Methanol reforming hydrogen production system capable of controlling temperature through heat conduction oil

Abstract

The utility model relates to a methanol reforming hydrogen production system capable of performing temperature control through heat conduction oil, which comprises a reforming methanol source, a heating methanol source, a gas source, a heater, a primary evaporator, a secondary evaporator and a reformer, the reforming methanol source is sequentially connected with a primary vaporization side of the primary evaporator, a secondary overheating side of the secondary evaporator and a reforming side of the reformer through pipelines, and an output end of the reforming side is connected with a reforming gas tank; the heating methanol source and the gas source are sequentially connected with the burner end of the heater and the smoke flow channel end of the primary evaporator through pipelines, and the heated end of the heater, the reforming heat supply side of the reformer and the evaporation heat supply side of the secondary evaporator form a loop through a heat conduction oil pipeline. High-temperature-resistant oil liquid is adopted, and the temperature of the reformer is controlled through the high-temperature-resistant oil liquid. And under the same reaction condition, the gas-liquid heat exchange efficiency of the heat-conducting oil is higher, so that the temperature difference between the front part and the rear part of the reformer can be better controlled, and the reforming reaction is stably carried out.

Description

Technical Field

[0001] The utility model relates to the technical field of a methanol hydrogen production device, and in particular to a methanol reforming hydrogen production system which performs temperature control through heat transfer oil. Background Art

[0002] With the development of new energy, the hydrogen energy industry is rapidly rising. Hydrogen can be used as a fuel source for fuel cells or as a fuel source for hydrogen internal combustion engines. It is the ultimate energy source for achieving low-carbon and environmental protection. As one of the ways to produce hydrogen, methanol steam reforming reaction has received widespread attention due to its low cost, relatively mild reaction conditions and abundant resources, and has become an ideal hydrogen source. Among them, the stability of the performance of the methanol steam reforming hydrogen production reactor as a key component determines the performance of hydrogen production. The reforming reaction is an endothermic reaction, and the reaction process requires a large amount of heat to be supplied externally, so it is easy to cause a large temperature difference between the front and back of the reactor. For example, the common methanol autothermal reforming hydrogen production reactor currently uses the hot flue gas of methanol oxidation to heat the reforming reaction of methanol steam, and the maximum temperature difference before and after can reach 100°C. This leads to incomplete and uneven reforming reaction, unstable and difficult to control reformer temperature. Utility Model Content

[0003] The technical problem to be solved by the utility model is to provide a methanol reforming hydrogen production system which controls the temperature through heat transfer oil, thereby improving the temperature stability of the reformer and ensuring uniform and complete reforming reaction.

[0004] The utility model solves the technical problem by adopting the following technical scheme: providing a methanol reforming hydrogen production system which controls the temperature through heat transfer oil, comprising a reforming methanol source, a heating methanol source, a gas source, a heater, a primary evaporator, a secondary evaporator and a reformer, wherein the reforming methanol source is connected with the primary vaporization side of the primary evaporator, the secondary overheating side of the secondary evaporator and the reforming side of the reformer in sequence through pipelines, the output end of the reforming side is connected with the reforming gas tank, the heating methanol source and the gas source are connected with the burner end of the heater and the flue gas flow channel end of the primary evaporator in sequence through pipelines, the heated end of the heater, the heating side of the reformer and the heating side of the secondary evaporator form a loop through the heat transfer oil pipeline, and a circulating pump is arranged in the loop.

[0005] Preferably, the reforming methanol source and the heating methanol source are methanol water tanks, and the methanol water tanks are provided with input valves.

[0006] Preferably, the air source is an exhaust fan.

[0007] Preferably, the front end of the heater is connected to an electric heating device, and a temperature control device is provided inside the heater. Beneficial Effects

[0008] The utility model adopts high temperature resistant oil with higher specific heat to control the temperature of the reformer through high temperature oil. Under the same reaction conditions, the heat carried by the liquid itself is higher, and the efficiency of gas-liquid heat exchange is also higher, so the temperature difference before and after the reformer can be better controlled, so that the reforming reaction can proceed stably.

[0009] At the same time, the heat transfer oil that has been partially cooled after passing through the reformer is heated again through the secondary evaporator. The high-temperature exhaust gas generated by the heater heats the methanol water in the primary evaporator when passing through the flue gas flow duct, effectively realizing the efficient utilization of the raw methanol water. BRIEF DESCRIPTION OF THE DRAWINGS

[0010] Figure 1 This is a schematic diagram of the structure of a methanol reforming hydrogen production system that uses heat transfer oil for temperature control.

[0011] Figure 2 The figure is a flow chart of a methanol reforming hydrogen production system with temperature control through heat transfer oil.

[0012] Among them, 1-heater; 101-burner end; 102-heating end; 2-primary evaporator; 201-primary vaporization side; 202-flue gas flow duct; 3-secondary evaporator; 301-evaporation heating side; 302-secondary superheating side; 4-reformer; 401-reforming heating side; 402-reforming side; 5-circulation pump; 6-heating methanol source; 7-gas source; 8-reforming methanol source; 9-reforming gas tank; 10-heat transfer oil pipeline.

[0013] The same reference numerals in the various drawings represent the same components. DETAILED DESCRIPTION

[0014] The present invention is further described below in conjunction with specific embodiments. It should be understood that these embodiments are only used to illustrate the present invention and are not used to limit the scope of the present invention. In addition, it should be understood that after reading the content taught by the present invention, those skilled in the art can make various changes or modifications to the present invention, and these equivalent forms also fall within the scope defined by the claims attached to this application.

[0015] like Figure 1 , 2As shown, the utility model provides a methanol reforming hydrogen production system with temperature control through heat transfer oil, comprising a reforming methanol source 8, a heating methanol source 6, a gas source 7, a heater 1, a primary evaporator 2, a secondary evaporator 3 and a reformer 4, wherein the reforming methanol source 8 is connected to the primary vaporization side 201 of the primary evaporator 2, the secondary overheating side 302 of the secondary evaporator 3 and the reforming side 402 of the reformer 4 in sequence through pipelines, and the output end of the reforming side 402 is connected to the reforming gas tank 9, the heating methanol source 6 and the gas source 7 are connected to the burner end 101 of the heater 1 and the flue gas flow channel 202 end of the primary evaporator 2 in sequence through pipelines, the heated end 102 of the heater 1, the reforming heating side 401 of the reformer 4 and the evaporation heating side 301 of the secondary evaporator 3 form a loop through the heat transfer oil pipeline 10, and a circulating pump 5 is provided in the loop.

[0016] In a specific embodiment, the reforming methanol source 8 and the heating methanol source 6 are both methanol water tanks, in which a methanol water mixture is temporarily stored, wherein the water is deionized water. An input valve is provided on the surface of the methanol water tank, and the methanol water mixture can be added to the tank according to the storage in the tank or replaced with a new methanol water tank after disconnection.

[0017] In a specific embodiment, the air source 7 is an exhaust fan, which draws in fresh air and methanol water provided by the heating methanol source 6 and inputs it into the burner end 101 of the heater 1 through a pipeline, and an oxidation reaction occurs in the burner to generate a large amount of heat, so that the temperature of the heat transfer oil passing through the heating end 102 of the heater 1 is increased to the reaction temperature (350±25°C) and first sent to the reforming heating side 401 through the heat transfer oil pipeline 10. The hot flue gas generated by the combustion of methanol water at the burner end 101 passes through the flue gas flow channel 202 of the primary evaporator 2 and is discharged.

[0018] In a specific embodiment, the front end of the heater 1 is connected to an electric heating device, and the heater 1 is preheated to the starting temperature of the catalyst before starting the system. A temperature sensor can be set in the heated end 102 or the reforming side 402 of the reformer 4, and a temperature control device is provided in the heater 1. According to the temperature detected by the temperature sensor, the input amount of the heated methanol source 6 and the gas source 7 is increased or decreased to ensure that the temperature transmitted to the heated side is within the reaction temperature range.

[0019] During use, the circulation pump 5 is first started to allow the heat transfer oil to circulate in the heat transfer oil pipeline 10; the methanol-water mixture to be reformed to produce hydrogen is output from the reforming methanol source 8 (methanol-water tank), first enters the primary vaporization side 201 of the primary evaporator 2, and initially absorbs heat from the flue gas flow duct 202 adjacent thereto to increase the temperature and vaporize; then it is input into the secondary superheating side 302 of the secondary evaporator 3, and absorbs heat from the heat transfer oil passing through the adjacent evaporation heating side 301 for a secondary superheating; finally, it enters the reforming side 402 of the reformer 4, absorbs heat from the heat transfer oil passing through the adjacent reforming heating side 401 to increase the temperature to the reaction temperature, reforms to produce hydrogen, and outputs the reformed gas to the outside.

[0020] The evaporator used in the utility model can be a common commercially available plate heat exchanger, which has the advantages of small size and large heat exchange capacity. The hot side is the flow channel of the heat transfer oil, and the cold side is the flow channel of the methanol water. When the methanol water passes through the flow channel, heat exchange occurs, and the methanol water is heated and evaporated to the temperature required for the reaction.

[0021] The structural form of the reformer used in the utility model includes but is not limited to the stacking and assembly of unit plates. The two sides of the unit plates are respectively provided with flow channels. After being stacked and assembled, an internal core structure is formed. The inlet and outlet end covers on the reforming reaction side and the shunt and confluence pipes on the heating side are matched to encapsulate the core to form a complete reformer. During use, the heat transfer oil enters the flow channel on the heating side through the shunt port and then flows out from the confluence port, while the methanol water vapor enters the reforming side flow channel from the inlet. Under the action of the catalyst, a reforming reaction occurs. The reforming reaction is an endothermic reaction. The required heat is provided by the heat transfer oil in the adjacent flow channel. The specific heat of the heat transfer oil is relatively large, so the temperature of the entire reformer can be maintained within the temperature range required for a stable reaction. The reformed mixed gas after reforming is discharged through the outlet and enters the next link.

Claims

1. A methanol reforming hydrogen production system with temperature control by heat transfer oil, characterized in that: The invention comprises a reforming methanol source (8), a heating methanol source (6), a gas source (7), a heater (1), a primary evaporator (2), a secondary evaporator (3) and a reformer (4); the reforming methanol source (8) is connected to the primary vaporization side (201) of the primary evaporator (2), the secondary superheating side (302) of the secondary evaporator (3) and the reforming side (402) of the reformer (4) in sequence through pipelines; the output end of the reforming side (402) is connected to a reforming gas tank (9); The heating methanol source (6) and the gas source (7) are connected to the burner end (101) of the heater (1) and the flue gas flow channel (202) end of the primary evaporator (2) in sequence through pipelines. The heat receiving end (102) of the heater (1), the reforming heat supply side (401) of the reformer (4), and the evaporation heat supply side (301) of the secondary evaporator (3) form a loop through a heat transfer oil pipeline (10), and a circulation pump (5) is provided in the loop.

2. A methanol reforming hydrogen production system using heat transfer oil for temperature control according to claim 1, characterized in that: The reforming methanol source (8) and the heating methanol source (6) are methanol water tanks, and the methanol water tanks are provided with input valves.

3. A methanol reforming hydrogen production system with temperature control by heat transfer oil according to claim 1, characterized in that: The air source (7) is an exhaust fan.

4. A methanol reforming hydrogen production system with temperature control by heat transfer oil according to claim 1, characterized in that: The front end of the heater (1) is connected to an electric heating device, and a temperature control device is provided inside the heater (1).

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