Methanol water reforming reaction hydrogen production system

Abstract

The utility model discloses a methanol water reforming reaction hydrogen production system, which comprises an air flue gas heat exchanger, a hydrogen generator and a methanol burner, a hot air outlet, a hot flue gas inlet and a hot flue gas outlet are arranged on the air flue gas heat exchanger, the hot air outlet is connected with the methanol burner, an outlet of the methanol burner is connected with the hydrogen generator, and the hot flue gas inlet is connected with the methanol burner. And an outlet of the hydrogen generator is connected with a hot flue gas inlet of the air-flue gas heat exchanger. According to the utility model, the combination of the air-flue gas heat exchanger and the methanol burner is used for providing heat energy for the hydrogen generator instead of the current mode of supplying electric energy by a fuel cell, so that the heat efficiency of the hydrogen production system is obviously improved, and the technical problem of high power consumption is also solved.

Description

Technical Field

[0001] The utility model relates to the technical field of methanol hydrogen production, in particular to a methanol-water reforming reaction hydrogen production system. Background Art

[0002] As the limitations of conventional energy sources become increasingly apparent, the world faces the dual challenges of resource scarcity and environmental pollution. Energy conservation and environmental protection have become a focus of attention, and the active exploration of new energy sources is of great significance to our times. Hydrogen, which produces only water after complete combustion, is an ideal clean energy source and is currently widely used in the chemical, pharmaceutical, metallurgical, and food processing industries.

[0003] There are many ways to produce hydrogen, but methanol-to-hydrogen production has become a top choice in many fields due to its wide raw material availability, low operating costs, and distributed deployment. When methanol-to-hydrogen production is combined with power generation, the methanol-to-hydrogen production unit, coupled with a fuel cell, has very high power requirements. The produced hydrogen is fed to the fuel cell for power generation. If too much electricity is used to power the methanol-to-hydrogen production unit, the power generation efficiency of the equipment will be too low, making it unsuitable for the scenario.

[0004] In view of this, this patent application is filed. Utility Model Content

[0005] The purpose of the utility model is to provide a methanol-water reforming reaction hydrogen production system to solve the above-mentioned technical problems of low power generation efficiency and high power consumption of the methanol hydrogen production device currently matched with fuel cells.

[0006] The utility model is achieved through the following technical solutions:

[0007] The purpose of the utility model is to provide a methanol-water reforming reaction hydrogen production system, which includes an air-to-flue gas heat exchanger, a hydrogen generator, and a methanol burner. The air-to-flue gas heat exchanger is provided with a hot air outlet, a hot flue gas inlet, and a hot flue gas outlet. The hot air outlet is connected to the methanol burner, the outlet of the methanol burner is connected to the hydrogen generator, and the outlet of the hydrogen generator is connected to the hot flue gas inlet of the air-to-flue gas heat exchanger.

[0008] In an optional embodiment, the hydrogen generator includes an evaporation and superheating layer flue gas channel and a reaction layer flue gas channel, and the evaporation and superheating layer flue gas channel and the reaction layer flue gas channel are both connected to the flue gas outflow end on the methanol burner, and a raw liquid flow channel is provided in the evaporation and superheating layer flue gas channel, and a reforming reaction channel is provided in the reaction layer flue gas channel, and the raw liquid flow channel is connected to the reforming reaction channel, and the evaporation and superheating layer flue gas channel and the reaction layer flue gas channel are connected to the hot flue gas inlet of the air-to-flue gas heat exchanger.

[0009] In an optional embodiment, the air-to-gas heat exchanger is a shell-and-tube heat exchanger.

[0010] In an optional embodiment, the outside of the heat exchange tubes of the shell-and-tube heat exchanger are all wrapped with heat exchange fins;

[0011] and / or the heat exchange fins are of a spiral sheet structure;

[0012] And / or the heat exchange fins are made of stainless steel;

[0013] And / or the air-to-gas heat exchanger is provided with an expansion joint.

[0014] In an optional embodiment, the air-to-gas heat exchanger is further provided with a cold air inlet;

[0015] And / or a blower is provided at the cold air inlet, and an induced draft fan is provided at the hot flue gas outlet.

[0016] In an optional embodiment, the evaporation and superheating layer flue gas channel is connected to the reaction layer flue gas channel, and the flue gas outflow end on the methanol burner is connected to the evaporation and superheating layer flue gas channel.

[0017] In an optional embodiment, the reaction layer flue gas channel is sleeved on the outside of the evaporation and superheating layer flue gas channel, and a flue gas communication channel is provided between the evaporation and superheating layer flue gas channel and the reaction layer flue gas channel.

[0018] In an optional embodiment, the reaction layer flue gas channel is provided with an insulation layer on the outside.

[0019] In an optional embodiment, a heat exchanger is further included, and the heat exchanger is provided with a raw liquid inlet, a raw liquid heat exchange outlet, a crude hydrogen inlet, and a crude hydrogen outlet. The raw liquid heat exchange outlet is connected to the raw liquid flow channel, and the crude hydrogen outflow end of the hydrogen generator is connected to the crude hydrogen inlet.

[0020] In an optional embodiment, it further includes a gas-liquid separation tank and a pressure swing adsorption purifier, wherein the gas-liquid separation tank is connected to the crude hydrogen outlet end of the heat exchanger, and the outlet of the gas-liquid separation tank is connected to the pressure swing adsorption purifier.

[0021] The advantages and beneficial effects of the present invention compared to the prior art are:

[0022] The methanol-water reforming reaction hydrogen production system in this utility model utilizes a combination of an air-to-gas heat exchanger and a methanol burner to provide heat energy for the hydrogen generator, replacing the current fuel cell method of supplying electricity. After providing heat energy to the hydrogen generator, the hot flue gas returns to the air-to-gas heat exchanger, exchanges heat with cold air, and is then discharged. This significantly improves the thermal efficiency of the hydrogen production system and solves the technical problem of high power consumption. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] In order to more clearly illustrate the technical solutions of the exemplary embodiments of the present invention, the following briefly introduces the drawings required for use in the examples. It should be understood that the following drawings only illustrate certain embodiments of the present invention and should not be considered as limiting the scope. A person of ordinary skill in the art can also derive other relevant drawings based on these drawings without inventive effort. In the drawings:

[0024] Figure 1 This is a structural schematic diagram of a crude hydrogen device in a methanol-water reforming reaction hydrogen production system provided in Example 1 of the present invention.

[0025] Figure 2 This is a structural schematic diagram of the hydrogen generator provided by the utility model.

[0026] Figure 3 This is a structural schematic diagram of a methanol-water reforming reaction hydrogen production system provided by the utility model.

[0027] Markings and corresponding parts names in the accompanying drawings:

[0028] 1-air-flue gas heat exchanger, 101-hot air outlet, 102-hot flue gas inlet, 103-hot flue gas outlet, 104-cold air inlet, 105-heat exchange fins, 106-expansion joint, 2-hydrogen generator, 201-evaporation superheated layer flue gas channel, 202-reaction layer flue gas channel, 203-raw liquid flow channel, 204-reforming reaction channel, 205-flue gas communication channel, 206-raw liquid inlet, 207-hydrogen outflow end, 208-heat source cylinder, 209-insulation layer, 3-methanol burner, 4-blower, 5-induced draft fan, 6-heat exchanger, 601-raw liquid inlet, 602-raw liquid heat exchange outlet, 603-crude hydrogen inlet, 604-crude hydrogen outlet, 7-gas-liquid separation tank, 8-pressure swing adsorption purifier. DETAILED DESCRIPTION

[0029] In order to make the purpose, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below in conjunction with embodiments and drawings. The schematic implementation methods of the present invention and their descriptions are only used to explain the present invention and are not intended to limit the present invention.

[0030] In the following description, numerous specific details are set forth to provide a thorough understanding of the present invention. However, it will be apparent to one skilled in the art that these specific details are not necessarily required to practice the present invention. In other embodiments, well-known structures, circuits, materials, or methods are not described in detail to avoid obscuring the present invention.

[0031] Throughout this specification, references to "one embodiment," "an embodiment," "an example," or "an example" mean that a particular feature, structure, or characteristic described in conjunction with the embodiment or example is included in at least one embodiment of the present invention. Therefore, the phrases "one embodiment," "an embodiment," "an example," or "an example" appearing in various places throughout this specification do not necessarily refer to the same embodiment or example. In addition, the particular features, structures, or characteristics may be combined in one or more embodiments or examples in any suitable combination and / or subcombination. Furthermore, it will be understood by those of ordinary skill in the art that the figures provided herein are for illustrative purposes only and are not necessarily drawn to scale. As used herein, the term "and / or" includes any and all combinations of one or more of the associated listed items.

[0032] In the description of the present invention, the terms "front", "rear", "left", "right", "up", "down", "vertical", "horizontal", "high", "low", "inside", "outside", etc., indicating directions or positional relationships, are based on the directions or positional relationships shown in the accompanying drawings. They are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific direction, be constructed and operated in a specific direction. Therefore, they should not be understood as limiting the scope of protection of the present invention.

[0033] Example 1:

[0034] like Figure 1 As shown in FIG, a methanol-water reforming reaction hydrogen production system is provided, specifically comprising an air-to-gas heat exchanger 1, a hydrogen generator 2, and a methanol burner 3, which constitute the crude hydrogen equipment of the hydrogen production system for producing crude hydrogen. The air-to-gas heat exchanger 1 is provided with a hot air outlet 101 and a hot flue gas inlet 102. It is also provided with a cold air inlet 104 and a hot flue gas outlet 103. The hot air outlet 101 is connected to the methanol burner 3, the outlet of the methanol burner 3 is connected to the hydrogen generator 2, and the outlet of the hydrogen generator 2 is connected to the hot flue gas inlet of the air-to-gas heat exchanger 1. The hot air exiting the air-to-gas heat exchanger 1 enters the methanol burner 3, where it reacts with and combusts with the methanol therein. The resulting gas enters the hydrogen generator 2 for a methanol reforming reaction. The hot flue gas produced after the reaction enters the air-to-gas heat exchanger 1, where it undergoes heat exchange with the cold air to form hot air. After the reaction, the hot flue gas can be discharged through the hot flue gas outlet 103.

[0035] This embodiment provides a methanol-water reforming reaction hydrogen production system that utilizes a combination of an air-to-gas heat exchanger 1 and a methanol burner 3 to provide heat energy to a hydrogen generator 2, replacing the current fuel cell method of supplying electricity. After providing heat energy to the hydrogen generator 2, the hot flue gas returns to the air-to-gas heat exchanger 1, exchanges heat with cold air, and is then discharged. This embodiment significantly improves the thermal efficiency of the hydrogen production system and solves the technical problem of high power consumption.

[0036] The hydrogen generator 2 in this embodiment includes an evaporation and superheating layer flue gas channel 201 and a reaction layer flue gas channel 202. Both the evaporation and superheating layer flue gas channel 201 and the reaction layer flue gas channel 202 are connected to the flue gas outlet port of the methanol burner 3. A raw material liquid flow channel 203 is provided within the evaporation and superheating layer flue gas channel 201, and a reforming reaction channel 204 is provided within the reaction layer flue gas channel 202. The raw material liquid flow channel 203 is connected to the reforming reaction channel 204. When producing hydrogen through a water reforming reaction, hot flue gas from the methanol burner 3 is respectively introduced into the evaporation and superheating layer flue gas channel 201 and the reaction layer flue gas channel 202. The raw material liquid is introduced into the hydrogen generator 2 through the raw material liquid flow channel 203. The raw material liquid, heated by the heat of the hot flue gas, enters the reforming reaction channel 204. The raw material liquid is heated by the hot flue gas in the reaction layer flue gas channel 202 located outside the reforming reaction channel 204, causing the material to react within the reforming reaction channel 204. The evaporation and superheating layer flue gas channel 201 and the reaction layer flue gas channel 202 can be designed to be connected to the hot flue gas inlet of the air-to-gas heat exchanger 1. In this way, the hot flue gas in the evaporation and superheating layer flue gas channel 201 and the reaction layer flue gas channel 202 can enter the air-to-gas heat exchanger 1.

[0037] Preferably, the air-to-gas heat exchanger 1 in this embodiment is a shell-and-tube heat exchanger. Heat exchange fins 105 are wrapped around the exterior of the heat exchange tubes. More preferably, the heat exchange fins 105 are spirally shaped to increase the heat exchange area. More preferably, the heat exchange fins 105 are made of stainless steel, and an expansion joint 106 is also provided on the air-to-gas heat exchanger 1.

[0038] Preferably, a blower 4 is provided at the cold air inlet 104 of the air-to-gas heat exchanger 1 , and an induced draft fan 5 is provided at the hot flue gas outlet 103 , so as to accelerate the entry of cold air and the discharge of hot flue gas.

[0039] Example 2:

[0040] Based on Example 1, this example provides a methanol-water reforming reaction hydrogen production system, in which an evaporation and superheating layer flue gas channel 201 is connected to a reaction layer flue gas channel 202, and the flue gas outlet of a methanol burner 3 is connected to the evaporation and superheating layer flue gas channel 201. In this way, the hot flue gas from the methanol burner 3 first enters the evaporation and superheating layer flue gas channel 201 to heat the raw material liquid, and then enters the reaction layer flue gas channel 202.

[0041] Preferably, the reaction layer flue gas channel 202 is sleeved outside the evaporation and superheating layer flue gas channel 201, such as Figure 2 As shown in FIG, the outer tube surface of the evaporation and superheating layer flue gas channel 201 is aligned with the inner circumference of the reaction layer flue gas channel 202, enclosing the evaporation and superheating layer flue gas channel 201 within the interior space of the reaction layer flue gas channel 202. A flue gas communication channel 205, such as a flue gas hole, is provided between the evaporation and superheating layer flue gas channel 201 and the reaction layer flue gas channel 202. In this way, the flue gas in the evaporation and superheating layer flue gas channel 201 enters the reaction layer flue gas channel 202 through the flue gas hole.

[0042] A heat source cylinder 208 can also be set up to pass hot flue gas into the heat source cylinder 208, and a flue gas hole is also set between the heat source cylinder 208 and the evaporation superheating layer flue gas channel 201, and the flue gas enters the evaporation superheating layer flue gas channel 201 through the heat source cylinder 208.

[0043] The purpose of this arrangement is to significantly reduce the area occupied by the hydrogen generator 2, and to make the heat of the flue gas more concentrated and not dispersed, thereby improving the heat utilization rate of the flue gas and the thermal efficiency of the whole machine. The addition of the heat source cylinder 208 can also protect the evaporation coil from being directly heated by the flame.

[0044] Furthermore, the hydrogen production system also includes a heat exchanger 6, which is provided with a feed liquid inlet 601, a feed liquid heat exchange outlet 602, a crude hydrogen inlet 603, and a crude hydrogen outlet 604. The feed liquid heat exchange outlet 602 is connected to the feed liquid flow channel 203, and the crude hydrogen outflow end of the hydrogen generator 2 is connected to the crude hydrogen inlet 603. The heat exchanger 6 is also provided with a cooling water inlet and a cooling water outlet. The heat exchanger 6 can be a plate heat exchanger 6. The feed liquid is initially preheated by the heat exchanger 6 before entering the hydrogen generator 2. The produced crude hydrogen is then cooled by the heat exchanger 6.

[0045] Example 3:

[0046] This embodiment provides a methanol-water reforming reaction hydrogen production system, based on Example 1 or Example 2, such as Figure 3As shown in FIG, the hydrogen production system also includes a gas-liquid separator 7 and a pressure swing adsorption purifier 8. The gas-liquid separator 7 is connected to the crude hydrogen outlet 604 of the heat exchanger 6, and the outlet of the gas-liquid separator 7 is connected to the pressure swing adsorption purifier 8. The gas-liquid separator 7 is used to initially remove condensed water from the crude hydrogen, while the pressure swing adsorption purifier is used to purify the crude hydrogen to a purity of 99% to 99.9999%. The purified hydrogen is connected to the hydrogen consumption end of the rear end.

[0047] The working principle of the methanol-water reforming reaction hydrogen production system of the present invention is:

[0048] Process 1: The raw liquid is preheated through the plate heat exchanger 6 and enters the hydrogen generator 2, where high-temperature crude hydrogen gas is generated. The high-temperature crude hydrogen gas returns to the heat exchanger 6 and is cooled by the raw liquid and cooling water to below 40 degrees. It then enters the gas-liquid separation tank 7 to remove the condensed water in the crude hydrogen. The dried crude hydrogen gas is then passed into the pressure swing adsorption purification device to obtain high-purity hydrogen after purification.

[0049] Process 2: Pure methanol and air are mixed and burned in methanol burner 3 to generate hot flue gas, which provides heat for hydrogen generator 2. In air-to-flue heat exchanger 1, the hot flue gas exchanges heat with cold air before being discharged. The cold air is preheated and then mixed with methanol for combustion, recovering the heat from the hot flue gas. This device utilizes methanol combustion, significantly reducing power consumption. The highly integrated hydrogen generator 2 also improves overall thermal efficiency.

[0050] The above specific implementation methods further illustrate the purpose, technical solutions and beneficial effects of the utility model in detail. It should be understood that the above are only specific implementation methods of the utility model and are not used to limit the scope of protection of the utility model. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principles of the utility model should be included in the scope of protection of the utility model.

Claims

1. A methanol-water reforming reaction hydrogen production system, characterized in that: The invention comprises an air-to-gas heat exchanger (1), a hydrogen generator (2), and a methanol burner (3); the air-to-gas heat exchanger (1) is provided with a hot air outlet (101), a hot flue gas inlet (102), and a hot flue gas outlet (103); the hot air outlet (101) is connected to the methanol burner (3); the outlet of the methanol burner (3) is connected to the hydrogen generator (2); and the outlet of the hydrogen generator (2) is connected to the hot flue gas inlet of the air-to-gas heat exchanger (1).

2. A methanol-water reforming reaction hydrogen production system according to claim 1, characterized in that: The hydrogen generator (2) comprises an evaporation and superheating layer flue gas channel (201) and a reaction layer flue gas channel (202), the evaporation and superheating layer flue gas channel (201) and the reaction layer flue gas channel (202) are both connected to the flue gas outflow end of the methanol burner (3), a raw liquid flow channel (203) is provided in the evaporation and superheating layer flue gas channel (201), a reforming reaction channel (204) is provided in the reaction layer flue gas channel (202), the raw liquid flow channel (203) is connected to the reforming reaction channel (204), and the evaporation and superheating layer flue gas channel (201) and / or the reaction layer flue gas channel (202) are connected to the hot flue gas inlet of the air-to-flue gas heat exchanger (1).

3. A methanol-water reforming reaction hydrogen production system according to claim 1, characterized in that: The air-to-gas heat exchanger (1) is a shell-and-tube heat exchanger.

4. A methanol-water reforming reaction hydrogen production system according to claim 3, characterized in that: The outside of the heat exchange tubes of the shell-and-tube heat exchanger are all wrapped with heat exchange fins (105); And / or the heat exchange fin (105) is a spiral sheet structure; And / or the heat exchange fins (105) are made of stainless steel; And / or the air-to-gas heat exchanger (1) is provided with an expansion joint (106).

5. A methanol-water reforming reaction hydrogen production system according to any one of claims 1 to 4, characterized in that: The air-smoke heat exchanger (1) is further provided with a cold air inlet (104); and / or a blower (4) is provided at the cold air inlet (104), and an induced draft fan (5) is provided at the hot smoke outlet (103).

6. A methanol-water reforming reaction hydrogen production system according to claim 2, characterized in that: The evaporation and superheating layer flue gas channel (201) is connected to the reaction layer flue gas channel (202), and the flue gas outflow end on the methanol burner (3) is connected to the evaporation and superheating layer flue gas channel (201).

7. A methanol-water reforming reaction hydrogen production system according to claim 6, characterized in that: The reaction layer flue gas channel (202) is sleeved on the outside of the evaporation and superheating layer flue gas channel (201), and a flue gas communication channel (205) is provided between the evaporation and superheating layer flue gas channel (201) and the reaction layer flue gas channel (202).

8. A methanol-water reforming reaction hydrogen production system according to claim 7, characterized in that: The reaction layer flue gas channel (202) is provided with a heat-insulating layer (209) on the outside.

9. A methanol-water reforming reaction hydrogen production system according to claim 8, characterized in that: The heat exchanger (6) is further included. The heat exchanger (6) is provided with a raw liquid inlet (601), a raw liquid heat exchange outlet (602), a crude hydrogen inlet (603), and a crude hydrogen outlet (604). The raw liquid heat exchange outlet (602) is connected to the raw liquid flow channel (203), and the crude hydrogen outflow end of the hydrogen generator (2) is connected to the crude hydrogen inlet (603).

10. A methanol-water reforming reaction hydrogen production system according to claim 9, characterized in that: It also includes a gas-liquid separation tank (7) and a pressure swing adsorption purifier (8), wherein the gas-liquid separation tank (7) is connected to the crude hydrogen outlet (604) end of the heat exchanger (6), and the outlet of the gas-liquid separation tank (7) is connected to the pressure swing adsorption purifier (8).

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