. to 20° C.) and discharging only hydrogen.

As shown in FIG. 6 , the separator 240 may include a plurality of separation modules 240a and 240b connected in parallel to each other.

On the other hand, in the case of FIG. 6 , the separator 240 has been described focusing on an embodiment including two separation modules 240a and 240b connected in parallel to each other, but the separator 240 includes a single separation module or Of course, an embodiment including three or more separation modules connected in various ways, such as series and parallel, is also possible depending on the system capacity.

More specifically, the separator 240 includes a first separation module 240a, a second separation module 240b, and a plurality of valves ( V11, V12, V21, V22) may be included.

In this case, the first separation module 240a and the second separation module 240b may be used alternately for continuous hydrogen separation.

That is, while the first separation module 240a among the separation modules 240a and 240b separates hydrogen in the mixed gas, the other second separation module 240b is regenerated (or can be replaced).

For example, while the first separation module 240a separates hydrogen from the mixed gas, the valves V11 and V21 corresponding to the first separation module 240a are opened, and corresponding to the second separation module 240b The valves V12 and V22 are closed.

Since the first separation module 240a separates and discharges only hydrogen from the mixed gas, the hydrogen that has passed through the first separation module 240a may be injected into the hydrogen storage unit 300 to be described later through the V21 valve.

As hydrogen separation proceeds in the first separation module 240a, when the first separation module 240a is saturated after a certain time elapses, on the contrary, valves V11 and V21 are closed to regenerate the first separation module 240a (or replacement), the V12 and V22 valves are opened to inject the mixed gas into the second separation module 240b.

Similarly, hydrogen separated by passing through the second separation module 240b may be injected into the hydrogen storage unit 300 to be described later through the V22 valve.

That is, hydrogen separation can be continuously performed without interruption through the first separation module 240a and the second separation module 240b.

By the way, while nitrogen adsorption through the first separation module 240a or the second separation module 240b is performed in a low temperature environment (20 bar, 0° C. to 20° C.), the first separation module 240a or the second separation module ( 240b) regeneration (nitrogen emission) requires a relatively high temperature environment.

At this time, as a heat source for regeneration of the first separation module 240a or the second separation module 240b, the high-temperature exhaust gas discharged from the heating unit 250 may be utilized.

3, the high-temperature exhaust gas formed as a result of combustion through the heating unit 250 is moved along the outer walls of the first separation module 240a and the second separation module 240b, and the first separation module The temperature of the 240a and the second separation module 240b may be raised to a temperature suitable for regeneration.

At this time, a plurality of valves (V41, V42, V51, V52) for controlling the flow direction of the exhaust gas of the heating unit 250 on the separator 240 side may be provided.

When regeneration of the first separation module 240a is required, V51 and V41 are opened to increase the temperature of the first separation module 240a, and the exhaust gas flowing along the outer wall of the first separation module 240a is externally passed through V41. is exhausted (V, vent).

The nitrogen discharged from the first separation module 240a by the regeneration process is exhausted (V, vent) to the outside through the vacuum pump 80 riding the V31 valve. At this time, V52, V42, V32 of the second separation module 240b maintains the closed state.

Conversely, when regeneration of the second separation module 240b is required, V52 and V42 are opened to increase the temperature of the second separation module 240b, and the exhaust gas flowing along the outer wall of the second separation module 240b passes through V42. It is exhausted (V, vent) to the outside through

The nitrogen discharged from the second separation module 240b by the regeneration process is exhausted (V, vent) to the outside through the vacuum pump 80 riding the V32 valve. At this time, V51, V41, V31 of the first separation module 240a maintains the closed state.

That is, the exhaust gas of the heating unit 250 for heating the vaporizer 210 of the present invention has an advantage that can be utilized as a heat source for regeneration of the separator 240 .

Hydrogen that has passed through the first separation module 240a or the second separation module 240b may be injected into the hydrogen storage unit 300 .

At this time, between the separator 240 and the hydrogen storage unit 300, a second compressor 40 for compressing the hydrogen that has passed through the separator 240 to a high pressure may be installed.

On the other hand, in the present invention, in order to check the hydrogen concentration of the gas that has passed through the separator 240 in real time, it is installed at the front end of the dispenser unit 400, more specifically, the front end of the second compressor 40 to detect the hydrogen concentration passing through. A hydrogen concentration sensor 94 may be further included.

The hydrogen concentration sensor 94 may check whether the equipment is normally operated by detecting in real time whether the gas passing through meets a hydrogen concentration higher than a preset standard (eg, 99.995% or more).

The hydrogen storage unit 300 is configured to store hydrogen compressed at high pressure through the second compressor 40, and various configurations are possible if it is configured to store high-pressure hydrogen or liquid hydrogen.

The dispenser unit 400 is connected to external equipment that requires hydrogen charging, and various configurations are possible in a configuration for supplying hydrogen stored in the hydrogen storage unit 300 to the external equipment.

Here, the external equipment may include all equipment using hydrogen as a fuel, and for example, as shown in FIG. 7 , may be a hydrogen vehicle 50 using a fuel cell.

Hereinafter, the circulation system of the ammonia-based on-site hydrogen charging station including the above-described configuration will be described in detail.

Referring to FIG. 3 , the hydrogen production unit 200 includes an ammonia distributor 270 for distributing at least a portion of gaseous ammonia that has passed through the vaporizer 210 to the heating unit 250 and the reactor 220, respectively, and a separator. A hydrogen distributor 280 for distributing at least a portion of the hydrogen separated in 240 to the heating unit 250 and the hydrogen storage unit 300 may be further included.

The ammonia distributor 270 is installed between the vaporizer 210 and the reactor 220 to inject the majority of gaseous ammonia that has passed through the vaporizer 210 into the reactor 220 and distributes at least a portion to the heating unit 250 . A variety of configurations are possible.

Similarly, the hydrogen distributor 280 is installed between the separator 240 and the hydrogen storage unit 300 (more specifically, the second compressor 40), the majority of the separated and discharged from the separator 240 As a configuration for injecting hydrogen into the hydrogen storage unit 300 through the compressor 40 and distributing at least a portion to the heating unit 250 , various configurations are possible.

Through this, the heating unit 250 may receive ammonia and hydrogen respectively and utilize it as fuel for combustion.

The exhaust gas produced after the ammonia and hydrogen supplied to the heating unit 250 through the ammonia distributor 270 and the hydrogen distributor 280 is combusted can be utilized as a heat source of the separator 240 as described above. same.

More specifically, the hydrogen production unit 200 is, the ammonia and hydrogen supplied to the heating unit 250 through the ammonia distributor 270 and the hydrogen distributor 280 is combusted, and then the generated exhaust gas is discharged to the separator ( 240) may include an exhaust gas transport line 292 for use as a heat source.

Since the above has only been described with respect to some of the preferred embodiments that can be implemented by the present invention, the scope of the present invention as noted above should not be construed as being limited to the above embodiments, and It will be said that the technical idea and the technical idea accompanying the fundamental are all included in the scope of the present invention.

100: liquid ammonia storage unit 200: hydrogen production unit
300: hydrogen storage unit 400: dispenser unit

Claims (11)

An ammonia storage tank unit 100 for storing liquid ammonia, and
A hydrogen production unit 200 for producing hydrogen using the liquid ammonia supplied from the ammonia storage tank unit 100;
A hydrogen storage unit 300 for storing the hydrogen produced by the hydrogen production unit 200, and
Ammonia-based on-site hydrogen charging station, characterized in that it is connected to external equipment requiring hydrogen charging and comprises a dispenser unit 400 for supplying hydrogen stored in the hydrogen storage unit 300 to the external equipment. The method according to claim 1,
The ammonia storage tank unit 100 is an ammonia-based on-site hydrogen charging station, characterized in that it is installed in an underground space (B) separated from the ground by being surrounded by a protective wall (2) on all sides below the ground. 3. The method according to claim 2,
The ammonia storage tank unit 100,
A storage tank 110 for storing liquid ammonia located in the underground space B, and a liquid ammonia inlet pipe 120 communicating with the liquid ammonia supply unit 10 and introducing liquid ammonia into the storage tank 110 and , Ammonia-based on-site hydrogen charging station, characterized in that it communicates with the hydrogen production unit (200) and comprises a liquid ammonia outlet pipe (130) for discharging liquid ammonia from the storage tank (110). 4. The method of claim 3,
The ammonia storage tank unit 100 includes a leak detection unit 140 for detecting whether the storage tank 110 is leaking, and vapor phase ammonia into the underground space B when a leak occurs in the storage tank 110 . Ammonia-based on-site hydrogen charging station, characterized in that it further comprises a solvent spraying unit 150 for spraying a solvent 23 that can be dissolved. The method according to claim 1,
The ammonia storage tank unit 100, ammonia-based on-site, characterized in that it further comprises at least one sensor 160 for measuring at least one of temperature and pressure inside the storage tank 110 hydrogen refueling station. The method according to claim 1,
The ammonia storage tank unit 100 is installed on the outside of the storage tank 110, ammonia-based on-site hydrogen, characterized in that it further comprises a temperature control unit 170 for controlling the temperature of the liquid ammonia charging station. The method according to claim 1,
The hydrogen production unit 200 includes a vaporizer 210 that receives liquid ammonia stored in the ammonia storage tank unit 100 and vaporizes it into vapor phase ammonia, and decomposes vapor phase ammonia vaporized in the vaporizer 210 into nitrogen and hydrogen. a reactor 220, an adsorber 230 for adsorbing unreacted ammonia among the mixed gas passing through the reactor 220, and a separator 240 for separating hydrogen from the mixed gas passing through the adsorber 230. Ammonia-based on-site hydrogen charging station, characterized in that it comprises. 8. The method of claim 7,
The hydrogen production unit 200,
A heating unit 250 for heating the gaseous ammonia in the reactor 220, and a heat exchanger 260 installed between the reactor 220 and the adsorber 230 to recover the heat of the mixed gas are additionally provided. Ammonia-based on-site hydrogen charging station, characterized in that it comprises. 9. The method of claim 8,
The hydrogen production unit 200,
An ammonia distributor 270 for distributing at least a portion of the vapor phase ammonia that has passed through the vaporizer 210 to the heating unit 250 and the reactor 220, respectively, and at least a portion of the hydrogen separated by the separator 240 Ammonia-based on-site hydrogen charging station, characterized in that it further comprises a hydrogen distributor (280) for distributing each to the heating unit (250) and the hydrogen storage unit (300). 10. The method of claim 9,
The hydrogen production unit 200, after combustion of ammonia and hydrogen supplied to the heating unit 250 through the ammonia distributor 270 and the hydrogen distributor 280, is a heat source of the separator 240. Ammonia-based on-site hydrogen charging station, characterized in that it further comprises an exhaust gas transport line (292) for use as a. 9. The method of claim 8,
The vaporizer 210 includes a first flow path P1 through which a fluid exchanging heat with liquid ammonia passing through the vaporizer 210 flows,
The heat exchanger 260 includes a second flow path P2 through which a fluid exchanging heat with the mixed gas passing through the heat exchanger 260 flows,
The hydrogen production unit 200, a fluid circulation line 294 for circulating communication between the first flow path P1 and the second flow path P2, and the fluid circulation line 294 to circulate the fluid along the fluid circulation line 294 Ammonia-based on-site hydrogen charging station, characterized in that it further comprises a circulation pump (296) installed in the line (294).

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