Methanol hydrogen production system

Abstract

The utility model relates to the technical field of hydrogen preparation, in particular to a methanol hydrogen production system which comprises a methanol water supply device, the input end of the first passage of the heat exchange equipment is connected with the output end of the methanol water supply device through a pipeline; the input end of the tube pass of the reforming reactor is connected with the output end of the first passage of the heat exchange equipment; the input end of the reactant recovery equipment is connected with the output end of the tube pass of the reforming reactor through a pipeline; the external heat supply equipment comprises an external hot gas circulating pipeline, and the hot gas circulating pipeline passes through the second passage of the heat exchange equipment and the shell pass of the reforming reactor so as to supply heat to the heat exchange equipment and the reforming reactor. According to the methanol hydrogen production system, hot gas can be provided through the hot gas circulating pipeline on the external heat supply equipment, heat is provided for the heat exchange equipment and the reforming reactor through hot gas circulation, the process is simplified, energy is saved, energy consumption is reduced, and meanwhile the danger of hydrogen production equipment is greatly reduced.

Description

Technical Field

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

[0002] Traditional methods of producing one ton of steel emit 1.5 to 3 tons of carbon dioxide. Globally, approximately 2 billion tons are produced annually, a staggering figure. According to statistics, the high emissions from the steel industry account for 7 to 9% of global emissions. Therefore, hydrogen-based ironmaking is an effective way to optimize the steel industry's energy mix, process flow, and industrial structure, ultimately achieving low-carbon, green, and sustainable development. In recent years, hydrogen energy research has advanced rapidly, yielding numerous achievements and applications. Hydrogen production methods primarily include water electrolysis and chemical production. Water electrolysis is less widely used due to its high energy consumption, high risk, and limited production capacity. Utility Model Content

[0003] In order to solve the above problems, the utility model proposes a methanol hydrogen production system, which can use an external heat source to provide heat to the hydrogen production system, thereby reducing carbon emissions to the greatest extent.

[0004] In order to achieve the above purpose, the technical solution adopted by the utility model is:

[0005] A methanol hydrogen production system, comprising:

[0006] A methanol water supply device, used for providing methanol water;

[0007] A heat exchange device, wherein the input end of the first passage is connected to the output end of the methanol water supply device via a pipeline, and the heat exchange device is used to heat the methanol water and gasify it to form methanol water vapor;

[0008] a reforming reactor, the input end of the tube side of which is connected to the output end of the first passage of the heat exchange device, the reforming reactor being used to decompose methanol vapor to produce hydrogen;

[0009] a reactant recovery device, the input end of which is connected to the output end of the tube side of the reforming reactor through a pipeline, and is used to process the decomposition products of methanol and water vapor;

[0010] An external heat supply device includes an external hot gas circulation pipeline, which passes through the second passage of the heat exchange device and the shell side of the reforming reactor to supply heat to the heat exchange device and the reforming reactor.

[0011] Preferably, the methanol water supply device includes a methanol water tank and a booster pump, the input end of the booster pump is connected to the methanol water tank through a pipeline, and the output end of the booster pump is connected to the input end of the first passage of the heat exchange equipment through a pipeline to provide pressurized methanol water to the first passage of the heat exchange equipment.

[0012] Preferably, the heat exchange equipment includes a heat exchanger and a superheater, wherein the input end of the first passage of the heat exchanger is connected to the output end of the methanol water supply device through a pipeline, the output end of the first passage of the heat exchanger is connected to the input end of the first passage of the superheater through a pipeline, and the output end of the first passage of the superheater is connected to the input end of the tube side of the reforming reactor through a pipeline.

[0013] Preferably, the output end of the shell side of the reforming reactor is connected to the input end of the second passage of the heat exchanger through a pipeline, and the output end of the second passage of the heat exchanger is connected to the input end of the reactant recovery device.

[0014] Preferably, the hot gas circulation pipeline passes through the second passage of the heat exchange device and the shell side of the reforming reactor in sequence.

[0015] Preferably, the external heat supply equipment is a steelmaking furnace.

[0016] Preferably, the hot gas circulation pipeline is a water vapor circulation pipeline.

[0017] Preferably, the reactant recovery device comprises an MDEA system, and the MDEA system comprises an output end and two output ends;

[0018] The first output end of the MDEA system is a CO2 gas output end, and the first output end of the MDEA system is connected to the CO2 liquefaction system through a pipeline;

[0019] The second output end of the MDEA system is a reducing gas output end, and the second output end of the MDEA system is connected to a buffer tank through a pipeline.

[0020] The beneficial effects of using the utility model are:

[0021] This methanol-to-hydrogen system utilizes hot gas circulation piping connected to an external heat supply device to provide heat to the heat exchanger and reforming reactor. This high-temperature gas circulation replaces fuel combustion for heating and provides heat for the methanol steam reforming process. This simplifies the process, saves energy, reduces energy consumption, and significantly reduces the risk of hydrogen production equipment. Furthermore, the use of the MDEA system in the hydrogen production system improves CO2 absorption performance, helping to reduce energy consumption throughout the recovery process and minimize byproduct formation. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 This is a schematic diagram of the methanol hydrogen production system of the present invention.

[0023] Reference numerals include:

[0024] 1-Methanol water tank, 2-Booster pump, 3-Heat exchanger, 4-Superheater, 5-Reforming reactor, 6-MDEA system, 7-Buffer tank, 8-CO2 liquefaction system, 9-Steelmaking furnace. DETAILED DESCRIPTION

[0025] In order to make the purpose, technical solution and advantages of this technical solution more clear, the following technical solution is further described in detail in conjunction with specific implementation methods. It should be understood that these descriptions are only exemplary and are not intended to limit the scope of this technical solution.

[0026] In order to solve the problems of high energy consumption, high risk, limited production capacity and less application of hydrogen production equipment in existing technologies, such as Figure 1 As shown, this embodiment provides a methanol-to-hydrogen system. Specifically, a methanol water tank 1 stores and supplies methanol water. The input end of a booster pump 2 is connected to the methanol water tank 1. The methanol water is pressurized by the booster pump 2 and then fed to the rear end. The output end of the booster pump 2 is connected to the input end of the first passage of a heat exchanger 3, which is in turn connected to the input end of the first passage of a superheater 4. The methanol water is heated to a predetermined temperature after passing through the heat exchanger 3. The output end of the first passage of the superheater 4 is connected to the input end of the tube side of a reforming reactor 5. The heated methanol water is vaporized after passing through the heat exchanger 3 to form methanol vapor. In this embodiment, the predetermined temperature of the methanol vapor is 380°C-450°C and the pressure is 2-3 MPa.

[0027] Methanol water is fed into the tube side of the reforming reactor 5 in gaseous form. The vaporized methanol water vapor enters the tube side of the reforming reactor 5 and undergoes a reforming reaction over the catalyst, producing a mixed reformed gas including H2, CO2, CO, and H2O. The reforming reaction is an endothermic reaction. The steelmaking furnace 9 provides a hot gas circulation pipeline, within which high-temperature steam circulates. In this embodiment, the high-temperature steam has a temperature of 450-500°C and a pressure of 4.0-5.0 MPa. The high-temperature steam passes through the shell side of the reforming reactor 5, providing heat to the high-temperature steam tube side. The steam passing through the reforming reactor 5 then enters the second passage of the superheater 4, providing heat to the superheater 4, utilizing the waste heat of the high-temperature steam.

[0028] The output end of the tube side of the reforming reactor 5 is connected to the second passage of the heat exchanger 3. The gas obtained after the reforming reaction in the reforming reactor 5 has a relatively high temperature. After the gas is passed into the second passage of the heat exchanger 3, it provides heat for heating the methanol water.

[0029] The gas produced after the reforming reaction in reforming reactor 5 passes through heat exchanger 3 and enters MDEA system 6. The activated MDEA aqueous solution absorbs CO2 from the gas at high pressure and room temperature. The CO2 is then desorbed from the solvent under reduced pressure and heating. The resulting CO2 gas is then liquefied in CO2 liquefaction system 8 to produce product CO2. The CO2-free gas becomes hydrogen-rich reducing gas, which enters buffer tank 7 to provide reducing gas.

[0030] The MDEA system 6 in this embodiment is highly selective and has a high selectivity for the absorption of CO2, which means that it can effectively and selectively absorb CO2 from a mixed gas containing other gases. The MDEA system 6 absorbent can generally effectively absorb and desorb CO2 at a lower energy input, which helps to reduce the energy consumption of the entire recovery process. The CO2 recovered by the MDEA system 6 is generally of high purity, which is very important for selling CO2 as a product or using it for other industrial applications. The MDEA system 6 can reduce the formation of by-products during the CO2 recovery process, thereby reducing the need and cost for subsequent processing of the by-products. The MDEA system 6 supports the development of carbon capture and storage technology, which helps to reduce greenhouse gas emissions and combat global climate change.

[0031] The above content is only a preferred embodiment of the present invention. For ordinary technicians in this field, many changes can be made in the specific implementation methods and application scope based on the ideas of the present technical content. As long as these changes do not deviate from the concept of the present invention, they all fall within the scope of protection of this patent.

Claims

1. A methanol hydrogen production system, characterized by: include: A methanol water supply device, used for providing methanol water; A heat exchange device, wherein the input end of the first passage is connected to the output end of the methanol water supply device via a pipeline, and the heat exchange device is used to heat the methanol water and gasify it to form methanol water vapor; a reforming reactor, the input end of the tube side of which is connected to the output end of the first passage of the heat exchange device, the reforming reactor being used to decompose methanol vapor to produce hydrogen; a reactant recovery device, the input end of which is connected to the output end of the tube side of the reforming reactor through a pipeline, and is used to process methanol water vapor decomposition products; an external heat supply device, the external heat supply device including an external hot gas circulation pipeline, the hot gas circulation pipeline passing through the second passage of the heat exchange device and the shell side of the reforming reactor to provide heat to the heat exchange device and the reforming reactor; The external heat supply equipment is a steelmaking furnace.

2. The methanol-to-hydrogen system according to claim 1, characterized in that: The methanol water supply device includes a methanol water tank and a booster pump, the input end of the booster pump is connected to the methanol water tank through a pipeline, and the output end of the booster pump is connected to the input end of the first passage of the heat exchange equipment through a pipeline to provide pressurized methanol water to the first passage of the heat exchange equipment.

3. The methanol-to-hydrogen system according to claim 1, characterized in that: The heat exchange equipment includes a heat exchanger and a superheater, wherein the input end of the first passage of the heat exchanger is connected to the output end of the methanol water supply device through a pipeline, the output end of the first passage of the heat exchanger is connected to the input end of the first passage of the superheater through a pipeline, and the output end of the first passage of the superheater is connected to the input end of the tube side of the reforming reactor through a pipeline.

4. The methanol-to-hydrogen system according to claim 3, characterized in that: The output end of the shell side of the reforming reactor is connected to the input end of the second passage of the heat exchanger through a pipeline, and the output end of the second passage of the heat exchanger is connected to the input end of the reactant recovery device.

5. The methanol-to-hydrogen system according to claim 1, characterized in that: The hot gas circulation pipeline passes through the second passage of the heat exchange device and the shell side of the reforming reactor in sequence.

6. The methanol-to-hydrogen system according to claim 1, characterized in that: The hot gas circulation pipeline is a water vapor circulation pipeline.

7. The methanol-to-hydrogen system according to any one of claims 1 to 6, characterized in that: The reactant recovery device includes an MDEA system, and the MDEA system includes an output end and two output ends; The first output end of the MDEA system is a CO2 gas output end, and the first output end of the MDEA system is connected to the CO2 liquefaction system through a pipeline; The second output end of the MDEA system is a reducing gas output end, and the second output end of the MDEA system is connected to a buffer tank through a pipeline.

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