Methanol hydrogen production system
By using the flue gas generated by the open flame burner as a heat source in the methanol hydrogen production system, it directly heats to the raw material vaporization and superheating unit and the main reaction unit, the problem of large device size and complex operation in conventional technology is solved, and a highly integrated Miniaturized design.
Patent Information
- Application Number
- CN202420773592.X
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-04-15
- Publication Date
- 2025-01-07
- Estimated Expiration
- 2034-04-15
AI Technical Summary
Conventional methanol hydrogen production technology requires heating of thermal oil systems or catalytic combustion systems, resulting in large size and complex operation, and the inability to achieve miniaturized design and integration.
The fuel is directly burned by an open flame burner. The generated flue gas passes through the raw material vaporization and superheating unit, the main reaction unit and the raw material preheating unit, as a heat source for the production of hydrogen by methanol, and the traditional thermal oil system or catalytic combustion system is abolished to achieve high integration. .
The equipment footprint is minimized, the design of a miniaturized methanol hydrogen production system is realized, and the operation process is simplified.
Smart Images
Figure CN222305731U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of methanol hydrogen production, in particular to a methanol hydrogen production conversion system. Background Art
[0002] The heat required for conventional methanol hydrogen production is generally supplied by a heat transfer oil system or heated by low-temperature flue gas from catalytic combustion. To heat the methanol hydrogen production catalyst at low temperature, an additional heat transfer oil system or catalytic combustion system (catalyst, circulating fan, etc.) must be added. As a result, the device is large in size, complex to operate, and cannot be miniaturized and integrated. Utility Model Content
[0003] In view of the above technical problems, the utility model provides a methanol hydrogen production system.
[0004] A methanol hydrogen production system includes an open flame burner, a raw material vaporization superheating unit, a main reaction unit and a raw material preheating unit. The open flame burner is provided with an oxygen source and a fuel inlet, and the flue gas flow generated by the open flame burner provides heat for the raw material preheating unit, the raw material vaporization superheating unit and the main reaction unit. The raw material vaporization superheating unit, the main reaction unit and the raw material preheating unit are arranged in sequence from the upstream to the downstream of the flue gas flow. The raw material preheating unit, the raw material vaporization superheating unit and the main reaction unit are connected by pipelines in sequence from the upstream to the downstream of the raw material flow. Optionally, the oxygen source and the fuel inlet are configured to include an independent oxygen source inlet and an independent fuel inlet. Optionally, the oxygen source and the fuel inlet are configured to also include an independent desorption gas inlet.
[0005] Furthermore, the methanol hydrogen production system disclosed in the utility model also includes a side reaction unit, a first heat exchange unit and a second heat exchange unit. The first heat exchange unit, the second heat exchange unit and the raw material preheating unit are connected by pipelines from upstream to downstream of the raw material flow. The main reaction unit, the second heat exchange unit, the side reaction unit and the first heat exchange unit are connected by pipelines from upstream to downstream of the product flow.
[0006] Furthermore, the methanol hydrogen production system disclosed in the utility model also includes a water-cooled purification separator and a pressure swing adsorption unit. The first heat exchange unit, the water-cooled purification separator and the pressure swing adsorption unit are connected in sequence by pipelines from the upstream to the downstream of the product flow.
[0007] Furthermore, the methanol hydrogen production system disclosed in the utility model also includes a blower, and the blower is connected to the oxygen source and the fuel inlet pipeline.
[0008] Furthermore, the methanol-to-hydrogen system disclosed in the utility model also includes a booster pump, and in the direction of the feedstock flow, the booster pump is arranged upstream of the first heat exchange unit.
[0009] The features and advantages of the present disclosure include: the methanol hydrogen production system of the present utility model directly burns fuel through an open flame burner, and the flue gas generated by the direct combustion of the fuel flows through the raw material vaporization superheating unit, the main reaction unit and the raw material preheating unit in sequence, and finally the flue gas is directly discharged into the atmosphere. The flue gas generated by the open flame combustion of the fuel is used as the heat source for methanol hydrogen production, eliminating the traditional bulky thermal oil system or catalytic combustion system, minimizing the footprint of the device, achieving high integration, and can be used in various small-scale methanol hydrogen production sites. BRIEF DESCRIPTION OF THE DRAWINGS
[0010] In order to more clearly illustrate the technical solutions in the embodiments of the present disclosure, the drawings required for use in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present disclosure. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.
[0011] Figure 1 It is a schematic diagram of a methanol hydrogen production system provided by the utility model.
[0012] Description of reference numerals:
[0013] 12-open flame burner, 14-raw material vaporization superheating unit, 16-main reaction unit, 18-raw material preheating unit, 120-oxygen source and fuel inlet, 122-fuel inlet, 124-oxygen source inlet, 126-desorption gas inlet; 28-first heat exchange unit, 26-side reaction unit, 24-second heat exchange unit; 32-water-cooled purification separator, 34-pressure swing adsorption unit, 36-blower, 38-boosting pump. DETAILED DESCRIPTION
[0014] The following will be combined with the drawings in the embodiments of the present disclosure to clearly and completely describe the technical solutions in the embodiments of the present disclosure. Obviously, the described embodiments are only part of the embodiments of the present disclosure, not all of the embodiments. Based on the embodiments in the present disclosure, all other embodiments obtained by ordinary technicians in this field without making creative work are within the scope of protection of the present disclosure.
[0015] refer to Figure 1The utility model discloses a methanol hydrogen production system, including an open flame burner 12, a raw material vaporization superheating unit 14, a main reaction unit 16 and a raw material preheating unit 18. Specifically, although not shown, the methanol hydrogen production system may include a reformer, and the open flame burner 12 may be arranged at the end of the reformer, for example, at the top or bottom of the reformer; the methanol hydrogen production system is provided with a flue, and the open flame burner directly burns the fuel in an oxygen environment to produce flue gas, and the flue is configured to provide a channel for the flow of flue gas. The open flame burner 12 is provided with an oxygen source and a fuel inlet 120, and the oxygen source and the fuel may be mixed first and then enter the oxygen source and the fuel inlet 120, or they may enter the oxygen source and the fuel inlet 120 separately. Optionally, the oxygen source and the fuel inlet 120 are configured to include an independent oxygen source inlet 124 and an independent fuel inlet 122. Optionally, the oxygen source and fuel inlet 120 is configured to further include an independent desorbed gas inlet 126. In some embodiments, the final stage of the process of the hydrogen production system uses pressure swing adsorption to purify the product. After pressure swing adsorption, the desorbed gas containing components such as CO2, H2 and CO can be used as fuel to enter the open flame burner 12 from the desorbed gas inlet 126. Alternatively, the desorbed gas can be mixed with the fuel and then enter the open flame burner 12 from the fuel inlet 122. The flue gas flow generated by the open flame burner 12 provides heat for the raw material preheating unit 18, the raw material vaporization superheating unit 14 and the main reaction unit 16.
[0016] Specifically, the raw material is a methanol-water solution, and the molar ratio of methanol to water is in the range of 0.8 to 1.5. The fuel can be used alone or in combination. For example, the fuels that can be used alone or in combination include but are not limited to methanol, methanol-water solution, pressure swing adsorption desorption gas, natural gas, methane, hydrocarbon mixtures, hydrogen and mixtures containing hydrogen and similar fuels; the oxygen source can be selected from oxygen, air, oxygen-enriched air, oxygen-depleted air, nitrogen-free air or a mixture thereof.
[0017] Specifically, from the upstream to the downstream direction of the flue gas flow, the methanol hydrogen production system is sequentially provided with a raw material vaporization superheating unit 14, a main reaction unit 16 and a raw material preheating unit 18. In some embodiments, the temperature of the flue gas flow at the most upstream (between the open flame burner 12 and the raw material vaporization superheating unit 14) is 1000-1500°C, the temperature of the flue gas flow between the raw material vaporization superheating unit 14 and the main reaction unit 16 is 700-1200°C, the temperature of the flue gas flow between the main reaction unit 16 and the raw material preheating unit 18 is 400-700°C, and the temperature of the most downstream flue gas flow leaving the raw material preheating unit 18 is 100-300°C.
[0018] Specifically, from the upstream to the downstream direction of the raw material flow, the raw material preheating unit 18, the raw material vaporization and superheating unit 14 and the main reaction unit 16 are connected in sequence by pipelines. Among them, the raw material flowing into the raw material preheating unit 18 is a raw material preheated by other heat exchange devices, and the raw material preheating unit 18 further heats the raw material and outputs it to the raw material vaporization and superheating unit 14. In some embodiments, the temperature of the raw material flowing into the raw material preheating unit 18 is 100~200℃, and the temperature of the raw material flowing out of the raw material preheating unit 18 is 200~300℃. The raw material vaporization and superheating unit 14 receives the raw material flowing out of the raw material preheating unit 18 and vaporizes the liquid methanol aqueous solution. The main reaction unit 16 receives the vaporized raw material flowing out of the raw material vaporization and superheating unit 14, and a methanol steam reforming reaction (methanol water cracking reaction) occurs to produce a conversion gas including components such as H2, CO and CO2. In some embodiments, H2 accounts for 50~80 vol%, CO accounts for 0~10 vol%, and CO2 accounts for 10~30 vol% in the conversion gas. The temperature of the reformed gas flowing out of the main reaction unit 16 is 250-450°C, and the reformed gas generated by the main reaction unit 16 is further heat exchanged and participates in side reactions. The feed inlet of the main reaction unit 16 is the downstream end of the feed flow, and the reformed gas outlet of the main reaction unit 16 is the upstream starting point of the product flow.
[0019] Continue to refer Figure 1 The methanol hydrogen production system disclosed in the utility model also includes a side reaction unit 26, a first heat exchange unit 28 and a second heat exchange unit 24. From the upstream to the downstream direction of the raw material flow, the first heat exchange unit 28, the second heat exchange unit 24 and the raw material preheating unit 18 are connected by pipelines in sequence; from the upstream to the downstream direction of the product flow, the main reaction unit 16, the second heat exchange unit 24, the side reaction unit 26 and the first heat exchange unit 28 are connected by pipelines in sequence.
[0020] Specifically, the temperature of the raw material flowing into the first heat exchange unit 28 is 0-100°C, the temperature of the raw material flowing into the second heat exchange unit 24 after being heated by the first heat exchange unit 28 is 50-150°C, and the temperature of the raw material flowing into the raw material preheating unit 18 after being heated by the second heat exchange unit 24 is 100-200°C. Correspondingly, the temperature of the reformed gas flowing out of the main reaction unit 16 is 250-450°C, the temperature of the reformed gas flowing into the secondary reaction unit 26 after being cooled by the second heat exchange unit 24 is 200-400°C, the temperature of the reaction gas with a higher hydrogen content flowing out of the secondary reaction unit 26 and entering the first heat exchange unit 28 is 200-400°C, and the temperature of the reaction gas flowing out of the first heat exchange unit 28 is 100-200°C. Among them, a hydrogen production reaction further occurs in the secondary reaction unit 26 to obtain a reaction gas with a higher hydrogen content; in some embodiments, H2 accounts for 65-85 vol% in the reaction gas.
[0021] Furthermore, the methanol hydrogen production system disclosed in the present invention further includes a water-cooled purification separator 32 and a pressure swing adsorption unit 34. From the upstream to the downstream direction of the product flow, the first heat exchange unit 28, the water-cooled separation purifier 32 and the pressure swing adsorption unit 34 are sequentially connected by pipelines.
[0022] The water-cooled purification separator 32 separates the reaction gas to obtain dry conversion gas and process condensate. The dry conversion gas is separated by the pressure swing adsorption unit 34 to obtain desorbed gas and product hydrogen. The desorbed gas can be introduced into the open flame burner 12 as fuel for combustion reaction.
[0023] Furthermore, the methanol hydrogen production system disclosed in the utility model also includes a blower 36 and a booster pump 38. The blower 36 is connected to the oxygen source and the fuel inlet 120 pipeline of the open flame burner 12, for example, it can be connected to the independent oxygen source inlet 124 pipeline. In the direction of the raw material flow, the booster pump 38 is arranged upstream of the first heat exchange unit 28. When the blower 36 is configured, the optional oxygen source is air, and the air is blown into the open flame burner 12 through the blower 36. The booster pump 38 is used to increase the pressure of the raw material (methanol aqueous solution) before the raw material enters the first heat exchange unit 28, so that the pressure of the hydrogen production reaction system is maintained at 1.0~2.5MPa.
[0024] The methanol hydrogen production system disclosed in the utility model is provided with an open flame burner, and flue gas is provided by directly burning fuel (methanol, methanol aqueous solution, pressure swing adsorption desorption gas or natural gas and other fuels), and the flue gas passes through the raw material vaporization superheating unit, the main reaction unit and the raw material preheating unit in sequence, and finally the flue gas is directly discharged into the atmosphere. The flue gas directly provides heat for the methanol steam reforming reaction, cancels the traditional heat transfer oil system or the bulky catalytic combustion system, minimizes the footprint of the device, achieves high integration, and can be used in various small-scale methanol hydrogen production sites.
[0025] The above are only several embodiments of the present disclosure. Those skilled in the art may make various changes or modifications to the embodiments of the present disclosure based on the contents disclosed in the application documents without departing from the spirit and scope of the present disclosure.
Claims
1. A methanol hydrogen production system, characterized in that: It comprises an open flame burner (12), a raw material vaporization superheating unit (14), a main reaction unit (16) and a raw material preheating unit (18); The open flame burner (12) is provided with an oxygen source and a fuel inlet (120), and the flue gas flow generated by the open flame burner (12) provides heat for the raw material preheating unit (18), the raw material vaporization superheating unit (14) and the main reaction unit (16); The raw material vaporization and superheating unit (14), the main reaction unit (16) and the raw material preheating unit (18) are arranged in sequence from the upstream to the downstream of the flue gas flow; The raw material preheating unit (18), the raw material vaporization superheating unit (14) and the main reaction unit (16) are connected in sequence by pipelines from the upstream to the downstream of the raw material flow.
2. The methanol to hydrogen system according to claim 1, characterized in that: It also includes a side reaction unit (26), a first heat exchange unit (28) and a second heat exchange unit (24); The first heat exchange unit (28), the second heat exchange unit (24) and the raw material preheating unit (18) are connected by pipelines in sequence from upstream to downstream of the raw material flow; The main reaction unit (16), the second heat exchange unit (24), the side reaction unit (26) and the first heat exchange unit (28) are connected in sequence by pipelines from upstream to downstream of the product flow.
3. The methanol to hydrogen system according to claim 2, characterized in that: Also included is a water-cooled purification separator (32) and a pressure swing adsorption unit (34); The first heat exchange unit (28), the water-cooled purification separator (32) and the pressure swing adsorption unit (34) are connected in sequence by pipelines from upstream to downstream of the product flow.
4. The methanol-to-hydrogen system according to claim 3, characterized in that: The invention also includes a blower (36), wherein the blower (36) is connected to the oxygen source and the fuel inlet (120) pipeline.
5. The methanol to hydrogen system according to any one of claims 2 to 4, characterized in that: It also includes a booster pump (38), which is arranged upstream of the first heat exchange unit (28) in the direction of raw material flow.
6. The methanol to hydrogen system according to claim 1, characterized in that: The oxygen source and fuel inlet (120) is configured to include an independent oxygen source inlet (124) and an independent fuel inlet (122).
7. The methanol-to-hydrogen system according to claim 6, characterized in that: The oxygen source and fuel inlet are configured to also include a separate stripping gas inlet (126).