Skid-mounted methanol high-temperature reforming hydrogen production device

Abstract

The utility model relates to a skid-mounted methanol high-temperature reforming hydrogen production device which comprises a reforming reactor, a palladium membrane purifier, a catalytic reactor and a multi-stage heat exchanger, and a pipeline between the output end of a shell pass of the reforming reactor and a carbon dioxide capture interface passes through the multi-stage heat exchanger; a pipeline between the methanol water supply interface and the input end of the reforming reactor tube pass passes through the multi-stage heat exchanger, and a pipeline between the compressed air inlet interface and the input end of the catalytic reactor passes through the multi-stage heat exchanger; a pipeline between the output end of the reforming reactor shell pass and the carbon dioxide capture interface and a pipeline between the methanol water supply interface and the input end of the reforming reactor tube pass exchange heat and form a third heat exchange node; and a pipeline between the output end of the reforming reactor shell pass and the carbon dioxide capture interface and a pipeline between the compressed air inlet interface and the input end of the catalytic reactor exchange heat and form a fourth heat exchange node. The device can improve the heat exchange efficiency of byproducts and raw materials.

Description

Technical Field

[0001] The utility model relates to the technical field of methanol-water hydrogen production, in particular to a skid-mounted methanol high-temperature reforming hydrogen production device. Background Art

[0002] The equipment for producing hydrogen by high temperature reforming of methanol in the prior art mostly adopts large-scale equipment. For example, large-scale equipment is connected to each other by pipelines. Such equipment is suitable for large-scale hydrogen production in factories, but cannot be skid-mounted and transported by towing vehicles.

[0003] In addition, due to equipment limitations, the heat required for the endothermic cracking of methanol and water needs to be supplied separately for the high-temperature reforming of methanol to produce hydrogen. At the same time, the heat released by the oxidation of carbon monoxide in the by-product is wasted. Although some technologies use heat exchangers for heat exchange, the heat exchange efficiency is not high. Utility Model Content

[0004] In order to solve the above problems, the utility model proposes a skid-mounted methanol high-temperature reforming hydrogen production device, which can increase the temperature of incoming raw materials, improve the heat exchange efficiency between by-products and raw materials, and can be skid-mounted for transportation.

[0005] In order to achieve the above purpose, the technical solution adopted by the utility model is:

[0006] A skid-mounted methanol high-temperature reforming hydrogen production device comprises a reforming reactor, a palladium membrane purifier, a catalytic reactor and a multi-stage heat exchanger, wherein the input end of the tube side of the reforming reactor is connected to a methanol water supply interface through a pipeline, the output end of the tube side of the reforming reactor is connected to the input end of the palladium membrane purifier through a pipeline, the palladium membrane purifier has two output ends, the first output end of the palladium membrane purifier is a hydrogen output end, the first output end of the palladium membrane purifier is connected to a hydrogen outflow interface through a pipeline, the second output end of the palladium membrane purifier is a by-product gas output end, the second output end of the palladium membrane purifier is connected to the input end of the catalytic reactor through a pipeline, the input end of the catalytic reactor is also connected to a compressed air inlet interface through a pipeline, the output end of the catalytic reactor is connected to the input end of the reforming reactor shell side through a pipeline, and the output end of the reforming reactor shell side is connected to a carbon dioxide capture interface through a pipeline;

[0007] The pipeline between the output end of the reforming reactor shell side and the carbon dioxide capture interface passes through a multi-stage heat exchanger, the pipeline between the methanol water supply interface and the input end of the reforming reactor tube side passes through a multi-stage heat exchanger, and the pipeline between the compressed air inlet interface and the input end of the catalytic reactor passes through a multi-stage heat exchanger;

[0008] The pipeline between the output end of the reforming reactor shell side and the carbon dioxide capture interface, and the pipeline between the methanol water supply interface and the input end of the reforming reactor tube side exchange heat and form a third heat exchange node;

[0009] The pipeline between the output end of the reforming reactor shell and the carbon dioxide capture interface, and the pipeline between the compressed air inlet interface and the input end of the catalytic reactor exchange heat and form a fourth heat exchange node.

[0010] Preferably, in the flow direction of the fluid in the pipeline between the output end of the reforming reactor shell side and the carbon dioxide capture interface, the third heat exchange node is located in front of the fourth heat exchange node.

[0011] Preferably, the pipeline between the first output end of the palladium membrane purifier and the hydrogen flow outflow interface passes through a multi-stage heat exchanger, and the pipeline between the first output end of the palladium membrane purifier and the hydrogen flow outflow interface, and the pipeline between the methanol water supply interface and the input end of the reforming reactor tube side exchange heat to form a second heat exchange node.

[0012] Preferably, in the flow direction of the fluid in the pipeline between the methanol water supply interface and the input end of the palladium membrane purifier tube, the second heat exchange node is located in front of the third heat exchange node.

[0013] Preferably, the pipeline between the output end of the reforming reactor shell side and the carbon dioxide capture interface passes through the multi-stage heat exchanger again after passing through the fourth heat exchange node; and

[0014] The pipeline between the output end of the reforming reactor shell side and the carbon dioxide capture interface, and the pipeline between the methanol water supply interface and the input end of the reforming reactor tube side exchange heat and form a first heat exchange node.

[0015] Preferably, in the flow direction of the fluid in the pipeline between the methanol water supply interface and the input end of the palladium membrane purifier tube, the first heat exchange node is located in front of the second heat exchange node.

[0016] Preferably, the pipeline between the first output end of the palladium membrane purifier and the hydrogen outflow interface passes through the multi-stage heat exchanger again after passing through the second heat exchange node; and

[0017] The pipeline between the first output end of the palladium membrane purifier and the hydrogen outflow interface, and the pipeline between the compressed air inlet interface and the input end of the catalytic reactor exchange heat and form a fifth heat exchange interface.

[0018] Preferably, in the flow direction of the fluid in the pipeline between the compressed air inlet interface and the input end of the catalytic reactor, the fifth heat exchange node is located in front of the fourth heat exchange node.

[0019] Preferably, an electric heater is provided on the pipeline between the compressed air inlet interface and the input end of the catalytic reactor, and the electric heater is located on the pipeline between the multi-stage heat exchanger and the input end of the catalytic reactor.

[0020] Preferably, the skid-mounted methanol high-temperature reforming hydrogen production device further comprises a skid frame, and the reforming reactor, palladium membrane purifier, catalytic reactor, multi-stage heat exchanger and connecting pipelines are all installed in the skid frame.

[0021] The beneficial effects of using the utility model are:

[0022] This skid-mounted methanol high-temperature reforming hydrogen production device uses a multi-stage heat exchanger to exchange the heat required for methanol water cracking and the heat generated by the oxidation of methanol water cracking byproducts. Through the use of multi-stage heat exchangers, the raw materials used in the device, such as methanol water and air, can be fully preheated; and the heat generated by the methanol water cracking byproducts, such as carbon dioxide, after oxidation, can be fully utilized. The cracking reaction in the reforming reactor is efficient and has few side reactions.

[0023] Compared with the traditional PSA separation process, the palladium membrane purification process eliminates the cooling, washing and gas-liquid separator processes, has a simple process, small equipment size, stable performance, and no waste gas or waste liquid emissions. In addition, due to its high reaction efficiency, this skid-mounted methanol high-temperature reforming hydrogen production device can be miniaturized and convenient for skid dragging and transportation. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] Figure 1 This is a schematic diagram of the skid-mounted methanol high-temperature reforming hydrogen production device of the present invention.

[0025] Figure 2 This is an axial schematic diagram of a skid-mounted methanol high-temperature reforming hydrogen production unit.

[0026] Figure 3 This is an axial schematic diagram of the skid-mounted methanol high-temperature reforming hydrogen production unit from another perspective.

[0027] Reference numerals include:

[0028] 11-methanol water supply interface, 12-boosting pump, 13-reforming reactor, 14-palladium membrane purifier, 15-catalytic reactor, 16-precision filter, 17-electric heater, 18-multi-stage heat exchanger, 19-compressed air inlet interface, 20-flow control valve, 21-hydrogen flow outlet interface, 22-hydrogen venting pipeline, 23-methanol water reflux interface, 24-carbon dioxide capture interface, 25-carbon dioxide venting pipeline, 26-skid frame;

[0029] E1-the first heat exchange node, E2-the second heat exchange node, E3-the third heat exchange node, E4-the fourth heat exchange node, and E5-the fifth heat exchange node. DETAILED DESCRIPTION

[0030] In order to make the purpose, technical solution and advantages of the technical solution more clear, the technical solution is further described in detail below 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 the technical solution.

[0031] In order to solve the problem that the equipment for producing hydrogen by high temperature reforming of methanol wastes heat and is too large to be dragged and transported in the prior art, Figure 1-Figure 3 As shown, this embodiment proposes a skid-mounted methanol high-temperature reforming hydrogen production device, including a reforming reactor 13, a palladium membrane purifier 14, a catalytic reactor 15 and a multi-stage heat exchanger 18, wherein the input end of the tube side of the reforming reactor 13 is connected to the methanol water supply interface 11 through a pipeline, and the output end of the tube side of the reforming reactor 13 is connected to the input end of the palladium membrane purifier 14 through a pipeline. The palladium membrane purifier 14 has two output ends, the first output end of the palladium membrane purifier 14 is a hydrogen output end, the first output end of the palladium membrane purifier 14 is connected to the hydrogen outflow interface 21 through a pipeline, the second output end of the palladium membrane purifier 14 is a by-product gas output end, the second output end of the palladium membrane purifier 14 is connected to the input end of the catalytic reactor 15 through a pipeline, the input end of the catalytic reactor 15 is also connected to the compressed air inlet interface 19 through a pipeline, the output end of the catalytic reactor 15 is connected to the input end of the shell side of the reforming reactor 13 through a pipeline, and the output end of the shell side of the reforming reactor 13 is connected to the carbon dioxide capture interface 24 through a pipeline.

[0032] The pipeline between the output end of the shell side of the reforming reactor 13 and the carbon dioxide capture interface 24 passes through the multi-stage heat exchanger 18, the pipeline between the methanol water supply interface 11 and the input end of the tube side of the reforming reactor 13 passes through the multi-stage heat exchanger 18, and the pipeline between the compressed air inlet interface 19 and the input end of the catalytic reactor 15 passes through the multi-stage heat exchanger 18.

[0033] The pipeline between the output end of the shell side of the reforming reactor 13 and the carbon dioxide capture interface 24, and the pipeline between the methanol water supply interface 11 and the input end of the tube side of the reforming reactor 13 exchange heat and form a third heat exchange node E3. The pipeline between the output end of the shell side of the reforming reactor 13 and the carbon dioxide capture interface 24, and the pipeline between the compressed air inlet interface 19 and the input end of the catalytic reactor 15 exchange heat and form a fourth heat exchange node E4. In the flow direction of the fluid in the pipeline between the output end of the shell side of the reforming reactor 13 and the carbon dioxide capture interface 24, the third heat exchange node E3 is located in front of the fourth heat exchange node E4.

[0034] The pipeline between the first output end of the palladium membrane purifier 14 and the hydrogen gas outlet interface 21 passes through the multi-stage heat exchanger 18, and the pipeline between the first output end of the palladium membrane purifier 14 and the hydrogen gas outlet interface 21, and the pipeline between the methanol water supply interface 11 and the input end of the tube side of the reforming reactor 13 exchange heat and form a second heat exchange node E2. In the flow direction of the fluid in the pipeline between the methanol water supply interface 11 and the input end of the tube side of the palladium membrane purifier 14, the second heat exchange node E2 is located in front of the third heat exchange node E3.

[0035] The pipeline between the output end of the shell side of the reforming reactor 13 and the carbon dioxide capture interface 24 passes through the multi-stage heat exchanger 18 again after passing through the fourth heat exchange node E4, and the pipeline between the output end of the shell side of the reforming reactor 13 and the carbon dioxide capture interface 24, and the pipeline between the methanol water supply interface 11 and the input end of the tube side of the reforming reactor 13 exchange heat and form the first heat exchange node E1. In the flow direction of the fluid in the pipeline between the methanol water supply interface 11 and the input end of the tube side of the palladium membrane purifier 14, the first heat exchange node E1 is located in front of the second heat exchange node E2.

[0036] The pipeline between the first output end of the palladium membrane purifier 14 and the hydrogen gas outlet interface 21 passes through the multi-stage heat exchanger 18 again after passing through the second heat exchange node, and the pipeline between the first output end of the palladium membrane purifier 14 and the hydrogen gas outlet interface 21, and the pipeline between the compressed air inlet interface 19 and the input end of the catalytic reactor 15 exchange heat and form a fifth heat exchange interface. In the flow direction of the fluid in the pipeline between the compressed air inlet interface 19 and the input end of the catalytic reactor 15, the fifth heat exchange node E5 is located in front of the fourth heat exchange node E4.

[0037] An electric heater 17 is provided on the pipeline between the compressed air inlet interface 19 and the input end of the catalytic reactor 15 . The electric heater 17 is located on the pipeline between the multi-stage heat exchanger 18 and the input end of the catalytic reactor 15 .

[0038] like Figure 2 and Figure 3 As shown, the skid-mounted methanol high-temperature reforming hydrogen production device also includes a skid frame 26 , in which the reforming reactor 13 , the palladium membrane purifier 14 , the catalytic reactor 15 , the multi-stage heat exchanger 18 and the connecting pipelines are all installed.

[0039] In this embodiment, the methanol water supply interface 11 is pressurized by the booster pump 12 to supply methanol water into the tube side of the reforming reactor 13 and cracked to form hydrogen and gas byproducts, such as carbon monoxide. The gas output from the tube side of the reforming reactor 13 first passes through the precision filter 16 and enters the palladium membrane purifier 14. The hydrogen and gas byproducts enter the palladium membrane purifier 14 for filtration, and the hydrogen is transported to the hydrogen outlet interface 21 through the pipeline for discharge. If the hydrogen outlet interface 21 cannot receive more hydrogen, the excess hydrogen is discharged in the hydrogen venting pipeline 22.

[0040] The carbon monoxide filtered out by the palladium membrane purifier 14 enters the catalytic reactor 15, and the compressed air inlet interface 19 conveys an appropriate amount of compressed air into the catalytic reactor 15 through the control of the flow control valve 20, and the carbon monoxide and the compressed air form an oxidation reaction and release heat. The catalytic reactor 15 outputs high-temperature gas to enter the reforming reactor 13, which provides heat for the methanol water cracking in the shell of the reforming reactor 13. In addition, if the methanol water output is sufficient, the excess methanol water refluxes through the methanol water reflux interface 23. The carbon dioxide gas formed by the oxidation of carbon monoxide in the catalytic reactor 15 is discharged through the carbon dioxide capture interface 24 after heat exchange. When the carbon dioxide capture interface 24 cannot capture carbon dioxide, the carbon dioxide gas is emptied through the carbon dioxide venting pipeline 25.

[0041] The gas output from the shell side of the reforming reactor 13 still has a relatively high temperature, and the hydrogen output from the palladium membrane purifier 14 also has a relatively high heat. Therefore, the gas output from the shell side of the reforming reactor 13 and the hydrogen output from the palladium membrane purifier 14 are both subjected to heat exchange in the multi-stage heat exchanger 18 .

[0042] The methanol aqueous solution passes through the multi-stage heat exchanger 18, and sequentially passes through the first heat exchange node E1, the second heat exchange node E2, and the third heat exchange node E3, and is heated from 20°C to 410°C, absorbing 310KW of heat.

[0043] The catalytic oxidation exhaust gas after reforming and absorbing heat passes through the third heat exchange node E3, the fourth heat exchange node E4, and the first heat exchange node E1 in sequence, and is cooled from 415°C to 100°C, releasing 454.5KW of heat.

[0044] The purified hydrogen passes through the second heat exchange node E2 and the fifth heat exchange node E5 in sequence, and is cooled from 410°C to 35°C, releasing 189.7KW of heat.

[0045] The compressed combustion air passes through the fifth heat exchange node E5 and the fourth heat exchange node E4 in sequence, and is heated from 28°C to 200°C, absorbing 334KW of heat.

[0046] Table 1 below is a table of fluid temperature, fluid flow rate and heat exchange power at various nodes in the multi-stage heat exchanger 18 .

[0047] Table 1 shows the fluid temperature, fluid flow rate and heat transfer power of each node in the multi-stage heat exchanger

[0048]

[0049]

[0050] This system uses high-temperature reforming hydrogen production catalysts and adopts 350℃~450℃ high-temperature reforming hydrogen production. Compared with conventional low-temperature reforming hydrogen production, it is highly efficient and has fewer side reactions. The catalyst space velocity is several times higher, so the equipment volume advantage is obvious. The use of high-temperature reforming is conducive to the back-end combined palladium and palladium alloy membrane purification of hydrogen. The use of the same temperature reforming hydrogen production as palladium membrane purification ensures that hydrogen production and purification are carried out under the same conditions, that is, it ensures that a set of systems only needs one operating condition, which has absolute advantages over low-temperature catalysis in terms of intelligent automatic control of equipment or equipment space volume. Compared with the traditional PSA separation process, the palladium membrane purification process omits the cooling, washing and gas-liquid separator processes, has a simple process, small equipment volume, stable performance, and no waste gas and waste liquid emissions. The use of multi-channel heat exchangers solves the heat exchange between the fluids and reduces the energy loss of the system. The compact structure and high-efficiency heat exchange provide great help for the integration of the skid-mounted equipment.

[0051] The above contents are only preferred embodiments of the present invention. For ordinary technicians in this field, many changes can be made in the specific implementation methods and application scopes 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 skid-mounted methanol high-temperature reforming hydrogen production device, characterized in that: It comprises a reforming reactor, a palladium membrane purifier, a catalytic reactor and a multi-stage heat exchanger, wherein the input end of the tube side of the reforming reactor is connected to a methanol water supply interface through a pipeline, the output end of the tube side of the reforming reactor is connected to the input end of the palladium membrane purifier through a pipeline, the palladium membrane purifier has two output ends, the first output end of the palladium membrane purifier is a hydrogen output end, the first output end of the palladium membrane purifier is connected to a hydrogen outflow interface through a pipeline, the second output end of the palladium membrane purifier is a by-product gas output end, the second output end of the palladium membrane purifier is connected to the input end of the catalytic reactor through a pipeline, the input end of the catalytic reactor is also connected to a compressed air inlet interface through a pipeline, the output end of the catalytic reactor is connected to the input end of the shell side of the reforming reactor through a pipeline, and the output end of the shell side of the reforming reactor is connected to a carbon dioxide capture interface through a pipeline; The pipeline between the output end of the reforming reactor shell side and the carbon dioxide capture interface passes through a multi-stage heat exchanger, the pipeline between the methanol water supply interface and the input end of the reforming reactor tube side passes through a multi-stage heat exchanger, and the pipeline between the compressed air inlet interface and the input end of the catalytic reactor passes through a multi-stage heat exchanger; The pipeline between the output end of the reforming reactor shell side and the carbon dioxide capture interface, and the pipeline between the methanol water supply interface and the input end of the reforming reactor tube side exchange heat and form a third heat exchange node; The pipeline between the output end of the reforming reactor shell and the carbon dioxide capture interface, and the pipeline between the compressed air inlet interface and the input end of the catalytic reactor exchange heat and form a fourth heat exchange node.

2. The skid-mounted methanol high-temperature reforming hydrogen production device according to claim 1 is characterized in that: In the flow direction of the fluid in the pipeline between the output end of the reforming reactor shell side and the carbon dioxide capture interface, the third heat exchange node is located in front of the fourth heat exchange node.

3. The skid-mounted methanol high-temperature reforming hydrogen production device according to claim 1 is characterized in that: The pipeline between the first output end of the palladium membrane purifier and the hydrogen flow outlet interface passes through a multi-stage heat exchanger, and the pipeline between the first output end of the palladium membrane purifier and the hydrogen flow outlet interface, and the pipeline between the methanol water supply interface and the input end of the reforming reactor tube pass through heat exchange and form a second heat exchange node.

4. The skid-mounted methanol high-temperature reforming hydrogen production device according to claim 3 is characterized in that: In the flow direction of the fluid in the pipeline between the methanol water supply interface and the input end of the palladium membrane purifier tube, the second heat exchange node is located in front of the third heat exchange node.

5. The skid-mounted methanol high-temperature reforming hydrogen production device according to claim 3 is characterized in that: The pipeline between the output end of the reforming reactor shell side and the carbon dioxide capture interface passes through the multi-stage heat exchanger again after passing through the fourth heat exchange node; and The pipeline between the output end of the reforming reactor shell side and the carbon dioxide capture interface, and the pipeline between the methanol water supply interface and the input end of the reforming reactor tube side exchange heat and form a first heat exchange node.

6. The skid-mounted methanol high-temperature reforming hydrogen production device according to claim 5 is characterized in that: In the flow direction of the fluid in the pipeline between the methanol water supply interface and the input end of the palladium membrane purifier tube, the first heat exchange node is located in front of the second heat exchange node.

7. The skid-mounted methanol high-temperature reforming hydrogen production device according to claim 1 is characterized in that: The pipeline between the first output end of the palladium membrane purifier and the hydrogen flow outlet interface passes through the multi-stage heat exchanger again after passing through the second heat exchange node; and The pipeline between the first output end of the palladium membrane purifier and the hydrogen outflow interface, and the pipeline between the compressed air inlet interface and the input end of the catalytic reactor exchange heat and form a fifth heat exchange interface.

8. The skid-mounted methanol high-temperature reforming hydrogen production device according to claim 7 is characterized in that: In the flow direction of the fluid in the pipeline between the compressed air inlet interface and the input end of the catalytic reactor, the fifth heat exchange node is located in front of the fourth heat exchange node.

9. The skid-mounted methanol high-temperature reforming hydrogen production device according to claim 1, characterized in that: An electric heater is arranged on the pipeline between the compressed air inlet interface and the input end of the catalytic reactor, and the electric heater is located on the pipeline between the multi-stage heat exchanger and the input end of the catalytic reactor.

10. The skid-mounted methanol high-temperature reforming hydrogen production device according to any one of claims 1 to 9, characterized in that: The skid-mounted methanol high-temperature reforming hydrogen production device also includes a skid frame, and the reforming reactor, palladium membrane purifier, catalytic reactor, multi-stage heat exchanger and connecting pipelines are all installed in the skid frame.

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