A methanol-to-hydrogen device
By optimizing the methanol-to-hydrogen unit through modular integration and a closed-loop system, the problems of low energy conversion efficiency and resource waste in existing technologies have been solved, achieving efficient hydrogen production and low carbon emissions.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- SICHUAN FENGDE TIANNENG ENERGY EQUIPMENT CO LTD
- Filing Date
- 2025-06-18
- Publication Date
- 2026-07-03
AI Technical Summary
Existing methanol-to-hydrogen systems suffer from low energy conversion efficiency, insufficient chemical reaction efficiency, poor system integration, low heat recovery rate, and serious resource waste, resulting in low hydrogen yield, high carbon emissions, and low resource utilization.
The modular integrated methanol-to-hydrogen unit optimizes the linear layout of gasification-reforming-cooling-separation through waste heat recovery design and closed-loop system. It utilizes heat transfer oil circulation to preheat the raw materials and realize the recycling of reaction water, thereby improving heat utilization and resource utilization.
It increased hydrogen production by 15%-20%, reduced energy consumption by 10%-15%, extended catalyst life, and achieved high space utilization and water resource recycling, thus reducing carbon emissions.
Smart Images
Figure CN224442956U_ABST
Abstract
Description
Technical Field
[0001] This utility model relates to the technical field of methanol-to-hydrogen systems, specifically to a methanol-to-hydrogen device. Background Technology
[0002] As the global energy structure transitions towards a low-carbon model, hydrogen energy has become an important energy carrier due to its zero-carbon emission characteristics. However, traditional hydrogen production technologies, such as coal-to-hydrogen and natural gas reforming, suffer from high carbon emissions, while water electrolysis for hydrogen production is limited by high electricity prices and low efficiency, hindering large-scale deployment. Furthermore, hydrogen storage and transportation face challenges such as poor safety and high costs, restricting the development of the hydrogen energy industry. Methanol (CH3OH), with its high hydrogen content (12.5 wt%), ease of liquid storage and transportation, and wide availability (synthesized from fossil fuels or renewable energy sources), is considered an ideal hydrogen carrier.
[0003] Existing methanol-to-hydrogen systems are inefficient, mainly due to the following key technological bottlenecks and system design flaws:
[0004] 1. Low energy conversion efficiency and large heat loss during gasification: Traditional systems use direct electric heating or combustion heating for the gasifier, resulting in uneven heat transfer and a thermal efficiency of only 50%-60%. 2. Insufficient preheating of raw materials: In traditional systems, methanol and demineralized water enter the gasifier at room temperature, requiring an additional 20%-30% energy to heat them to the gasification temperature (above 250℃).
[0005] Second, the chemical reaction efficiency is insufficient, the reforming reaction is incomplete, the catalyst in the traditional system is prone to sintering (due to large temperature fluctuations), the methanol conversion rate is only 85%-90%, and the byproduct CO content is high (3%-5%). The water-gas shift reaction is incomplete, the cooling rate of the traditional system is slow (>10 seconds), resulting in incomplete reaction of CO with water vapor (CO+H2O→CO2+H2), and the hydrogen purity is only below 99%.
[0006] Third, the system suffers from poor integration and low heat recovery rate. Traditional systems directly discharge high-temperature condensate (60-80℃) from the cooler, resulting in a waste heat utilization rate of <10%. Space utilization is also insufficient; traditional systems have dispersed components, long piping, and significant heat loss, resulting in a volumetric power density of <0.5kW / m³. 3 .
[0007] Fourth, there is serious waste of resources, with high water consumption. In traditional systems, 5-6 kg of demineralized water is required to produce 1 kg of hydrogen, and the condensate is discharged directly. There is also residual methanol loss; the separator wastewater in traditional systems contains 2%-3% unreacted methanol, and direct discharge results in low raw material utilization. Utility Model Content
[0008] This invention provides a methanol-to-hydrogen device that improves hydrogen yield, extends catalyst life, and reduces carbon emissions through waste heat recovery design and modular integration. It is suitable for distributed energy, mobile hydrogen sources, and industrial hydrogen applications.
[0009] To achieve the above objectives, this utility model provides the following technical solution: a methanol-to-hydrogen device, comprising: a frame, the frame being a rectangular hollow structure; a vaporizer, the vaporizer being fixedly installed within the frame, and the vaporizer having a first feed port, a second feed port, and a vaporization outlet; a reforming reactor, the reforming reactor being installed within the frame and located on one side of the vaporizer, the reforming reactor having a feed inlet and a mixed gas outlet, the feed inlet being connected to the vaporization outlet; a cooler, the cooler being installed within the frame and located on one side of the reforming reactor, the cooler having a high-temperature inlet and a condensation outlet, the high-temperature inlet being connected to the mixed gas outlet; and a separator, the separator being installed within the frame and located on one side of the cooler, the separator having a liquid inlet and a purification outlet, the liquid inlet being connected to the condensation outlet.
[0010] Preferably, it also includes a heat transfer oil tank, a heating unit, and a heating pump; the vaporizer is provided with a pair of heating circulation ports, and forms a circulation loop with the heat transfer oil tank, the heating unit, and the heating pump through the heating circulation ports.
[0011] Preferably, the heat transfer oil tank is provided with a methanol pipeline and a demineralized water pipeline running through it. The methanol pipeline and the demineralized water pipeline are respectively connected to the corresponding first feed port and second feed port via a raw material pump.
[0012] Preferably, a cooling circulation pump is fixedly installed inside the frame; the cooler is provided with a first circulation interface and a second circulation interface, and the first circulation interface and the second circulation interface respectively form a circulation loop with the cooling circulation pump.
[0013] Preferably, the separator is provided with a drain outlet at the bottom, and the drain outlet is connected to the input end of the demineralized water pipeline through a return water pipe.
[0014] The advantages of this invention are: it allows for modular installation of each component within a frame, forming a compact hydrogen production system. Methanol and demineralized water are fed into the vaporizer through the first and second feed ports, respectively. The vaporized water is heated and vaporized within the vaporizer, forming a mixture of methanol vapor and water vapor, which is then output from the vaporization outlet. This mixture enters the reforming reactor through the feed port, where a reforming reaction occurs under the action of catalysts such as Cu / ZnO / Al2O3: CH3OH + H2O → 3H2 + CO2, generating a hydrogen-rich mixture containing H2, CO2, and a small amount of CO. The high-temperature mixture enters the cooler from the outlet, where it is cooled to 40-60°C through heat exchange, condensing the water vapor. The gas-liquid mixture enters the separator through the liquid inlet, where it is separated by gravity or centrifugation. Hydrogen is output from the purified outlet, and condensate is discharged from the bottom. This integrated design achieves lightweight construction and high space utilization. Furthermore, the linear layout of vaporization-reforming-cooling-separation optimizes heat transfer and airflow paths, increasing hydrogen yield by 15%-20%. The gasifier forms a closed-loop circulation system with the other three components via a heating circulation port. The heat transfer oil, heated to 200-300℃ by a heating unit consisting of an electric heater or burner, is then pumped to the gasifier's heating circulation port for indirect heating of the material inside the gasifier. The cooled heat transfer oil returns to the heat transfer oil tank for reheating, creating a continuous heating cycle. The heat transfer oil circulation system ensures that the gasifier temperature fluctuation is ≤±5℃, preventing localized overheating. The closed-loop system reduces heat loss and lowers energy consumption by 10%-15%. The heat transfer oil tank contains a continuous methanol and demineralized water pipeline, which are connected to the gasifier's first and second feed ports via feed pumps. As the methanol and demineralized water flow through the pipelines in the heat transfer oil tank, they are preheated to 80-100℃ by the high-temperature heat transfer oil before entering the gasifier. The feed pump precisely controls the feed ratio, maintaining a methanol:water ratio of 1:1 to 1:1.5. Utilizing the waste heat of the heat transfer oil to preheat the feed increases gasification efficiency by 20%. Preheating prevents low-temperature feedstock from directly entering the gasifier and causing coking. Cooling water, driven by a cooling circulation pump, flows through the high-temperature inlet side of the cooler, absorbing heat from the mixed gas before returning to the cooling tower or heat exchanger for further cooling, forming a circulating cooling system. The cooling temperature is controlled within the range of 40-60℃ by a flow valve. This circulating cooling reduces the cooling time of the mixed gas to 3-5 seconds, preventing heavy components from condensing and clogging pipes. The closed-loop system reduces cooling water consumption by more than 30%. The condensate discharged from the separator flows back to the demineralized water pipeline via a return water pipe, mixes with fresh demineralized water, and participates in the reaction again, achieving water recycling with a water resource utilization rate of over 95%. It also allows for the recovery of unreacted methanol, increasing the total hydrogen yield by 2%-3%. Attached Figure Description
[0015] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.
[0016] Figure 1 This is a schematic diagram of the overall structure of this utility model.
[0017] In the diagram: 1. Frame; 2. Gasifier; 3. Reformer; 4. Cooler; 5. Separator; 6. Heat transfer oil tank; 7. Heating unit; 8. Heating pump; 9. Cooling circulation pump; 10. Return water pipe; 11. Methanol pipeline; 12. Demineralized water pipeline; 13. Purification outlet; 14. Raw material pump. Detailed Implementation
[0018] The technical solution of this utility model will now be clearly and completely described with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this utility model, and not all embodiments. Based on the embodiments of this utility model, all other embodiments obtained by those skilled in the art without creative effort are within the protection scope of this utility model.
[0019] according to Figure 1 As shown, a methanol-to-hydrogen apparatus includes: a frame 1, which has a rectangular hollow structure; a vaporizer 2, which is fixedly installed inside the frame 1 and has a first feed port, a second feed port, and a vaporization outlet; a reforming reactor 3, which is installed inside the frame 1 and located on one side of the vaporizer 2, and has a feed inlet and a mixed gas outlet, the feed inlet being connected to the vaporization outlet; a cooler 4, which is installed inside the frame 1 and located on one side of the reforming reactor 3, and has a high-temperature inlet and a condensation outlet, the high-temperature inlet being connected to the mixed gas outlet; and a separator 5, which is installed inside the frame 1 and located on one side of the cooler 4, and has a liquid inlet and a purification outlet 13, the liquid inlet being connected to the condensation outlet.
[0020] The above configuration allows for modular installation of all components within the frame 1, forming a compact hydrogen production system. Methanol and demineralized water are fed into the vaporizer 2 through the first and second feed ports, respectively. The vaporized water is heated and vaporized within the vaporizer 2, forming a mixture of methanol vapor and water vapor, which is then output from the vaporization outlet. This mixture enters the reforming reactor 3 through the feed port, where a reforming reaction occurs under the action of catalysts such as Cu / ZnO / Al2O3: CH3OH + H2O → 3H2 + CO2, generating a hydrogen-rich mixture containing H2, CO2, and a small amount of CO. The high-temperature mixture enters the cooler 4 from the outlet, where it is cooled to 40-60°C through heat exchange, condensing the water vapor. The gas-liquid mixture enters the separator 5 from the inlet, where it is separated by gravity or centrifugation. Hydrogen is output from the purification outlet 13, and condensate is discharged from the bottom. This integrated design achieves lightweight construction and high space utilization. Furthermore, the linear layout of vaporization-reforming-cooling-separation optimizes heat transfer and airflow paths, increasing hydrogen yield by 15%-20%.
[0021] It also includes a heat transfer oil tank 6, a heating unit 7 and a heating pump 8; the vaporizer 2 is provided with a pair of heating circulation ports, and forms a circulation loop with the heat transfer oil tank 6, the heating unit 7 and the heating pump 8 through the heating circulation ports.
[0022] In this setup, the vaporizer 2 forms a closed-loop circulation system with the other three components via a heating circulation port. The heat transfer oil is heated to 200-300℃ by the heating unit 7, which consists of an electric heater or burner, and then pumped by the heating pump 8 to the heating circulation port of the vaporizer 2, indirectly heating the material inside. The cooled heat transfer oil returns to the heat transfer oil tank 6 for reheating, forming a continuous heating cycle. The heat transfer oil circulation system ensures that the temperature fluctuation of the vaporizer 2 is ≤±5℃, preventing localized overheating. The closed-loop system reduces heat loss and lowers energy consumption by 10%-15%.
[0023] The heat transfer oil tank 6 is provided with a methanol pipeline 11 and a demineralized water pipeline 12 running through it. The methanol pipeline 11 and the demineralized water pipeline 12 are respectively connected to the first feed port and the second feed port through the raw material pump 14.
[0024] The heat transfer oil tank 6 contains a methanol pipeline 11 and a demineralized water pipeline 12, which are connected to the first and second feed ports of the gasifier 2 via a feed pump 14. As the methanol and demineralized water flow through the pipelines in the heat transfer oil tank 6, they are preheated to 80-100°C by the high-temperature heat transfer oil before entering the gasifier 2. The feed pump 14 precisely controls the feed ratio, ensuring a methanol:water ratio of 1:1 to 1:1.5. Utilizing the waste heat of the heat transfer oil to preheat the feedstock increases the gasification efficiency by 20%. Preheating prevents low-temperature feedstock from directly entering the gasifier 2 and causing coking.
[0025] A cooling circulation pump 9 is fixedly installed inside the frame 1; the cooler 4 is provided with a first circulation interface and a second circulation interface, and the first circulation interface and the second circulation interface respectively form a circulation loop with the cooling circulation pump 9.
[0026] In this setup, cooling water, driven by cooling circulation pump 9, flows through the high-temperature inlet side of cooler 4, absorbs heat from the mixed gas, and then returns to the cooling tower or heat exchanger for further cooling, forming a circulating cooling system. The cooling temperature is controlled within the range of 40-60℃ by a flow valve. This circulating cooling reduces the cooling time of the mixed gas to 3-5 seconds, preventing heavy components from condensing and clogging the pipes. The closed-loop system reduces cooling water consumption by more than 30%.
[0027] The separator 5 is provided with a drain outlet at the bottom, and the drain outlet is connected to the input end of the demineralized water pipe 12 through the return water pipe 10.
[0028] In this setup, the condensate discharged from separator 5 is returned to demineralized water pipe 12 via return water pipe 10, mixed with fresh demineralized water, and then participates in the reaction again, realizing the recycling of reaction water. The water resource utilization rate reaches over 95%, and the recovery of unreacted methanol increases the total hydrogen production rate by 2%-3%.
[0029] The above description is merely a specific embodiment of this utility model, but the protection scope of this utility model is not limited thereto. Any variations or substitutions that can be easily conceived by those skilled in the art within the technical scope disclosed in this utility model should be included within the protection scope of this utility model. Therefore, the protection scope of this utility model should be determined by the scope of the claims.
Claims
1. A methanol-to-hydrogen device, characterized in that, include: The frame (1) is a rectangular hollow structure; A gasifier (2) is fixedly installed inside the frame (1), and the gasifier (2) is provided with a first feed port, a second feed port and a gasification outlet; A reforming reactor (3) is installed inside the frame (1) and located on one side of the gasifier (2). The reforming reactor (3) is provided with a feed inlet and a mixed gas outlet, and the feed inlet is connected to the gasification outlet. Cooler (4), the cooler (4) is installed in the frame (1) and located on one side of the reforming reactor (3), the cooler (4) is provided with a high temperature inlet and a condensation outlet, the high temperature inlet is connected to the mixed gas outlet; A separator (5) is installed inside the frame (1) and located on one side of the cooler (4). The separator (5) is provided with an inlet and a purification outlet (13). The inlet is connected to the condensation outlet.
2. The device for producing hydrogen from methanol according to claim 1, characterized in that: It also includes a heat transfer oil tank (6), a heating unit (7) and a heating pump (8); the vaporizer (2) is provided with a pair of heating circulation ports, and forms a circulation loop with the heat transfer oil tank (6), the heating unit (7) and the heating pump (8) through the heating circulation ports.
3. The device for producing hydrogen from methanol according to claim 2, characterized in that: The heat transfer oil tank (6) is provided with a methanol pipeline (11) and a demineralized water pipeline (12) running through it. The methanol pipeline (11) and the demineralized water pipeline (12) are respectively connected to the first feed port and the second feed port through the raw material pump (14).
4. The device for producing hydrogen from methanol according to claim 1, characterized in that: The frame (1) is fixedly equipped with a cooling circulation pump (9); the cooler (4) is provided with a first circulation interface and a second circulation interface, and the first circulation interface and the second circulation interface respectively form a circulation loop with the cooling circulation pump (9).
5. The device for producing hydrogen from methanol according to claim 3, characterized in that: The separator (5) has a drain outlet at the bottom, which is connected to the input end of the demineralized water pipe (12) through a return water pipe (10).