TW201300575A - Hydrogen production apparatus - Google Patents

Abstract

A hydrogen production apparatus includes a pump, a heating assembly, an electrolyser, at least one radiator and a converting unit. The heating assembly has at least one front-heater, a middle-heater and a solar heater. The front-heater connects to the pump. The middle-heater is mounted between the front-heater and the solar heater. The electrolyser connects to the solar heater and locates between the solar heater and the radiator. The radiator connects to the electrolyser and the front-heater. The converting unit connects to the radiator.

Description

Hydrogen production unit

The present invention relates to a hydrogen producing apparatus, and more particularly to a hydrogen producing apparatus for producing liquid hydrogen using liquid water.

With the rise of environmental awareness, in order to reduce oil consumption and carbon emissions, the development of new energy has gradually flourished. Among them, hydrogen energy plays an extremely important role in the development of new energy sources in the future due to its light weight, good thermal conductivity, non-toxicity and various storage and transportation characteristics.

For example, referring to FIG. 1, a conventional hydrogen generator 9 is disclosed, which is connected to each other by a compressor 91, a cooler 92, and a turbine 93 in sequence. In the hydrogen production operation, the conventional hydrogen production unit 9 first introduces gaseous hydrogen [H ₂ (g)] at normal pressure and normal temperature [pressure of about 1 atm and temperature of about 300 K] into the compressor 91. In order to convert it into high-pressure high-temperature gaseous hydrogen [pressure is about 20 atm, temperature is about 800 K]; then, the high-pressure high-temperature gaseous hydrogen flows into the cooler 92 to be constant-pressure and temperature-lowering, so that the gaseous hydrogen is maintained. Pressure; finally, when the high-pressure gaseous hydrogen flows through the turbine 93, low-pressure low-temperature liquid hydrogen [H ₂ (l)] is obtained for storage.

In general, the above-mentioned conventional hydrogen production device 9 mainly uses gaseous hydrogen to generate liquid hydrogen. However, since hydrogen molecules are mostly in a gaseous state, the compressor 91 must consume the bonding strength of gaseous hydrogen. A considerable amount of energy can smoothly compress gaseous hydrogen at normal pressure and normal temperature into high-temperature and high-temperature gaseous hydrogen. Therefore, the above-mentioned conventional hydrogen production device 9 is quite uneconomical and cannot meet the demand for energy saving and carbon reduction advocated by modern times. Furthermore, since the conventional hydrogen generator 9 must use gaseous hydrogen as a reactant to obtain liquid hydrogen smoothly, the conventional hydrogen generator 9 cannot generate other products other than liquid hydrogen, so that The functionality of the conventional hydrogen production unit 9 is rather limited, and the utility of the conventional hydrogen production unit 9 is relatively reduced.

In general, the conventional hydrogen production device 9 described above still has many disadvantages such as energy consumption and poor practicability, and further improvement is required.

SUMMARY OF THE INVENTION The object of the present invention is to solve the disadvantages of the prior art to provide a hydrogen producing apparatus which uses liquid water to pressurize and re-electrolyze to generate liquid hydrogen to effectively achieve energy saving.

Another object of the present invention is to provide a hydrogen producing apparatus which can generate liquid hydrogen and liquid oxygen using liquid water to effectively improve the utility.

In order to achieve the foregoing object, the technical content of the present invention includes:

A hydrogen production apparatus comprising: a pump; a heating unit having at least one front heater, an intermediate heater and a solar heater, wherein the at least one front heater is connected to the pump, the intermediate heater system Provided between the at least one front heater and the solar heater; an electrolyzer connected to the solar heater; at least one heat exchanger connecting the electrolyzer and the at least one front heater, and the electrolyzer is disposed on Between the solar heater and the heat exchanger; and a conversion unit connecting the at least one heat exhaustor.

The hydrogen generation device of the present invention may further comprise at least one auxiliary heat exchanger and an auxiliary conversion unit, wherein the at least one auxiliary heat exchanger is disposed between the electrolyzer and the auxiliary conversion unit, and the at least one auxiliary heat exchanger is connected The at least one front heater is configured to produce liquid oxygen at normal temperature and low pressure.

The above and other objects, features and advantages of the present invention will become more <RTIgt;

The "normal temperature" of the present invention, which is referred to as 300 K, is understood by those skilled in the art; the "high temperature" as described below in the present invention means that the temperature is higher than the normal temperature of the crucible; The term "low temperature" as used herein refers to a temperature lower than the normal temperature of the crucible; the "lower temperature" as described below in the present invention means that the temperature is lower than that of the crucible.

The "normal pressure" of the present invention, which is referred to as "atmospheric pressure", is understood by those skilled in the art; the "high pressure" as described below in the present invention means that the pressure is higher than the pressure of the helium; The "low pressure" as used hereinafter in the present invention means that the pressure is lower than the pressure of the helium.

Referring to FIG. 2, the hydrogen generating apparatus according to the first embodiment of the present invention sequentially connects a pump 1, a heating unit 2, an electrolyzer 3, at least one heat exhaustor 4, and a first pipeline. A conversion unit 5.

The pump 1 is used for compressing liquid water [H ₂ O(l), hereinafter referred to as first liquid water raft] at normal temperature and normal pressure, in order to obtain liquid water of normal temperature and high pressure [hereinafter referred to as second liquid hydrazine]; In other words, the pump 1 is only used to increase the pressure of the liquid water, and the liquid water maintains the original temperature. In the present embodiment, the pump 1 compresses the first liquid water enthalpy of 1 atm 300 K into a second liquid water enthalpy of 20 atm 300 K.

The heating assembly 2 includes at least one front heater 21, an intermediate heater 22, and a solar heater 23, and the at least one front heater 21, the intermediate heater 22, and the solar heater 23 sequentially utilize the first tube. The roads are connected to each other; in other words, the at least one front heater 21 is connected to the pump 1, and the intermediate heater 22 is disposed between the at least one front heater 21 and the solar heater 23. It should be noted that the at least one front heater 21 may be connected to the at least one heat exhauster 4 for utilizing the heat (q) discharged by the at least one heat exchanger 4 during the high temperature and high pressure gaseous hydrogen circulation due to the temperature difference. The second liquid water bottle is heated to a first temperature [see the description below for details]. The intermediate heater 22 can raise the first temperature of the liquid water to a second temperature by using heat generated by burning natural gas or kerosene [Q1]. The solar heater 23 can further utilize the heat of the solar energy [Q2] to raise the second temperature of the liquid water to a third temperature to obtain high temperature and high pressure liquid water [hereinafter referred to as a third liquid water bottle], thereby ensuring the The thermal state of the third liquid water raft can reach the critical point smoothly.

In the present embodiment, a single front heater 21 is selected between the pump 1 and the intermediate heater 22 as an embodiment for illustration, and the front heater 21 can be generated by electrolysis. The heat discharged from the high enthalpy of the high temperature and high pressure gaseous hydrogen [q] heats the second liquid water raft from 300 K to 600 K [first temperature], and the intermediate heater 22 can raise the liquid water from 600 K. Up to 1000 K [second temperature], the solar heater 23 can further raise the liquid water from 1000 K to 1010 K [third temperature].

The electrolyzer 3 can be configured for various structures capable of electrolyzing high temperature and high pressure gaseous hydrogen [H ₂ (g)] and high temperature and high pressure gaseous oxygen [O ₂ (g)] at a critical point of the third liquid water enthalpy. Gaseous hydrogen and gaseous oxygen can be directed to different pipelines. In this embodiment, the electrolyzer 3 is simultaneously electrothermally decomposed with the solar heater 23 to add a catalytic catalyst to the third liquid water raft for smooth operation. Produces gaseous hydrogen and gaseous oxygen. More specifically, the electrolyzer 3 has an input end 31, a first output end 32 and a second output end 33, and the input end 31 is connected to the solar heater 23. The first output end 32 is connected to the at least one heat exhauster 4 for outputting high temperature and high pressure gaseous hydrogen [hereinafter referred to as first gaseous hydrogen hydroquinone]; the second output end 33 is connectable to another pipeline ( It is not shown) for outputting high temperature and high pressure gaseous oxygen [hereinafter referred to as "first gaseous oxygen oxime"). It is worth noting that the temperature and pressure of the gaseous hydrogen and the gaseous oxygen after passing through the electrolyzer 3 are maintained at the temperature and pressure of the third liquid water, that is, the electrolyte 3 can be obtained. Gaseous hydrogen and gaseous oxygen at atmospheric pressure of 1010 K.

The at least one heat exchanger 4 is mainly configured to discharge the heat of the first gaseous hydrogen hydrazine, and the first gaseous hydrogen hydrazine is cooled and fixed to obtain a gaseous hydrogen at normal temperature and high pressure (hereinafter referred to as a second gaseous hydrogen hydrazine). ]. It should be noted that the number of the at least one heat exchanger 4 may be selected corresponding to the number of the at least one front heater 21, and the corresponding heater 21 and the heat exhaustor 4 may be connected; The number of the at least one heat exchanger 4 may also be selected to be greater than the number of the at least one front heater 21, whereby in addition to discharging the heat of the first gaseous hydrogen hydrazine to the at least one front heater 21, The heat of the first gaseous hydroquinone can also be applied to a suitable component or occasion.

In this embodiment, the number of the at least one heat exchanger 4 is selected to correspond to the number of the at least one front heater 21, that is, the embodiment only selects a single heat exhaustor 4 as an implementation aspect; When the first gaseous hydrogen hydrazine passes through the heat eliminator 4 after 20 atmospheres of 1010 K, it can be converted into a second gaseous hydroquinone at 20 atmospheres and 300 Torr. More importantly, the front heater 21 is used in combination with the heat exchanger composed of the heat exchanger 4 to heat the second liquid water bottle to the first temperature in advance, so that the intermediate heater 22 is only It is necessary to use a little energy to smoothly raise the liquid water from the first temperature to the second temperature, which helps to save the energy required for the intermediate heater 22.

The conversion unit 5 is configured to convert the second gaseous hydroquinone into a low temperature and low pressure liquid hydrogen [H ₂ (1)] and a gaseous hydrogen [H ₂ (g)], whereby the liquid hydrogen can be stored It is used to smoothly complete the hydrogen production operation, and the gaseous hydrogen can be introduced into the anode flow path of a fuel cell (not shown) to provide the electrolyzer 3 for use by electrochemical reaction output power. More specifically, the conversion unit 5 includes a turbine 51 and a final heater 52. The turbine 51 is disposed between the heat exhauster 4 and the final heater 52, and the heater 52 is disposed at the end. Between the turbine 51 and the separator 53. Wherein, the turbine 51 is configured to expand the second gaseous hydroquinone of the crucible and reduce the temperature to lower the temperature to convert the second gaseous hydroquinone to a lower temperature and lower pressure liquid hydrogen [hereinafter referred to as "first liquid hydroquinone"] And a mixture of a lower temperature and a lower pressure gaseous hydrogen [hereinafter referred to as a third gaseous hydroquinone]; the heater 52 is capable of utilizing heat generated by general industrial waste heat [Q3], the first liquid hydrogen hydrazine and hydrazine of the hydrazine The third gaseous hydroquinone is subjected to isostatic heating to convert it into a mixture of low-temperature low-pressure liquid hydrogen (hereinafter referred to as second liquid hydroquinone) and low-temperature low-pressure gaseous hydrogen (hereinafter referred to as fourth gaseous hydroquinone). It is worth noting that when the second gaseous hydroquinone flows into the turbine 51, the turbine 51 can be enabled to output shaft work, which can be used to drive a heat engine unit (not shown) to act.

In the present embodiment, the turbine 51 converts the second gaseous hydroquinone at 20 atmospheres and 300 Torr into the first liquid hydroquinone and the third gaseous hydroquinone at 0.1 atmospheres and 20 K, and the second heater 52 Then, the pressure is respectively heated to 0.1 atm. 66 K after the second liquid hydroquinone and the fourth gaseous hydrogen hydroquinone.

Referring to FIG. 2 again, in the hydrogen production operation of the present invention, the first liquid water enthalpy of 1 atm 300 K is introduced into the pump 1 for isothermal pressurization to obtain 20 atmospheres. After 200 K, the second liquid leeches. In the initial stage of operation, when the heat exchanger 4 has not discharged the heat [q] generated by the high-temperature electrolysis to the front heater 21, the intermediate heater 22 can be directly used to transfer the second liquid water of 20 atmospheres and 300 Torr. After heating at a constant pressure to 1000 K, the solar heater 23 is further used to further heat it at a constant pressure to obtain a third liquid water enthalpy at 20 atmospheres of 1010 K. When the third liquid water enthalpy flows into the electrolyzer 3 and reacts with the catalyst in a critical state, the first output end 32 of the electrolyzer 3 can introduce the first gaseous hydroquinone at 20 atmospheres and 1010 K into the heat rejection. The heat exchanger 4 can smoothly introduce the heat [q] of the first gaseous hydroquinone into the front heater 21. Thereby, in the middle of the operation, the front heater 21 can smoothly heat the second liquid water enthalpy of 20 atm 300 K to 600 K by the heat [q], and then the intermediate heater 22 It is heated to 1000 K to save the energy required for the intermediate heater 22.

After the heat exchanger 4 performs isostatic heat rejection for the first gaseous hydroquinone at 20 atmospheres of 1010 K, the second gaseous hydrogen hydrazine at 20 atmospheres and 300 K is introduced into the turbine 51 to make the second gaseous hydrogen. The turbine 51 expands and depressurizes and cools to obtain a first liquid hydroquinone and a third gaseous hydroquinone at a pressure of 0.1 atm. Thereby, the first liquid hydroquinone and the third gaseous hydroquinone of the crucible are further heated by the end heater 52 to generate a second liquid hydroquinone and a fourth gaseous hydrogen gas of 0.1 atm 66 K. 〞, in order to smoothly obtain hydrogen energy with many characteristics such as light weight, good thermal conductivity, non-toxicity and storage and transportation according to different types.

The main technical feature of the hydrogen generating device of the present invention is that since the bonding strength of the liquid water is weaker than the bonding strength of the gaseous hydrogen, it is quite easy to pressurize the liquid water at normal temperature and normal pressure to the normal temperature and high pressure. The energy required for the pump 1 can be relatively saved; moreover, the heat exchanger composed of the front heater 21 and the heat exhaustor 4 is used together with the design of the solar heater 23, and only a small amount is needed. The energy can heat the liquid water in an environment close to a critical state, so that the high temperature and high pressure liquid water can be smoothly electrolyzed to generate high temperature and high pressure gaseous hydrogen. Thereby, the invention can effectively achieve the energy saving effect.

Referring to FIG. 3, a hydrogen generation apparatus according to a second embodiment of the present invention is disclosed. In contrast to the first embodiment, the conversion unit 5 of the second embodiment is further provided with a resolver 53, and the second implementation For example, an auxiliary auxiliary heat exchanger 6, an auxiliary conversion unit 7, and a fuel cell (P) are additionally provided as an embodiment; wherein the second output end 33 of the electrolyzer 3 utilizes a second pipeline The at least one auxiliary heat exchanger 6 and the auxiliary conversion unit 7 are connected in sequence, and the fuel cell (P) is connected to the conversion unit 5 and the auxiliary conversion unit 7.

The decomposer 53 is connected to the final heater 52 and the fuel cell (P), and the final heater 52 is interposed between the turbine 51 and the resolver 53; the decomposer 53 can be used to the second liquid hydrogen The crucible is guided to a storage unit (not shown) for storage, and the crucible fourth gaseous hydroquinone is directed to the anode flow path of the fuel cell (P).

The at least one auxiliary heat exchanger 6 is mainly configured to discharge the heat of the first gaseous oxygen enthalpy, and the first gaseous oxygen enthalpy is cooled and fixed to obtain a gaseous oxygen of normal temperature and high pressure [hereinafter referred to as 〝 second gaseous oxygen] 〞]. It should be noted that the number of the at least one auxiliary heat exchanger 6 may also be selected corresponding to the number of the at least one front heater 21, and the corresponding front heater 21 and the at least one auxiliary heat exchanger 6 may be connected; Moreover, depending on the use requirement, the number of the at least one auxiliary heat exchanger 6 may be more than the number of the at least one front heater 21, thereby discharging the heat of the first gaseous oxygen enthalpy to the at least one The front heater 21 can further apply the heat of the first gaseous oxygen enthalpy to a suitable component or occasion.

In this embodiment, the number of the at least one auxiliary heat exchanger 6 is selected to correspond to the number of the at least one front heater 21, that is, the embodiment selects a single auxiliary heat extractor 6 as an implementation aspect. Wherein, after the first atmospheric oxygen enthalpy of 20 at 10 10 K passes through the auxiliary heat eliminator 6, it can be converted into a second gaseous oxygen of 20 atm 300 K. More importantly, the front heater 21 is utilized. The heat exchanger comprising the heat exchanger 4 and the auxiliary heat exchanger 6 can quickly raise the first temperature of the second liquid water tank to be close to the second temperature, so that the intermediate heater 22 The liquid water can be quickly raised from the first temperature to the second temperature with a small amount of energy.

The auxiliary conversion unit 7 is configured to convert the second gaseous oxygen gas into a liquid oxygen [O ₂ (l)] and a gaseous oxygen [O ₂ (g)] at a normal temperature and a low pressure, whereby the liquid oxygen can be stored. For use, to enhance the utility of the hydrogen production device, and the gaseous oxygen can be introduced into the cathode flow channel of the fuel cell (P) to cooperate with the fourth gaseous hydrogen hydrazine to serve as the fuel cell (P). ) the fuel. More specifically, the auxiliary conversion unit 7 includes an auxiliary turbine 71, an auxiliary end heater 72, and an auxiliary resolver 73. The auxiliary turbine 71 is disposed in the auxiliary heat exchanger 6 and the auxiliary end heater 72. The auxiliary end heater 72 is disposed between the auxiliary turbine 71 and the auxiliary resolver 73. Wherein, the auxiliary turbine 71 is configured to expand the second gaseous oxygen enthalpy and reduce the temperature to reduce the temperature of the second gaseous oxygen enthalpy to low temperature and low pressure liquid oxygen [hereinafter referred to as first liquid oxygen enthalpy] and A mixture of low temperature and low pressure gaseous oxygen [hereinafter referred to as third gaseous oxygen oxime]. The auxiliary end heater 72 can use the heat generated by the general industrial waste heat [Q4] to isothermally heat the first liquid oxygen enthalpy and the third gaseous oxygen enthalpy to smoothly obtain the liquid oxygen at normal temperature and low pressure [ Weigh the second liquid oxygen oxime] and the gaseous oxygen at normal temperature and low pressure [hereinafter referred to as the fourth gaseous oxindole]. The auxiliary resolver 73 is connected to the auxiliary end heater 72 and the fuel cell (P), and the auxiliary end heater 72 is interposed between the auxiliary turbine 71 and the auxiliary resolver 73; the auxiliary resolver 73 can be used to The second liquid oxygen enthalpy is directed to a storage unit (not shown) for storage, and the fourth gaseous oxygen enthalpy is directed to the cathode flow path of the fuel cell (P). It is noted that when the second gaseous oxygen enthalpy flows into the auxiliary turbine 71, the auxiliary turbine 71 can be made to output shaft work, which can be used to push another heat engine unit (not shown) to act.

In the present embodiment, the auxiliary turbine 71 converts the second gaseous oxygen enthalpy of 20 atmospheres and 300 Torr into the first liquid oxygen enthalpy and the third gaseous oxygen enthalpy of 0.1 atmospheres 66 K, and the auxiliary final heater 72, and then separately heated to a pressure of 0.1 atm, 300 K, a second liquid oxygen enthalpy and a fourth gaseous oxygen enthalpy.

The fuel cell (P) is connected to the decomposer 53 and the auxiliary decomposer 73, and the fuel cell (P) can also be connected to the electrolyzer 3; the fuel cell (P) is the fourth gaseous hydrogen hydride and The fourth gaseous oxygen oxime is used as a fuel, and electric power is generated by an electrochemical reaction to drive the electrolyzer 3 to operate, and the third liquid hydrazine can be smoothly electrolyzed to generate the first gaseous hydroquinone and hydrazine. A gaseous oxygen oxime.

The hydrogen generating device of the second embodiment of the present invention has the same functions and functions as those of the first embodiment, and can further generate liquid oxygen at normal temperature and low pressure, and relatively save energy required for the intermediate heater 22. . Furthermore, the second embodiment further drives the electrolyzer 3 to operate by the design of the fuel cell (P).

Referring to FIG. 4, a hydrogen generating apparatus according to a third embodiment of the present invention is disclosed. Compared with the second embodiment, the third embodiment can selectively connect the converting unit 5 to a first heat engine unit 8a. Alternatively, the auxiliary conversion unit can be connected to a second heat engine unit 8b.

In addition, in this embodiment, the number of the at least one front heater 21, the at least one heat exhaustor 4, and the at least one auxiliary heat exchanger 6 are selected as a plurality of embodiments. More specifically, in this embodiment, a first front heater 21a and a second front heater 21b are disposed between the pump 1 and the intermediate heater 22, and the first front heater 21a is connected to the first front heater 21a. Pumping 1 and the second front heater 21b is connected to the intermediate heater 22; the number of the plurality of heat exchangers 4 is selected as four, that is, the first output of the electrolyzer 3 The end 32 is connected to a first heat exhaustor 4a, a second heat exhaustor 4b, a third heat exhaustor 4c and a fourth heat exchanger 4d, and the fourth heat exchanger 4d is connected to the turbine. 51; the number of the auxiliary auxiliary heat exchangers 6 is selected as two embodiments, that is, the second output end 33 of the electrolyzer 3 is sequentially connected to a first auxiliary heat extractor 6a and a first The second auxiliary heat exchanger 6b connects the second auxiliary heat exchanger 6b to the auxiliary turbine 71.

It is to be noted that the first front heater 21a is connected to the second heat exhauster 4b and the second auxiliary heat exchanger 6b, and the second front heater 21b is connected to the first heat exchanger 4a and the first auxiliary Heater 6a. Therefore, in this embodiment, the first gaseous hydroquinone and the first gaseous oxygen enthalpy are selected to perform isostatic heat removal in a multi-stage manner, so that the first and second front heaters 21a, 21b can be The first liquid mash of the crucible is isostatically heated. Furthermore, the fourth heat exchanger 4d can be connected to the auxiliary end heater 72 of the auxiliary conversion unit 7, whereby the heat discharged by the first gaseous hydrogen hydrazine during the isothermal heat removal process can be used to heat the The first liquid oxygen enthalpy and the third gaseous oxygen enthalpy can further save the energy required for the auxiliary final heater 72.

The first heat engine unit 8a is connected to the turbine 51 of the conversion unit 5 to drive the first heat engine unit 8a to be actuated by the shaft power outputted by the turbine 51, so that the first heat engine unit 8a can provide power to various places. Required components or places. More specifically, the first heat engine unit 8a is sequentially connected to each other by a first compressor 81a, a first evaporator 82a, a first steam turbine 83a, and a first condenser 84a. The pipeline is filled with a first working fluid. The first compressor 81a is connected to the turbine 51, so that the first compressor 81a is driven by the shaft power outputted by the turbine 51 to compress the first working fluid, so that the first working fluid can smoothly perform a first A power cycle causes the first steam turbine 83a to output shaft work [W1]. It should be noted that, in this embodiment, the first condenser 84a may be connected to the second front heater 21b to discharge the low-quality sensible heat of the first working fluid to the second front heater 21b. The energy required for the intermediate heater 22 can also be relatively saved.

The second heat engine unit 8b is connected to the auxiliary turbine 71 of the auxiliary conversion unit 7 to drive the second heat engine unit 8b to operate by the shaft power outputted by the auxiliary turbine 71, so that the second heat engine unit 8b can provide power. To all the required components or places. More specifically, the second heat engine unit 8b is sequentially connected to each other by a second compressor 81b, a second evaporator 82b, a second steam turbine 83b, and a second condenser 84b. The pipeline is filled with a second working fluid. The second compressor 81b is connected to the auxiliary turbine 71 to drive the second compressor 81b to compress the second working fluid by the shaft power outputted by the auxiliary turbine 71, so that the second working fluid can be smoothly performed. A second power cycle causes the second steam turbine 83b to output shaft work [W2].

It should be noted that, in this embodiment, the second evaporator 82b can be connected to the third heat exchanger 4c for receiving the heat discharged by the third heat exchanger 4c, so as to effectively save the need to input the second The heat required by the heat engine unit 8b. More importantly, the second condenser 84b can be connected to the first front heater 21a to discharge the low-quality sensible heat of the second working fluid to the first front heater 21a, thereby substantially saving the middle. The energy required for the heater 22 is required.

The hydrogen generating device of the third embodiment of the present invention has the same functions and functions as those of the second embodiment, and can further utilize the shaft power outputted by the turbine 51 and the auxiliary turbine 71 to respectively drive the first and The second heat engine units 8a, 8b are actuated, and the first and second heat engine units 8a, 8b can also be connected to the front heater 21 for heat exchange, which helps to save energy required for the intermediate heater 22.

In summary, the hydrogen production apparatus of the present invention is much less expensive than the gaseous hydrogen which converts the liquid water at normal temperature and pressure into the high temperature and high pressure liquid water, and is much smaller than the gaseous hydrogen which converts the gaseous hydrogen at normal temperature and normal pressure into high temperature and high pressure. The energy consumed is required, and the present invention can simultaneously generate liquid hydrogen and liquid oxygen. Therefore, the present invention can effectively achieve many functions such as saving energy and improving practicality.

While the invention has been described in connection with the preferred embodiments described above, it is not intended to limit the scope of the invention. The technical scope of the invention is protected, and therefore the scope of the invention is defined by the scope of the appended claims.

[this invention]

1. . . Pump

2. . . Heating component

twenty one. . . Front heater

21a. . . First front heater

21b. . . Second front heater

twenty two. . . Intermediate heater

twenty three. . . Solar heater

3. . . Electrolyzer

31. . . Input

32. . . First output

33. . . Second output

4. . . Heat exchanger

4a. . . First heat extractor

4b. . . Second heat exchanger

4c. . . Third heat exchanger

4d. . . Fourth heat exchanger

5. . . Conversion unit

51. . . Turbine

52. . . Final heater

53. . . Splitter

6. . . Auxiliary heat exchanger

6a. . . First auxiliary heat exchanger

6b. . . Second auxiliary heat exchanger

7. . . Auxiliary conversion unit

71. . . Auxiliary turbine

72. . . Auxiliary end heater

73. . . Auxiliary resolver

8a. . . First heat unit

81a. . . First compressor

82a. . . First evaporator

83a. . . First steam turbine

84a. . . First condenser

8b. . . Second heat engine unit

81b. . . Second compressor

82b. . . Second evaporator

83b. . . Second steam turbine

84b. . . Second condenser

P. . . The fuel cell

[知知]

9. . . Hydrogen production unit

91. . . compressor

92. . . Cooler

93. . . Turbine

Figure 1: Schematic diagram of a conventional hydrogen production unit.

Fig. 2 is a schematic view showing a hydrogen producing apparatus according to a first embodiment of the present invention.

Fig. 3 is a schematic view showing a hydrogen producing apparatus according to a second embodiment of the present invention.

Fig. 4 is a schematic view showing a hydrogen producing apparatus according to a third embodiment of the present invention.

1. . . Pump

2. . . Heating component

twenty one. . . Front heater

twenty two. . . Intermediate heater

twenty three. . . Solar heater

3. . . Electrolyzer

31. . . Input

32. . . First output

33. . . Second output

4. . . Heat exchanger

5. . . Conversion unit

51. . . Turbine

52. . . Final heater

Claims (11)

A hydrogen production apparatus comprising: a pump; a heating unit having at least one front heater, an intermediate heater and a solar heater, wherein the at least one front heater is connected to the pump, and the intermediate heater is configured Between the at least one front heater and the solar heater; an electrolyzer connected to the solar heater; at least one heat exchanger connecting the electrolyzer and the at least one front heater, and the electrolyzer is disposed at the Between the solar heater and the heat exchanger; and a conversion unit connecting the at least one heat exhaustor. The hydrogen generation device according to claim 1, wherein the conversion unit comprises a turbine and a final heater, and the turbine is disposed between the at least one heat exhaustor and the final heater. The hydrogen generation device according to claim 2, wherein the conversion unit further comprises a decomposer, the decomposer is connected to the end heater, and the heater is interposed between the turbine and the decomposer. The hydrogen generation apparatus of claim 2, wherein the turbine is connected to a first heat engine unit. The hydrogen generating apparatus of claim 4, wherein the first heat engine unit has a first condenser, and the first condenser is connected to the at least one front heater. The hydrogen-making device according to claim 1, 2, 3, 4 or 5, wherein the electrolyzer has an input end, a first output end and a second output end, the input end being connected to the solar heater The first output end is connected to the at least one heat exhauster, the second output end is connected to the at least one auxiliary heat exchanger, and the at least one auxiliary heat exchanger is connected to the at least one front heater. The hydrogen generation device of claim 6, further comprising an auxiliary conversion unit, the at least one auxiliary heat exchanger being disposed between the auxiliary conversion unit and the electrolyzer. The hydrogen generation device of claim 7, wherein the auxiliary conversion unit comprises an auxiliary turbine, an auxiliary end heater and an auxiliary decomposer, the auxiliary turbine being disposed on the at least one auxiliary heat exchanger and auxiliary Between the final heaters, the auxiliary end heater is disposed between the auxiliary turbine and the auxiliary resolver, and the auxiliary turbine is coupled to a second heat unit. The hydrogen generating apparatus of claim 8, wherein the second heat engine unit has a second condenser, and the second condenser is connected to the at least one front heater. The hydrogen production apparatus according to claim 8, wherein the at least one heat exhauster is a plurality of heaters, and one of the heat exchangers is connected to the auxiliary heater. The hydrogen-producing device according to claim 8 , wherein the at least one heat exchanger is a plurality, and the second heat engine unit further comprises a second evaporator, wherein the second evaporator is connected to one of the heat exchangers.