Reactor and hydrogen production device

Abstract

The utility model belongs to the technical field of methanol hydrogen production, and particularly relates to a reactor and a hydrogen production device.The reactor comprises a shell, the shell defines a containing cavity, and the shell is further provided with a first inlet and a first outlet which communicate with the containing cavity; and the tubular heat exchange structure is connected with the shell and arranged in the containing cavity, the tubular heat exchange structure comprises a preheating section, a gasification section, an overheating section and a reforming section, and the preheating section, the gasification section, the overheating section and the reforming section are sequentially arranged in the direction from the first inlet to the first outlet. According to the hydrogen production device, the preheating section, the gasification section, the overheating section and the reforming section are arranged in the same shell, so that the integrated design of the reactor is realized, the structure of the reactor is simplified, the overall volume of the hydrogen production device is reduced, the hydrogen production device is convenient to transport, and meanwhile, the production cost is reduced. The preheating section, the gasification section, the overheating section and the reforming section all adopt tubular heat exchange structures, so that the conversion rate of raw materials can be increased, and the hydrogen production cost is reduced.

Description

Technical Field

[0001] The present invention belongs to the technical field of methanol hydrogen production, and particularly relates to a reactor and a hydrogen production device. Background Art

[0002] At present, the development of hydrogen energy and hydrogen fuel cell vehicles has become a hot topic of research. In view of the diverse market application scenarios, the demand for small hydrogen production and hydrogen refueling stations has gradually increased. Due to its special properties, the transportation and storage costs of hydrogen have remained high, which seriously restricts the popularization and application of hydrogen energy. Methanol hydrogen production is an important component technology for the current preparation and storage of hydrogen. Methanol hydrogen storage refers to the use of methanol as a hydrogen storage medium to transport methanol from the source to the hydrogen use site, and then release the hydrogen stored in the methanol through chemical conversion at the hydrogen use site. Carbon dioxide is also produced during the conversion process. Hydrogen and carbon dioxide are separated, hydrogen is used as fuel, and carbon dioxide is liquefied and collected and reused to produce methanol.

[0003] In existing hydrogen production devices, large-volume devices such as methanol solution storage tanks, vaporization towers, and water scrubbing towers are often included to prepare hydrogen, resulting in a large overall volume of the hydrogen production device, which makes it inconvenient to transport the hydrogen production device. Even if it can be transported, there is still a problem of high transportation costs. Utility Model Content

[0004] The purpose of the present application is to provide a reactor and a hydrogen production device, which can simplify the structure of the hydrogen production device and facilitate the transportation of the hydrogen production device.

[0005] The present disclosure provides a reactor, comprising:

[0006] A housing, wherein the housing is arranged to form a receiving cavity, and the housing is further provided with a first inlet and a first outlet communicating with the receiving cavity; and

[0007] A shell-and-tube heat exchange structure, the shell-and-tube heat exchange structure is connected to the shell and is arranged in the accommodating cavity, the shell-and-tube heat exchange structure includes a preheating section, a gasification section, a superheating section and a reforming section, and the preheating section, the gasification section, the superheating section and the reforming section are arranged in sequence from the first inlet to the first outlet.

[0008] In an exemplary embodiment of the present disclosure, the reactor further comprises an atomizing nozzle, wherein the atomizing nozzle is disposed in the preheating section, and the atomizing nozzle is used to provide a purified solution to the containing chamber of the preheating section.

[0009] In an exemplary embodiment of the present disclosure, the shell is provided with a first liquid drain port corresponding to the preheating section, the first liquid drain port is located at the bottom of the shell, and the first liquid drain port is used to discharge the liquid medium in the accommodating cavity corresponding to the preheating section.

[0010] In an exemplary embodiment of the present disclosure, the reactor includes a heat supply structure, which is connected to the shell, and the heat supply structure provides heat to at least a portion of the shell-and-tube heat exchange structure.

[0011] In an exemplary embodiment of the present disclosure, the shell is provided with a plurality of heat supply inlets and a plurality of heat supply outlets, one heat supply inlet is provided corresponding to one heat supply outlet, the heat supply inlet is provided at the bottom of the shell, the heat supply outlet is provided at the top of the shell, and the plurality of heat supply inlets are all connected to the heat supply structure, and the heat supply structure is used to provide a heat supply medium;

[0012] The gasification section, the superheating section and the reforming section are respectively provided with at least one heat supply inlet.

[0013] In an exemplary embodiment of the present disclosure, the accommodating chamber also includes a gas-liquid separation chamber, which is arranged between the gasification section and the superheating section. The gas-liquid separation chamber is used to separate the gas-liquid mixed medium, the gas phase medium moves toward the superheating section, and the liquid phase medium falls into the bottom of the gas-liquid separation chamber.

[0014] In an exemplary embodiment of the present disclosure, the shell corresponding to the gas-liquid separation chamber is provided with a second liquid drain port, the second liquid drain port is located at the bottom of the shell, and the second liquid drain port is used to discharge the liquid medium in the gas-liquid separation chamber.

[0015] In an exemplary embodiment of the present disclosure, the reforming section is filled with a catalyst, and a feedstock enters the reforming section and undergoes a reforming reaction based on the catalyst.

[0016] In an exemplary embodiment of the present disclosure, the shell is provided with a second inlet and a second outlet corresponding to the preheating section, the second inlet is located at the top of the shell, the second outlet is located at the bottom of the shell, the first outlet is connected to the second inlet, the gas phase medium is discharged from the first outlet, enters the accommodating chamber through the second inlet, and leaves the accommodating chamber through the second outlet to provide preheating heat.

[0017] In an exemplary embodiment of the present disclosure, the accommodating chamber includes a preheating chamber, a gasification chamber, an overheating chamber and a reforming chamber, the preheating section is arranged in the preheating chamber, the gasification section is arranged in the gasification chamber, the overheating section is arranged in the overheating chamber, and the reforming section is arranged in the reforming chamber;

[0018] The reactor includes a plurality of connectors, which are arranged between the preheating chamber, the gasification chamber, the superheating chamber and the reforming chamber, and two adjacent connectors are butted together to connect the preheating section, the gasification section, the superheating section and the reforming section in sequence.

[0019] The present disclosure provides a hydrogen production device, comprising a raw material configuration device, a cold dryer and any of the reactors described above, wherein the raw material configuration device is connected to the first inlet, and the cold dryer is connected to the shell to collect the gas phase medium after the reaction of the reactor.

[0020] This application scheme has the following beneficial effects:

[0021] The present disclosure realizes an integrated design of the reactor by arranging the preheating section, gasification section, superheating section and reforming section in the same shell, thereby simplifying the structure of the reactor and reducing the overall volume of the hydrogen production device, so that the hydrogen production device can be easily transported.

[0022] Other features and advantages of the present application will become apparent from the following detailed description, or may be learned in part by the practice of the present application.

[0023] It should be understood that the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the present application. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] The accompanying drawings herein are incorporated into and constitute a part of the specification, illustrate embodiments consistent with the present disclosure, and are used together with the specification to explain the principles of the present disclosure. Obviously, the accompanying drawings described below are only some embodiments of the present disclosure, and for ordinary technicians in this field, other accompanying drawings can be obtained based on these accompanying drawings without creative work.

[0025] Figure 1 It is a structural schematic diagram of a hydrogen production device in the prior art.

[0026] Figure 2 Schematic diagram of the structure of the reactor in the embodiment of the present disclosure.

[0027] Figure 3 Schematic diagram of the structure of the hydrogen production device in the embodiment of the present disclosure.

[0028] Description of reference numerals:

[0029] 100. Hydrogen production device;

[0030] 110. Reactor;

[0031] 111. Shell;

[0032] 1111, accommodating chamber; 1111a, gas-liquid separation chamber; 1112, first liquid discharge port; 1113, first inlet; 1114, first outlet; 1115, second inlet; 1116, second outlet; 1117, second liquid discharge port;

[0033] 112. Shell and tube heat exchange structure; 1121. Preheating section; 1122. Gasification section; 1123. Superheating section; 1124. Reforming section;

[0034] 113. Heating structure; 1131. Heating inlet; 1132. Heating outlet;

[0035] 114. Atomizing nozzle;

[0036] 115. Recovery pump;

[0037] 116. Connectors;

[0038] 120. Raw material preparation device; 121. Methanol raw material pump; 122. Deionized water pump; 123. Static mixer; 124. Raw material preparation tank; 125. Transport pump;

[0039] 130. Cold dryer;

[0040] X, horizontal direction. DETAILED DESCRIPTION

[0041] Example embodiments will now be described more fully with reference to the accompanying drawings. However, example embodiments can be implemented in a variety of forms and should not be construed as limited to the examples set forth herein; rather, these embodiments are provided so that this disclosure will be more comprehensive and complete and will fully convey the concept of the example embodiments to those skilled in the art.

[0042] In addition, the described features, structures or characteristics may be combined in one or more embodiments in any suitable manner. In the following description, many specific details are provided to provide a full understanding of the embodiments of the present disclosure. However, those skilled in the art will appreciate that the technical solutions of the present disclosure may be practiced without one or more of the specific details, or other methods, components, devices, steps, etc. may be adopted. In other cases, known methods, devices, implementations or operations are not shown or described in detail to avoid blurring the various aspects of the present disclosure.

[0043] The present disclosure is further described in detail below in conjunction with the accompanying drawings and specific embodiments. It should be noted that the technical features involved in the various embodiments of the present disclosure described below can be combined with each other as long as they do not conflict with each other. The embodiments described below with reference to the accompanying drawings are exemplary and are intended to be used to explain the present disclosure, and should not be understood as limiting the present disclosure.

[0044] like Figure 1As shown, the relevant hydrogen production device 100 generally includes a raw material storage tank, a preheater, a vaporizer, a superheater, a reformer, a cold dryer 130, a water scrubber, a heating structure 113 and other equipment, wherein the preheater, the vaporizer, the superheater and the reformer are independent reaction equipment, and the preheater, the vaporizer, the superheater and the reformer are connected by pipelines to realize the circulation of raw materials among the preheater, the vaporizer, the superheater and the reformer. However, such hydrogen production equipment has problems such as complex pipeline layout, large floor space and difficult transportation. The heating structure 113 provides heat for the preheater, the vaporizer, the superheater and the reformer during the preheating, gasification, heating and reforming processes. When the raw materials are in the preheating When the raw materials flow between the preheater, vaporizer, superheater and reformer, they need to pass through multiple pipelines. Therefore, there may be a large amount of heat loss when the raw materials flow between the preheater, vaporizer, superheater and reformer, thereby increasing the cost of hydrogen production. After the reforming reaction, there is still a large amount of raw materials that cannot be converted into product gas, and then the dryer 130 is required to cool the product gas, separate the condensed water, and use the water scrubber to further remove most of the impurity gases such as water and methanol in the product gas to obtain the product gas. The water scrubber is a large-volume equipment. When the water scrubber is used in the hydrogen production equipment, it will increase the floor space of the hydrogen production equipment, and also increase the transportation difficulty and transportation cost of the hydrogen production equipment.

[0045] In order to solve the above problems, the present disclosure provides a reactor 110 and a hydrogen production device 100 to reduce the volume of the reactor 110 and the hydrogen production device 100, so as to prepare for the skid-mounted hydrogen production device 100. It should be noted that skid-mounted means a form of overall combination of the hydrogen production device 100 and an equipment frame. By skid-mounting the hydrogen production device 100, the transportation of the hydrogen production device 100 can be facilitated.

[0046] In addition, the reactor 110 and the hydrogen production device 100 in the present disclosure may be a methanol solution, and the methanol solution undergoes a reforming reaction in the hydrogen production device 100 to obtain a product gas, namely, hydrogen and a small amount of methane and carbon monoxide.

[0047] Combine the following Figure 2 and Figure 3 The reactor 110 and the hydrogen production device 100 in the embodiment of the present disclosure are described in detail.

[0048] The embodiment of the present disclosure provides a reactor 110 , which includes a shell 111 and a shell-and-tube heat exchange structure 112 .

[0049] Among them, the shell 111 is arranged to form a accommodating chamber 1111, and a first inlet 1113 and a first outlet 1114 are respectively provided at the opposite ends of the shell 111. The first inlet 1113 and the first outlet 1114 can connect the accommodating chamber 1111, so that the raw material can enter the accommodating chamber 1111 through the first inlet 1113 and leave the accommodating chamber 1111 through the first outlet 1114.

[0050] It should be understood that the reactor 110 in the embodiment of the present disclosure needs to undergo a series of high-temperature reactions. Therefore, the material used to make the shell 111 should have a high melting point. At the same time, in order to avoid collisions between the reactor 110 and other equipment due to bumps during transportation, thereby causing damage to the reactor 110, the shell 111 in the embodiment of the present disclosure should also have the characteristic of high hardness.

[0051] In the disclosed embodiment, a shell-and-tube heat exchange structure 112 is provided in the accommodating cavity 1111. The shell-and-tube heat exchange structure 112 is connected to the shell 111 by a fixed tube sheet to achieve relative stability with the shell 111, thereby avoiding collision between the shell-and-tube heat exchanger and the shell 111 during transportation, which may cause damage to the shell 111 and the shell-and-tube heat exchanger, thereby extending the service life of the reactor 110, while also ensuring the safety and reliability of transportation.

[0052] Furthermore, the accommodating chamber 1111 includes a preheating chamber, a gasification chamber, an overheating chamber and a reforming chamber, and the preheating chamber, the gasification chamber, the overheating chamber and the reforming chamber are separated by fixed tube sheets, and the shell-and-tube heat exchange structure 112 includes a preheating section 1121, a gasification section 1122, a overheating section 1123 and a reforming section 1124, wherein the preheating section 1121 is arranged in the preheating chamber, the gasification section 1122 is arranged in the gasification chamber, the overheating section 1123 is arranged in the overheating chamber, and the reforming section 1124 is arranged in the reforming chamber, and the preheating section 1121, the gasification section 1122, the overheating section 1123 and the reforming section 1124 are arranged in sequence from the first inlet 1113 to the first outlet 1114.

[0053] It should be noted that the shell 111 in the embodiment of the present disclosure is placed horizontally as a whole, that is, when the reactor 110 is in the reaction process, the preheating section 1121, the gasification section 1122, the superheating section 1123 and the reforming section 1124 are arranged in sequence in the horizontal direction X, the first inlet 1113 and the first outlet 1114 are located on opposite sides of the horizontal direction X, and the preheating section 1121 is located on the side of the accommodating chamber 1111 close to the first inlet 1113, and the reforming section 1124 is located on the side of the accommodating chamber 1111 close to the first outlet 1114.

[0054] In the disclosed embodiment, the raw material enters the preheating section 1121 through the first inlet 1113. After passing through the preheating section 1121, the raw material obtains heat from the preheating chamber and achieves initial temperature rise. It should be noted that the temperature range of the raw material in the preheating section 1121 is 140°C-150°C.

[0055] Furthermore, the raw material enters the gasification section 1122 from the preheating section 1121 and is heated in the gasification section 1122 until the raw material is converted from a liquid medium to a gas medium. It should be noted that the temperature of the raw material in the gasification section 1122 reaches 200°C.

[0056] Furthermore, the raw material enters the superheating section 1123 from the gasification section 1122 and is heated in the superheating section 1123 until the raw material is heated to the temperature required for the reforming reaction. It should be noted that the temperature range of the raw material in the superheating section 1123 is 250°C-280°C. Then, the raw material undergoes a high-temperature reforming reaction in the reforming section 1124 to obtain a product gas.

[0057] In the disclosed embodiment, the reactor 110 further includes a heating structure 113, which is located outside the accommodating chamber 1111 and connected to the shell 111. The heating structure 113 contains a heating medium, which enters the accommodating chamber 1111 from the heating structure 113, thereby providing heat for the shell-and-tube heat exchange structure 112.

[0058] It should be noted that the heating structure 113 provides heat to at least part of the shell-and-tube heat exchange structure 112. For example, the heating structure 113 can provide heat to the gasification section 1122, the superheating section 1123 and the reforming section 1124, thereby preheating and gasifying the raw materials until the temperature required for the reforming reaction is reached, so as to improve the conversion rate of the raw materials after the reforming reaction.

[0059] Furthermore, the shell 111 is provided with multiple heat inlets 1131 and multiple heat outlets 1132. One heat inlet 1131 corresponds to one heat outlet 1132. The heat inlet 1131 is arranged at the bottom of the shell 111, and the heat outlet 1132 is arranged at the top of the shell 111. The multiple heat inlets 1131 are all connected to the heating structure 113, so that the heating medium can enter the accommodating cavity 1111 through the heat inlet 1131 and provide heat for the shell-and-tube heat exchange structure 112.

[0060] It should be noted that, since the reactor 110 in the present disclosure conducts heat through the heat supply medium in the heat supply structure 113 , the material of the shell-and-tube heat exchange structure 112 in the embodiment of the present disclosure should have good thermal conductivity.

[0061] At least one heat supply inlet 1131 is respectively provided in correspondence with the gasification section 1122, the superheating section 1123 and the reforming section 1124. For example, in the embodiment of the present disclosure, a heat supply inlet 1131 and a heat supply outlet 1132 are respectively provided in the gasification section 1122, the superheating section 1123 and the reforming section 1124. Specifically, the heat supply inlet 1131 corresponding to the gasification chamber is located at the bottom of the shell 111 corresponding to the gasification chamber, and the heat supply medium enters the gasification chamber and provides heat for the gasification section 1122 until the raw materials in the gasification section 1122 are heated and gasified, and the heat supply medium flows countercurrently from the bottom of the accommodating chamber 1111 to the top of the accommodating chamber 1111, and flows out from the heat supply outlet 1132 provided at the top of the shell 111 corresponding to the gasification chamber; the heat supply inlet 1131 corresponding to the superheating chamber is located at the bottom of the shell 111 corresponding to the superheating chamber, and the heat supply medium enters the superheating chamber and provides heat for the superheating chamber. Section 1123 provides heat until the raw materials in the superheating section 1123 are heated to the temperature required for the reforming reaction, and the heat supply medium flows countercurrently from the bottom of the accommodating chamber 1111 to the top of the accommodating chamber 1111, and flows out from the heat supply outlet 1132 arranged at the top of the shell 111 corresponding to the superheating chamber; the heat supply inlet 1131 corresponding to the reforming chamber is located at the bottom of the shell 111 corresponding to the reforming chamber, and the heat supply medium enters the reforming chamber and provides heat for the reforming section 1124, so that the temperature required for the reforming reaction is always maintained in the reforming section 1124 to ensure the conversion rate of the reforming reaction, and the heat supply medium flows countercurrently from the bottom of the accommodating chamber 1111 to the top of the accommodating chamber 1111, and flows out from the heat supply outlet 1132 arranged at the top of the shell 111 corresponding to the reforming chamber.

[0062] It should be noted that the heating medium in the embodiment of the present disclosure can be heat transfer oil, which flows evenly in the accommodating chamber 1111 and provides heat to the reactor 110 to achieve smooth control of the reforming reaction temperature, but is not limited to this. Other heating media that can provide heat to the shell-and-tube heat exchange structure 112 are included in the scope of the embodiment of the present disclosure.

[0063] It should be understood that during the reaction process of the reactor 110, low-temperature gas tends to gather at the bottom of the shell-and-tube heat exchange structure 112, and high-temperature gas tends to gather at the top of the shell-and-tube heat exchange structure 112. Therefore, in the embodiment of the present disclosure, the heat supply inlet 1131 is set at the bottom of the shell 111, so that the heat supply medium can first heat the low-temperature gas-phase medium gathered at the bottom of the shell-and-tube heat exchange structure 112, and then the heat supply medium countercurrently flows upward to heat the high-temperature gas-phase medium gathered at the top of the shell-and-tube heat exchange structure 112, so that the gas-phase medium in the shell-and-tube heat exchange structure 112 can reach the temperature required for the reforming reaction, and can improve the conversion rate of the reforming reaction, thereby saving the manufacturing cost of the product gas.

[0064] In addition, the present application realizes an integrated design of the reactor 110 by arranging the preheating section 1121, the gasification section 1122, the superheating section 1123 and the reforming section 1124 in the same shell 111, so that when the heating structure 113 provides heat for the reactor 110, the loss during heat import and export can be reduced, thereby improving the thermal utilization rate of the reactor 110.

[0065] In the disclosed embodiment, the reforming section 1124 is filled with a catalyst. Specifically, the catalyst is filled in each tube array so that the raw material can fully contact with the catalyst after entering the reforming section 1124 and complete the reforming reaction, thereby improving the conversion rate of the raw material and reducing the manufacturing cost of the product gas.

[0066] Furthermore, the space velocity range of the tubes in the reforming section 1124 is 300h-1-600h-1, specifically 300h-1, 350h-1, 400h-1, 450h-1, 500h-1, 550h-1, 600h-1, etc., so that the raw material can fully react with the catalyst in the tubes to improve the conversion rate of the raw material.

[0067] In the embodiment of the present disclosure, the shell 111 is provided with a second inlet 1115 and a second outlet 1116 corresponding to the preheating section 1121. The second inlet 1115 is located at the top of the shell 111, and the second outlet 1116 is located at the bottom of the shell 111. The first outlet 1114 is connected to the second inlet 1115. The product gas obtained after the reforming reaction is discharged from the first outlet 1114 and enters the accommodating chamber 1111 through the second inlet 1115 to provide preheating heat for the raw material in the preheating section 1121. After the product gas exchanges heat with the raw material, it leaves the accommodating chamber 1111 through the second outlet 1116.

[0068] It should be noted that the product gas obtained after the reforming reaction is still in a high-temperature state. In order to make full use of the heat of the product gas, the embodiment of the present disclosure connects the first outlet 1114 with the second inlet 1115. The high-temperature product gas is discharged from the first outlet 1114, enters the preheating chamber through the second inlet 1115, and provides preheating heat for the low-temperature raw material in the preheating chamber section, so that the raw material in the preheating section 1121 is initially heated up. By passing the high-temperature product gas obtained by the reforming reaction into the preheating chamber, the heat of the high-temperature product gas is fully utilized, thereby reducing the energy consumption of the reactor 110 and reducing the production cost of obtaining the product gas.

[0069] In addition, the second inlet 1115 in the present application is arranged at the top of the shell 111, and the second outlet 1116 is arranged at the bottom of the shell 111, so that when the product gas flows from the top of the preheating chamber to the bottom of the preheating chamber, the product gas can be fully in contact with the low-temperature raw material and transfer heat with the low-temperature raw material, so that part of the water in the product gas can be condensed out, thereby achieving purification of the product gas.

[0070] It should be noted that the raw material in the embodiment of the present disclosure is a methanol solution. The product gas obtained after the reforming reaction contains, in addition to hydrogen, impurity gases such as methane, carbon monoxide, water, and methanol. When the high-temperature product gas after the reaction is passed into the preheating chamber, the product gas transfers heat to the methanol solution in the preheating section 1121, and the product gas is cooled. After the temperature is lowered, part of the water condenses out of the product gas, and methanol is highly soluble in water. Therefore, the condensed water can be used to absorb part of the methanol in the product gas, thereby purifying the product gas.

[0071] Furthermore, in the embodiment of the present disclosure, the reactor 110 also includes an atomizing nozzle 114 , which is disposed in the preheating chamber to provide a purified solution to the containing chamber 1111 of the preheating section 1121 .

[0072] It should be noted that the atomizing nozzle 114 is located on one side of the accommodating chamber 1111 close to the bottom of the shell 111. Specifically, the atomizing nozzle 114 can be connected to the bottom of the preheating section 1121, or can be connected to the bottom of the shell 111 corresponding to the preheating chamber. The atomizing nozzle 114 can provide a mist-like purification solution for the preheating chamber. In the embodiment of the present disclosure, the purification solution can be a methanol aqueous solution. When the product gas flows from the top of the preheating chamber to the bottom of the preheating chamber, the methanol aqueous solution sprayed from the atomizing nozzle 114 contacts the product gas and absorbs the residual methanol in the product gas, thereby purifying the product gas. At the same time, the atomizing nozzle 114 is used in the present disclosure to make the methanol aqueous solution atomized, so that the methanol aqueous solution can be fully contacted with the product gas, and then the residual methanol in the product gas can be fully absorbed to improve the purity of the product gas.

[0073] Whether it is the aqueous solution condensed from the product gas after the temperature is lowered, or the purified solution sprayed from the atomizing nozzle 114, it is easy to form accumulation in the preheating chamber. To avoid this situation, the embodiment of the present disclosure is provided with a first liquid discharge port 1112 in the shell 111 corresponding to the preheating section 1121. The first liquid discharge port 1112 is located at the bottom of the shell 111 and is used to discharge the liquid medium in the preheating chamber, thereby avoiding the accumulation of the liquid medium in the preheating chamber and affecting the raw material concentration in the reactor 110, thereby improving the conversion rate of the raw material.

[0074] In addition, the bottom of the shell 111 corresponding to the preheating chamber may also have a small slope design, so that the liquid medium in the preheating chamber is gathered at the first liquid discharge port 1112, so that the liquid medium in the preheating chamber can be easily discharged from the accommodating chamber 1111.

[0075] In the embodiment of the present disclosure, the accommodating chamber 1111 also includes a gas-liquid separation chamber 1111a, which is arranged between the gasification section 1122 and the superheating section 1123. The gas-liquid separation chamber 1111a is used to separate the gas-liquid mixed medium, and the gas phase medium moves toward the superheating section 1123, and the liquid phase medium falls to the bottom of the gas-liquid separation chamber 1111a.

[0076] It should be noted that after the temperature of the gasification section 1122 is increased, most of the raw materials have been converted into gaseous medium, but at the same time there is also a small part of the raw materials that have not reached the gasification temperature, and thus have not been converted from liquid medium to gaseous medium. In order to prevent the low-temperature liquid medium from entering the superheating section 1123 and affecting the temperature of the superheating section 1123, the embodiment of the present disclosure sets a gas-liquid separation chamber 1111a between the gasification section 1122 and the superheating section 1123. After the raw materials of the gasification section 1122 enter the gas-liquid separation chamber 1111a, gas-liquid separation of the gas-liquid mixed medium can be achieved in the gas-liquid separation chamber 1111a. The low-temperature liquid medium falls to the bottom of the gas-liquid separation chamber 1111a due to its own gravity, and the high-temperature gas medium enters the superheating section 1123, thereby reducing the low-temperature liquid medium. The possibility of the medium entering the superheating section 1123 and affecting the temperature of the raw materials in the superheating section 1123 is reduced, thereby reducing the heat loss in the reaction process of the reactor 110 and reducing the production cost of manufacturing the product gas. At the same time, the design of the gas-liquid separation chamber 1111a can reduce the possibility of the liquid medium entering the superheating section 1123 and the reforming section 1124, so as to protect the high-temperature equipment corresponding to the superheating section 1123 and the reforming section 1124 from exploding when in contact with low-temperature liquid media such as water, thereby improving the safety and reliability of the reforming reaction process. In addition, the catalyst in the reforming section 1124 is easily powdered and deactivated when it comes into contact with water. By setting the gas-liquid separation chamber 1111a, the water in the raw materials can be removed to ensure that the catalyst can maintain its activity and improve the conversion rate of the reforming reaction.

[0077] Furthermore, a second drain port 1117 is provided in the shell 111 corresponding to the gas-liquid separation chamber 1111a, and the second drain port 1117 is located at the bottom of the shell 111. When the gas-liquid mixed medium in the gas-liquid separation chamber 1111a is separated, the gas phase medium enters the superheating section 1123, and the liquid phase medium automatically falls to the bottom of the gas-liquid separation chamber 1111a and is discharged from the gas-liquid separation chamber 1111a through the second drain port 1117, thereby avoiding a large amount of accumulation of the liquid phase medium in the gas-liquid separation chamber 1111a, and even causing part of the liquid phase medium to enter the superheating section 1123, thereby reducing the risk of explosion between the liquid phase medium and the equipment after entering the superheating section 1123 and the reforming section 1124, thereby improving the safety and reliability of the reforming reaction process, and at the same time, avoiding the possibility of deactivation of the catalyst in the reforming section 1124 due to water, thereby ensuring a high conversion rate of the raw materials.

[0078] The reactor 110 in the embodiment of the present disclosure may further include a recovery pump 115, one end of the recovery pump 115 is connected to the first liquid discharge port 1112, and the other end is connected to the first inlet 1113. It should be noted that the liquid medium discharged from the first liquid discharge port 1112 may contain water and methanol. By setting up the recovery pump 115, the water and methanol discharged from the first liquid discharge port 1112 are stored in the recovery pump 115, and the water and methanol are re-entered into the shell-and-tube heat exchanger as raw materials for reforming reaction through the recovery pump 115, thereby realizing the recycling of raw materials, improving the utilization rate of raw materials, and reducing the production cost of product gas.

[0079] In addition, the recovery pump 115 can also be connected to the second liquid discharge port 1117. It should be noted that the liquid medium discharged from the second liquid discharge port 1117 may also contain water and methanol. The liquid medium discharged from the second liquid discharge port 1117 enters the recovery pump 115 through a pipeline, and enters the shell-and-tube heat exchanger again through the recovery pump 115 for reforming reaction, thereby realizing the recycling of raw materials, improving the utilization rate of raw materials, and reducing the production cost of product gas.

[0080] In the disclosed embodiment, the reactor 110 further includes a plurality of connectors 116, which are disposed between the preheating chamber, the gasification chamber, the superheating chamber and the reforming chamber, and are used to realize the division of the accommodating chamber 1111. Two adjacent connectors 116 are docked so that the preheating section 1121, the gasification section 1122, the superheating section 1123 and the reforming section 1124 are assembled and connected in sequence.

[0081] For example, the connecting piece 116 in the embodiment of the present disclosure may be a flange, and a pair of flanges are arranged between the preheating section 1121 and the gasification section 1122 to realize the connection between the preheating section 1121 and the gasification section 1122; a pair of flanges are arranged between the gasification section 1122 and the superheating section 1123 to realize the connection between the gasification section 1122 and the superheating section 1123; a pair of flanges are arranged between the superheating section 1123 and the reforming section 1124 to realize the connection between the superheating section 1123 and the reforming section 1124.

[0082] It should be noted that the gas-liquid separation chamber 1111a is located in the gasification chamber, and the gas-liquid separation chamber 1111a is connected to the gasification section 1122 and the superheating section 1123 on opposite sides in the horizontal direction X. Therefore, the connecting piece 116 between the gasification section 1122 and the superheating section 1123 is specifically located between the gas-liquid separation chamber 1111a and the superheating section 1123, so that the liquid phase medium and the gas phase medium in the gasification section 1122 can be separated, ensuring that the raw material entering the superheating section 1123 is in a gaseous state, thereby avoiding the possibility of explosion of the low-temperature liquid phase medium after entering the superheating section 1123 and the high-temperature equipment in the superheating section 1123 and the reforming section 1124, thereby improving the safety and reliability of the reforming reaction process. At the same time, it also avoids the possibility of deactivation of the catalyst in the reforming section 1124 due to water, thereby improving the conversion rate of the raw material.

[0083] In addition, the first outlet 1114 is connected to the second inlet 1115, and the high-temperature product gas obtained by the reforming reaction passes through the first outlet 1114 and the second inlet 1115 in sequence and enters the preheating chamber. The high-temperature product gas can be used to provide thermal energy to the raw materials in the preheating section 1121. The first outlet 1114 and the second inlet 1115 can be connected by a conduit. Furthermore, in the embodiment of the present disclosure, a flange can be set between the first outlet 1114 and the conduit for connecting the conduit to the first outlet 1114.

[0084] However, the connecting member 116 in the embodiment of the present disclosure is not limited to a flange, and other connecting members 116 that can realize the connection between the preheating section 1121, the gasification section 1122, the superheating section 1123 and the reforming section 1124 are all included in the scope of the embodiment of the present disclosure.

[0085] The embodiment of the present disclosure provides a hydrogen production device 100, including a raw material configuration device 120, a cold dryer 130 and any one of the above-mentioned reactors 110, the raw material configuration device 120 is connected to the first inlet 1113 to provide the reactor 110 with raw materials for the reforming reaction, and the cold dryer 130 is connected to the second outlet 1116 to remove impurities in the collected product gas and obtain high-purity hydrogen.

[0086] It should be noted that the raw material preparation device in the embodiment of the present disclosure may include a methanol raw material pump 121 and a deionized water pump 122. The methanol raw material pump 121 and the deionized water pump 122 can store the raw material solution. At the same time, the methanol raw material pump 121 and the deionized water pump 122 can also increase the pressure of the raw material solution, so that the raw materials required for the reforming reaction can be transported to the reactor 110. In addition, compared with the raw material storage tank, the methanol raw material pump 121 and the deionized water pump 122 are smaller in size, thereby reducing the footprint of the hydrogen production device 100, making the hydrogen production device 100 easy to transport, thereby reducing the cost of the hydrogen source.

[0087] The reactor 110 in the present disclosure adopts a shell-and-tube heat exchange structure 112 as a whole. Compared with a separate preheater, vaporizer, superheater and reformer, the conversion rate of the methanol feedstock in the reactor 110 in the embodiment of the present disclosure is higher, and the methanol content in the obtained product gas is less. Therefore, the present application can omit the water washing tower for recovering methanol in the existing hydrogen production device 100, and by providing a cold dryer 130 connected to the second outlet 1116 to remove condensed water and methanol in the product gas, the footprint of the hydrogen production device 100 can be reduced, providing a guarantee for the skid-mounted hydrogen production device 100. At the same time, the structure of the hydrogen production device 100 can be simplified, and the hydrogen production process can be simplified, thereby ensuring the economy of the process.

[0088] The raw materials in the embodiment of the present disclosure can be configured continuously and automatically. Specifically, the methanol raw material pump 121 and the deionized water pump 122 in the embodiment of the present disclosure can both adopt precision variable frequency gear pumps, thereby realizing accurate metering of the raw material solution entering the reactor 110. When the hydrogen production device 100 is used in a hydrogen refueling station, the motor in the hydrogen production device 100 is pressure-interlocked with the hydrogen storage tank of the hydrogen refueling station, thereby being able to adapt to changes in operating conditions and accurately control the raw material solution delivered to the reactor 110.

[0089] The raw material preparation device may also be provided with a static mixer 123, and the static mixer 123 is connected to the methanol raw material pump 121 and the deionized water pump 122 to achieve sufficient mixing of methanol and water.

[0090] Furthermore, the embodiment of the present disclosure can compile a computer program for a continuous automatic configuration process, utilize the data fed back by the online methanol concentration meter in the static mixer 123, and timely adjust and control the rotation speeds of the methanol raw material pump 121 and the deionized water pump 122, thereby achieving automatic control of the methanol solution concentration and the methanol solution configuration rate.

[0091] In the embodiment of the present disclosure, the raw material preparation device may further include a raw material preparation tank 124, and the raw material preparation tank 124 is connected to the static mixer 123 for storing the prepared raw material solution.

[0092] In order to transport the raw material solution to the reactor 110 , the raw material preparation device in the present disclosure may further include a transport pump 125 , so as to increase the pressure of the raw material solution and continuously provide the reactor 110 with the raw materials required for the reforming reaction.

[0093] The hydrogen production device 100 may include a thermal conductivity online hydrogen detector. Specifically, the thermal conductivity online hydrogen detector may be arranged at the second outlet 1116 or in the cold dryer 130 to detect the hydrogen content in the product gas of the hydrogen production device 100 in real time and monitor the process operation status at any time.

[0094] The hydrogen production device 100 in the embodiment of the present disclosure may also include an integrated control room, a collection device and an integrated instrument. The integrated control room may include a control cabinet and a host computer to realize real-time monitoring of the operating status of the hydrogen production device 100. When an abnormality occurs in the hydrogen production device 100, the problem can be discovered and solved in time; the collection device can collect various sensor data in the hydrogen production device 100 and generate a data curve to help users quickly analyze the operating trend of the hydrogen production device 100 and make early warnings; the integrated instrument may include a pressure gauge and a pressure transmitter. The gauge and pressure transmitter are integrated on the skid-mounted instrument rack of the hydrogen production device 100, which can facilitate the viewing, maintenance and repair of pressure data. The present disclosure can collect the pressure data in the preheating section 1121, the gasification section 1122, the superheating section 1123 and the reforming section 1124 of the reactor 110 through the integrated instrument, and the collected data is transmitted to the collection equipment. The integrated control room can realize real-time monitoring of the operating status of the hydrogen production device 100 through the data in the collection equipment, thereby ensuring the normal operation of the hydrogen production device 100.

[0095] In addition, the dynamic balance of the equipment in the hydrogen production device 100 can be achieved by interlocking and linearly controlling (PID control) the equipment signals through a programmable logic controller (PLC), which is beneficial to the user's material preparation and the long-term stable operation of the equipment.

[0096] In this solution, the reactor 110 and the catalyst are highly sensitive to impurities. For example, acidic impurities in the raw materials pose a corrosion threat to carbon steel equipment. At the same time, impurities in the raw materials can cause the reforming catalyst to deactivate, thereby affecting the process stability. Therefore, in the embodiment of the present disclosure, the methanol product produced using natural gas as raw material is used as raw material to reduce impurities in the raw materials and reduce the damage of impurities in the raw materials to the hydrogen production device 100 and the catalyst, thereby ensuring the stability of the hydrogen production process.

[0097] The embodiment of the present disclosure adopts a shell-and-tube heat exchange structure 112 for the preheating section 1121, the gasification section 1122, the superheating section 1123 and the reforming section 1124 in the reactor 110, and the preheating section 1121, the gasification section 1122, the superheating section 1123 and the reforming section 1124 are integrated in the same shell 111, thereby avoiding the complex pipeline layout when using independent preheaters, vaporizers, superheaters and reformers to preheat, gasify, superheat and reform the raw materials, simplifying the structure and manufacturing of the reactor 110. The hydrogen process shortens the installation and commissioning period of the hydrogen production device 100 and reduces the hydrogen production cost. At the same time, it can also reduce the volume of the reactor 110, making the hydrogen production device 100 easy to transport. The present invention replaces the raw material storage tank with a methanol raw material pump 121 and an ion-free water pump, and eliminates the water washing tower for recovering methanol, thereby further reducing the footprint of the hydrogen production device 100, so that the hydrogen production device 100 can be skid-mounted, which is convenient for road transportation of the hydrogen production device 100 and reduces the transportation cost of the hydrogen production device 100.

[0098] In addition, the terms "first", "second", and "third" are used for descriptive purposes only and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Thus, a feature defined as "first", "second", and "third" may explicitly or implicitly include one or more of the feature. In the description of the present disclosure, the meaning of "plurality" is two or more, unless otherwise clearly and specifically defined.

[0099] It should be noted that "upper", "lower", "left", "right" and the like are only used for distinction to facilitate description, and do not impose any directional limitation on the embodiments of the present disclosure. For example, the "upper" may actually be "lower", "left", "right" and other directions. In the present disclosure, unless otherwise clearly specified and limited, the terms "assembly", "connection" and the like should be understood in a broad sense. For example, it may be a fixed connection, a detachable connection, or an integral whole; it may be a mechanical connection or an electrical connection; it may be a direct connection or an indirect connection through an intermediate medium; it may be the internal connection of two elements or the interaction relationship between two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the present disclosure can be understood according to the specific circumstances.

[0100] In the description of this specification, the description with reference to the terms "some embodiments", "exemplarily", etc. means that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present disclosure. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described may be combined in any one or more embodiments or examples in a suitable manner. In addition, those skilled in the art may combine and combine the different embodiments or examples described in this specification and the features of the different embodiments or examples, without contradiction.

[0101] Although the embodiments of the present disclosure have been shown and described above, it is to be understood that the above embodiments are exemplary and cannot be construed as limitations on the present disclosure. A person skilled in the art may change, modify, replace and modify the above embodiments within the scope of the present disclosure. Therefore, any changes or modifications made in accordance with the claims and specification of the present disclosure shall fall within the scope covered by the patent of the present disclosure.

Claims

1. A reactor, characterized in that: include: A housing, wherein the housing is arranged to form a receiving cavity, and the housing is further provided with a first inlet and a first outlet communicating with the receiving cavity; and A shell-and-tube heat exchange structure, the shell-and-tube heat exchange structure is connected to the shell and is arranged in the accommodating cavity, the shell-and-tube heat exchange structure includes a preheating section, a gasification section, a superheating section and a reforming section, and the preheating section, the gasification section, the superheating section and the reforming section are arranged in sequence from the first inlet to the first outlet.

2. The reactor according to claim 1, characterized in that The reactor further comprises an atomizing nozzle, which is arranged in the preheating section and is used for providing a purified solution to the containing chamber of the preheating section.

3. The reactor according to claim 1 or 2, characterized in that The shell is provided with a first liquid discharge port corresponding to the preheating section. The first liquid discharge port is located at the bottom of the shell. The first liquid discharge port is used to discharge the liquid medium in the accommodating chamber corresponding to the preheating section.

4. The reactor according to claim 1, characterized in that The reactor comprises a heat supply structure, which is connected to the shell and provides heat to at least a part of the shell-and-tube heat exchange structure.

5. The reactor according to claim 4, characterized in that The shell is provided with a plurality of heat supply inlets and a plurality of heat supply outlets, one heat supply inlet is provided corresponding to one heat supply outlet, the heat supply inlet is provided at the bottom of the shell, the heat supply outlet is provided at the top of the shell, the plurality of heat supply inlets are connected to the heat supply structure, and the heat supply structure is used to provide a heat supply medium; The gasification section, the superheating section and the reforming section are respectively provided with at least one heat supply inlet.

6. The reactor according to claim 1, characterized in that The accommodating chamber also includes a gas-liquid separation chamber, which is arranged between the gasification section and the superheating section. The gas-liquid separation chamber is used to separate the gas-liquid mixed medium, the gas phase medium moves toward the superheating section, and the liquid phase medium falls into the bottom of the gas-liquid separation chamber.

7. The reactor according to claim 6, characterized in that The shell corresponding to the gas-liquid separation chamber is provided with a second liquid discharge port, the second liquid discharge port is located at the bottom of the shell, and the second liquid discharge port is used to discharge the liquid medium in the gas-liquid separation chamber.

8. The reactor according to claim 1, characterized in that The reforming section is filled with a catalyst, and the raw material enters the reforming section and undergoes a reforming reaction based on the catalyst.

9. The reactor according to claim 1, characterized in that The shell is provided with a second inlet and a second outlet corresponding to the preheating section, the second inlet is located at the top of the shell, the second outlet is located at the bottom of the shell, the first outlet is connected to the second inlet, the gas phase medium is discharged from the first outlet, enters the accommodating chamber through the second inlet, and leaves the accommodating chamber through the second outlet to provide preheating heat.

10. The reactor according to claim 1, characterized in that The accommodating chamber comprises a preheating chamber, a gasification chamber, an overheating chamber and a reforming chamber, the preheating section is arranged in the preheating chamber, the gasification section is arranged in the gasification chamber, the overheating section is arranged in the overheating chamber, and the reforming section is arranged in the reforming chamber; The reactor includes a plurality of connectors, which are arranged between the preheating chamber, the gasification chamber, the superheating chamber and the reforming chamber, and two adjacent connectors are butted together to connect the preheating section, the gasification section, the superheating section and the reforming section in sequence.

11. A hydrogen production device, characterized in that: It comprises a raw material configuration device, a cold dryer and a reactor as described in any one of claims 1 to 10, wherein the raw material configuration device is connected to the first inlet, and the cold dryer is connected to the shell to collect the gas phase medium after the reaction of the reactor.

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