Dehydrogenation reactor

Abstract

The invention discloses a dehydrogenation reactor, and relates to the technical field of chemical equipment, the dehydrogenation reactor comprises a raw material tank, a preheating tank, a reaction tank and a separation tank, the preheating tank is connected with the raw material tank through a first material pipe; the reaction tank comprises a reaction chamber and a gas-liquid separation chamber, the preheating tank is connected with the reaction chamber through a second material pipe, the first material pipe is connected with the second material pipe through a connecting pipe, an interlayer chamber is arranged between the gas-liquid separation chamber and the outer wall of the reaction tank, and a heat conduction piece is arranged between the interlayer chamber and the gas-liquid separation chamber; the interlayer chamber is communicated with the preheating tank through a first air inlet pipe and a first air outlet pipe to form a first heat circulation loop; the separation tank comprises a secondary gas-liquid separation chamber and a multi-hydrocarbon adsorption chamber, the gas-liquid separation chamber is connected with the secondary gas-liquid separation chamber through a third material pipe, the multi-hydrocarbon adsorption chamber is provided with an exhaust pipe, and the secondary gas-liquid separation chamber is provided with a liquid discharge pipe. The problems that a dehydrogenation reaction device is low in waste heat utilization rate after reaction, and dehydrogenation reaction is high in energy consumption are effectively solved.

Description

Technical Field

[0001] The present application relates to the technical field of chemical equipment, and in particular to a dehydrogenation reactor. Background Art

[0002] Fossil energy has problems such as limited reserves, long renewable cycle and pollution, so clean renewable energy has become a hot spot for development and utilization. Hydrogen energy is a green and sustainable development energy with high combustion calorific value, abundant reserves and no pollution to the environment. It is recognized as a new type of secondary energy that is clean, pollution-free (zero carbon), renewable and abundant in reserves.

[0003] Dehydrogenation reaction is an important way to obtain hydrogen energy, but the existing dehydrogenation reaction equipment has a low utilization rate of the waste heat after the reaction, and the dehydrogenation reaction has the problem of high energy consumption. Summary of the invention

[0004] The main purpose of the present application is to provide a dehydrogenation reactor, aiming to solve the technical problems of low utilization rate of waste heat after the reaction in traditional dehydrogenation reaction devices and high energy consumption of the dehydrogenation reaction.

[0005] The technical solutions adopted in this application are as follows:

[0006] A dehydrogenation reactor, comprising:

[0007] Raw material tank;

[0008] A preheating tank, wherein the preheating tank is connected to the raw material tank via a first material pipe;

[0009] A reaction tank, wherein the reaction tank comprises a reaction chamber and a gas-liquid separation chamber, the preheating tank is connected to the reaction chamber via a second material pipe, the first material pipe and the second material pipe are connected via a connecting pipe, an interlayer chamber is provided between the gas-liquid separation chamber and the outer wall of the reaction tank, a heat conductor is provided between the interlayer chamber and the gas-liquid separation chamber, and the interlayer chamber is connected to the preheating tank via a first air inlet pipe and a first air outlet pipe to form a first heat circulation loop;

[0010] A separation tank, the separation tank comprises a secondary gas-liquid separation chamber and a multi-hydrocarbon adsorption chamber, the gas-liquid separation chamber is connected to the secondary gas-liquid separation chamber through a third material pipe, the multi-hydrocarbon adsorption chamber is provided with an exhaust pipe, and the secondary gas-liquid separation chamber is provided with a liquid discharge pipe.

[0011] Optionally, the connecting pipe is distributed in the preheating tank in the form of a serpentine pipe.

[0012] Optionally, an exhaust fan is provided in the preheating tank at one end of the first air outlet pipe.

[0013] Optionally, a multi-layer partition is arranged in the reaction chamber, and channel holes are alternately arranged at the bottom and top of the multi-layer partition to form a serpentine liquid flow channel in the reaction chamber, and a catalyst filler is arranged in the liquid flow channel.

[0014] Optionally, a heating coil is arranged outside the chamber wall of the reaction chamber, and a temperature control unit electrically connected to the heating coil is arranged outside the reaction tank.

[0015] Optionally, the dehydrogenation reactor further includes a recovery tank, the reaction chamber is connected to the recovery tank via a fourth material pipe, and the recovery tank is connected to the raw material tank via a fifth material pipe.

[0016] Optionally, an upper arched partition and a lower arc-shaped partition are provided in the gas-liquid separation chamber, the lower arc-shaped partition is provided with an air inlet, the upper arched partition is provided with an air outlet, and the air inlet and the air outlet are staggered.

[0017] Optionally, the gas-liquid separation chamber is located above the reaction chamber, and a chamber diameter of the gas-liquid separation chamber gradually decreases from one side of the reaction chamber to one side of the third material pipe.

[0018] Optionally, the heat conductor is arranged on the upper arched partition, and the gas-liquid separation chamber is provided with a through hole leading to the interlayer chamber, the heat conductor is led from the through hole to the interlayer chamber, and the diameter of the heat conductor located in the gas-liquid separation chamber is larger than the diameter of the heat conductor located in the interlayer chamber.

[0019] Optionally, the chamber diameter of the secondary gas-liquid separation chamber gradually decreases from the side of the third material pipe to the side of the multi-hydrocarbon adsorption chamber, the secondary gas-liquid separation chamber is connected to the multi-hydrocarbon adsorption chamber through a narrow opening, a wire mesh foam collector is provided at the narrow opening, and the multi-hydrocarbon adsorption chamber is filled with multi-hydrocarbon adsorbent.

[0020] Compared with the prior art, the beneficial effects of this application are:

[0021] A dehydrogenation reactor proposed in the present application includes a raw material tank, a preheating tank, a reaction tank and a separation tank, wherein the preheating tank is connected to the raw material tank through a first material pipe; the reaction tank includes a reaction chamber and a gas-liquid separation chamber, wherein the preheating tank is connected to the reaction chamber through a second material pipe, wherein the first material pipe and the second material pipe are connected through a connecting pipe, wherein an interlayer chamber is arranged between the gas-liquid separation chamber and the outer wall of the reaction tank, wherein a heat conducting member is arranged between the interlayer chamber and the gas-liquid separation chamber, wherein the interlayer chamber is connected to the preheating tank through a first air inlet pipe and a first air outlet pipe to form a first heat circulation Loop circuit; the separation tank includes a secondary gas-liquid separation chamber and a multi-hydrocarbon adsorption chamber, the gas-liquid separation chamber is connected to the secondary gas-liquid separation chamber through a third material pipe, the multi-hydrocarbon adsorption chamber is provided with an exhaust pipe, and the secondary gas-liquid separation chamber is provided with a liquid discharge pipe. The heat taken away by the gas generated during the dehydrogenation reaction is passed into the preheating tank to preheat the reaction raw materials, so that the reaction raw materials can quickly reach the reaction temperature in the reaction tank, thereby reducing the heat energy supply during the dehydrogenation reaction, effectively solving the problems of low utilization rate of waste heat after the dehydrogenation reaction device and high energy consumption of the dehydrogenation reaction. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 A schematic diagram of the structure of a dehydrogenation reactor provided in an embodiment of the present application;

[0023] Figure 2 This is a schematic diagram of the internal structure of the preheating tank;

[0024] Figure 3 Schematic diagram of the internal structure of the reaction tank;

[0025] Figure 4 Schematic diagram of the internal structure of the separation tank.

[0026] Description of the reference numerals in the accompanying drawings:

[0027] 1-raw material tank, 2-preheating tank, 3-reaction tank, 301-reaction chamber, 302-gas-liquid separation chamber, 303-catalyst filler, 304-interlayer chamber, 305-heating ring, 306-temperature control unit, 307-upper arched partition, 308-lower arc partition, 309-heat conducting member, 310-multi-layer partition, 4-separation tank, 401-secondary gas-liquid separation chamber, 402-wire mesh foam collector, 403-fine-pore partition, 404-multi-hydrocarbon adsorbent, 405-single-hole partition, 406-V-type partition, 407-vent pipe, 408-multi-hydrocarbon adsorption chamber, 409-interstitial cavity, 5-recovery tank, 6-first material pipe, 7-second material pipe, 8-third material pipe, 9-fourth material pipe, 10-fifth material pipe, 11-first air outlet pipe, 12-first air inlet pipe, 13-second air outlet pipe, 14-second air inlet pipe, 15-first delivery pump, 16-second delivery pump, 17-one-way valve, 18-solenoid valve, 19-three-way pipe joint, 20-recoil air pipe, 21-connecting pipe, 22-exhaust pipe, 23-liquid discharge pipe, 24-liquid outlet pipe, 25-exhaust fan. DETAILED DESCRIPTION

[0028] The following will be combined with the drawings in the embodiments of the present application to clearly and completely describe the technical solutions in the embodiments of the present application. Obviously, the described embodiments are only part of the embodiments of the present application, not all of the embodiments. Based on the embodiments in the present application, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of this application.

[0029] It should be noted that all directional indications in the embodiments of the present application (such as up, down, left, right, front, back, etc.) are only used to explain the relative position relationship, movement status, etc. between the components under a certain specific posture (as shown in the accompanying drawings). If the specific posture changes, the directional indication will also change accordingly.

[0030] In this application, unless otherwise clearly specified and limited, the terms "connection", "fixation", etc. should be understood in a broad sense. For example, "fixation" can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium, it can be the internal connection of two elements or the interaction relationship between two elements, unless otherwise clearly defined. For ordinary technicians in this field, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0031] In addition, if there are descriptions involving "first", "second", etc. in the embodiments of the present application, the descriptions of "first", "second", etc. are only used for descriptive purposes and cannot be understood as indicating or implying their relative importance or implicitly indicating the number of technical features indicated. Therefore, the features defined as "first" and "second" may explicitly or implicitly include at least one of the features. In addition, the meaning of "and / or" appearing in the full text includes three parallel schemes. Taking "A and / or B" as an example, it includes scheme A, or scheme B, or a scheme that satisfies both A and B. In addition, the technical solutions between the various embodiments can be combined with each other, but it must be based on the ability of ordinary technicians in the field to implement. When the combination of technical solutions is contradictory or cannot be implemented, it should be considered that such a combination of technical solutions does not exist and is not within the scope of protection required by this application.

[0032] Refer to the attached Figure 1 The embodiment of the present application provides a dehydrogenation reactor, comprising a raw material tank 1, a preheating tank 2, a reaction tank 3 and a separation tank 4. The raw material tank 1 is used to store the organic liquid involved in the dehydrogenation reaction, and a first material pipe 6 is arranged on the top of the raw material tank 1, and the first material pipe 6 is connected to the preheating tank 2. At the same time, a first delivery pump 15 is installed on the first material pipe 6, and the reaction organic liquid is delivered to the preheating tank 2 for preheating treatment through the first delivery pump 15, so that the organic liquid involved in the reaction can quickly reach the dehydrogenation reaction temperature.

[0033] The interior of the reaction tank 3 is divided into a reaction chamber 301 and a gas-liquid separation chamber 302, the reaction chamber 301 is at the bottom, and the gas-liquid separation chamber 302 is located above the reaction chamber 301. The water vapor produced after the dehydrogenation reaction moves upward due to its light weight, and most of the liquid is separated from the gas through the gas-liquid separation chamber 302. The preheating tank 2 is connected to the reaction chamber 301 through the second material pipe 7, and the first material pipe 6 and the second material pipe 7 are connected through the connecting pipe 21, and the preheated organic liquid is introduced into the reaction chamber 301 for dehydrogenation reaction. An interlayer chamber 304 is formed between the gas-liquid separation chamber 302 and the outer wall of the reaction tank 3. The interlayer chamber 304 is connected to the preheating tank 2 through the first air inlet pipe 12 and the first air outlet pipe 11 to form a first heat circulation loop. A heat conductor 309 is arranged between the interlayer chamber 304 and the gas-liquid separation chamber 302. The gas of the dehydrogenation reaction enters the gas-liquid separation chamber 302 with the residual heat of the reaction and contacts with the heat conductor 309. The heat conductor 309 absorbs the heat and performs heat exchange with the air in the interlayer chamber 304. The hot air in the interlayer chamber 304 is sent to the preheating tank 2 through the first air outlet pipe 11 to preheat the reaction organic liquid. The cold air after the heat exchange is completed is sent to the interlayer chamber 304 from the first air inlet pipe 12 for heat exchange, thereby utilizing the residual heat of the dehydrogenation reaction to provide a heat source for preheating the organic liquid.

[0034] The separation tank 4 includes a secondary gas-liquid separation chamber 401 and a multi-hydrocarbon adsorption chamber 408. The gas-liquid separation chamber 302 is connected to the secondary gas-liquid separation chamber 401 through a third material pipe 8. The multi-hydrocarbon adsorption chamber 408 is located above the secondary gas-liquid separation chamber 401. The multi-hydrocarbon adsorption chamber 408 is provided with an exhaust pipe 22, and the secondary gas-liquid separation chamber 401 is provided with a liquid discharge pipe 23.

[0035] It is not difficult to find that the dehydrogenation reactor provided in the embodiment of the present application, by adding a preheating tank 2 between the raw material tank 1 and the reaction tank 3, passes the heat carried away by the gas generated during the dehydrogenation reaction into the preheating tank 2, and preheats the reaction raw materials, so that the reaction raw materials can quickly reach the reaction temperature in the reaction tank 3, thereby reducing the heat energy supply during the dehydrogenation reaction, and effectively solving the problems of low utilization rate of waste heat after the reaction in the dehydrogenation reaction device and high energy consumption of the dehydrogenation reaction.

[0036] In the above, the raw material tank 1 is equipped with an explosion-proof valve, which is opened to release pressure in the case of a sudden increase in pressure in the tank to prevent explosion. At the same time, the raw material tank 1 is also equipped with a liquid level sensor to monitor the liquid level in the tank so as to remind the immediate replenishment of the reaction liquid. The raw material tank 1 selects a suitable storage tank type based on the nature, capacity and storage environment of the stored material, and the foundation should be kept firm and flat. The connection between the storage tank and the pipeline should be sealed to avoid leakage, corrosion and abnormal pressure. At the same time, it should be equipped with corresponding fire-fighting equipment to ensure safe production in the factory.

[0037] In one embodiment, if Figure 1 and 2 As shown, the connecting pipe 21 and the first material pipe 6 and the second material pipe 7 are an integrated structure, forming a good seal to avoid leakage. The connecting pipe is distributed in the preheating tank 2 in a serpentine shape. It can be understood that the serpentine-shaped connecting pipe 21 can effectively increase the residence time of the reaction organic liquid in the preheating tank 2, so that the organic liquid can increase the contact time with the hot air, thereby fully preheating the reaction organic liquid. In addition, as mentioned above, Figure 2 As shown, an exhaust fan 25 is installed inside the preheating tank 2 on one side of the first air outlet pipe 11. It is not difficult to understand that the exhaust fan 25 can speed up the air circulation in the preheating tank 2, so that hot air can be continuously delivered into the preheating tank 2, and cold air can be quickly discharged from the preheating tank 2, thereby effectively improving the preheating effect.

[0038] It can be seen that by setting the connecting pipe 21 in the preheating tank 2 as a serpentine pipe and providing an exhaust fan 25 on the side of the preheating tank 2 located at the first air outlet pipe 11, it has a positive effect on helping to improve the preheating effect of the organic liquid, which is of great significance for the organic liquid to quickly reach the reaction temperature. It can not only make full use of the waste heat of the dehydrogenation reaction, but also reduce the heat energy supply input of the dehydrogenation reaction, which plays a vital role in energy saving and consumption reduction.

[0039] In one embodiment, if Figure 1 and Figure 3 As shown, the interior of the reaction tank 3 is divided into a reaction chamber 301 and a gas-liquid separation chamber 302, the reaction chamber 301 is at the bottom of the tank, and the gas-liquid separation chamber 302 is above the reaction chamber 301. There is a gap between the outer wall of the reaction chamber 301 and the inner wall of the reaction tank 3, the preheating tank 2 is connected to the reaction chamber 301 through the second material pipe 7, and the preheated reaction organic liquid enters the reaction chamber 301 through the second material pipe 7. A multi-layer partition 310 is arranged in the reaction chamber 301, and the multi-layer partition 310 is arranged at intervals along the radial direction of the reaction tank 3. The bottom and top of the multi-layer partition 310 are staggered with channel holes to form a serpentine liquid flow channel in the reaction chamber 301, and a catalyst filler 303 is arranged in the liquid flow channel. It can be understood that the bottom and top of adjacent multi-layer partitions 310 are provided with staggered channel holes, and when the organic liquid flows through the multi-layer partitions 310, a serpentine liquid flow path is formed, thereby greatly increasing the residence time of the organic liquid in the reaction chamber 301. At the same time, catalyst fillers 303 are provided in the liquid flow channels between adjacent partitions, which can increase the contact time and number of contacts between the reacting organic liquid and the catalyst, so that the organic liquid can fully complete the dehydrogenation reaction.

[0040] Currently, catalysts can increase the rate of dehydrogenation reactions, and commonly used catalysts include metal catalysts (such as platinum, palladium, etc.) and non-metal catalysts (such as chromium oxide, iron oxide, etc.).

[0041] Of course, in this embodiment, the catalyst filler 303 is encapsulated in a mesh box, and the width of the mesh box is equal to the spacing between adjacent multi-layer partitions 310, so that the organic liquid can contact the catalyst filler 303 with the largest area. The mesh box can prevent the catalyst filler 303 from scattering, and the mesh box is hung on the multi-layer partition 310 by a hook. The mesh box can be lifted from the reaction chamber 301 by the hook to replace the catalyst filler 303, and the disassembly and assembly are convenient and simple.

[0042] It is also easy to understand that dehydrogenation is an oxidation reaction, which is usually carried out at high temperature to promote the reaction rate. The temperature range is generally between 100-300 ° C. Figure 1 and Figure 3 As shown, a heating coil 305 is disposed outside the chamber wall of the reaction chamber 301, and a temperature control unit 306 electrically connected to the heating coil 305 is disposed outside the reaction tank 3, and the temperature control unit 306 is connected to an industrial power supply. The heating coil 305 is controlled by the temperature control unit 306 to generate heat, and the organic liquid is heated to increase the reaction rate.

[0043] It is understandable that it is difficult to complete the dehydrogenation reaction of the organic liquid 100%, so the organic liquid after the reaction cannot be completely dehydrogenated. In order to avoid wasting resources, in a preferred embodiment, the dehydrogenation reactor also includes a recovery tank 5, and the reaction chamber 301 is connected to the recovery tank 5 through a fourth material pipe 9. The fourth material pipe 9 is arranged opposite to the third material pipe 8, and the third material pipe 8 and the fourth material pipe 9 are both submerged below the liquid surface of the organic liquid. The organic liquid after the reaction enters the recovery tank 5 through the fourth material pipe 9. The recovery tank 5 is connected to the raw material tank 1 through the fifth material pipe 10. The fifth material pipe 10 is equipped with a second delivery pump 16. The recovery tank 5 can return the organic liquid after the reaction to the raw material tank 1 for secondary dehydrogenation through purification and other methods, thereby improving the utilization rate of the raw materials. Of course, after the organic liquid after the reaction enters the recovery tank 5, the recovery tank 5 can also directly undergo secondary dehydrogenation through a separate reaction tank 3 without purification, so as to achieve the purpose of fully utilizing the organic raw materials, that is, Figure 1 As shown, a liquid outlet pipe 24 is provided at the bottom of the recovery tank 5, and the liquid outlet pipe 24 is directly connected to the attached reaction tank 3 for secondary dehydrogenation.

[0044] In one embodiment, if Figure 3 As shown, the gas-liquid separation chamber 302 is located above the reaction chamber 301, the third material pipe 8 is arranged on the top of the gas-liquid separation chamber 302, and an upper arched partition 307 and a lower arc-shaped partition 308 are arranged inside the gas-liquid separation chamber 302, a gas-liquid separation cavity is formed between the upper arched partition 307 and the lower arched partition 308, the arc-shaped convex directions of the lower arched partition 308 and the upper arched partition 307 are just opposite, the lower arched partition 308 is provided with an air inlet, the upper arched partition 307 is provided with an air outlet, and the air inlet and the air outlet are arranged alternately. Figure 3 The air inlet is centrally arranged on the lower arc-shaped partition 308, and the air outlet is arranged at both ends of the upper arched partition 307. It is not difficult to imagine that the gas produced after the dehydrogenation reaction carries moisture into the gas-liquid separation chamber from the air inlet. Since the air inlet and the air outlet are staggered, the hot air entering the gas-liquid separation chamber contacts the upper arched partition 307 upward, and the moisture in the gas forms droplets and falls to the lower arc-shaped partition 308. Since the arc-shaped protrusions of the lower arc-shaped partition 308 and the upper arched partition 307 are in opposite directions, an arc-shaped downward slope surface is formed on the inner side of the lower arc-shaped partition 308, so that the liquid falls into the reaction chamber 301 along the lower arc-shaped partition 308 and is discharged from the reaction chamber 301 from the fourth material pipe 9.

[0045] In addition, in the above, the chamber diameter of the gas-liquid separation chamber 302 gradually decreases from the side of the reaction chamber 301 to the side of the third material pipe 8. It can be understood that as the chamber diameter of the gas-liquid separation chamber 302 gradually decreases from the side of the reaction chamber 301 to the side of the third material pipe 8, the gas gradually converges after entering the gas-liquid separation chamber.

[0046] In one embodiment, if Figure 3As shown, an interlayer chamber 304 is formed between the gas-liquid separation chamber 302 and the reaction tank 3, and a through hole communicating with the interlayer chamber 304 is arranged on the chamber wall of the gas-liquid separation chamber 302. The heat conductor 309 is installed in the through hole and is located in both the interlayer chamber 304 and the gas-liquid separation chamber 302. The heat conductor 309 is located above the upper arch partition 307. The hot air after gas-liquid separation escapes from the air outlet and contacts the heat conductor 309. The heat conductor 309 is heated and transfers heat to the interlayer chamber 304 with a lower temperature located on the outside, thereby heating the low-temperature air in the interlayer chamber 304. The heated hot air enters the preheating tank 2 from the first air outlet pipe 11, and after completing heat exchange with the cold air in the preheating tank 2, it flows back to the interlayer chamber 304 from the first air inlet pipe 12 for further heating, thereby achieving the purpose of preheating the reaction organic liquid using the residual heat of the reaction. Of course, both the first air outlet pipe 11 and the first air inlet pipe 12 are provided with a one-way valve 17, so that the hot air flows from the interlayer chamber 304 to the preheating tank 2, and then flows back to the interlayer chamber 304 from the preheating tank 2, forming a one-way circulation.

[0047] Among the above, Figure 3 As shown, the diameter of the heat conductor 309 in the gas-liquid separation chamber 302 is larger than the diameter of the heat conductor 309 in the interlayer chamber 304. It is not difficult to see that the heat conductor 309 in the gas-liquid separation chamber 302 has a large diameter and can form a large contact area with the hot air, thereby absorbing the reaction waste heat to a large extent for reuse. Conventionally, the heat conductor 309 can be made of, but not limited to, a copper rod, which is low in cost and easy to manufacture.

[0048] In one embodiment, if Figure 4 As shown, a secondary gas-liquid separation chamber 401 and a multi-hydrocarbon adsorption chamber 408 are arranged in the separation tank 4, wherein the secondary gas-liquid separation chamber 401 is at the bottom of the tank, and the multi-hydrocarbon adsorption chamber 408 is above the secondary gas-liquid separation chamber 401. The chamber diameter of the secondary gas-liquid separation chamber 401 gradually decreases from the side of the third material pipe 8 to the side of the multi-hydrocarbon adsorption chamber 408, and the secondary gas-liquid separation chamber 401 and the multi-hydrocarbon adsorption chamber 408 are connected through a narrow opening, and a wire mesh frother 402 is arranged at the narrow opening, and the multi-hydrocarbon adsorption chamber 408 is filled with a multi-hydrocarbon adsorbent 404. It can be understood that most of the liquid in the gas can be removed by the gas-liquid separation chamber 302, and by arranging the wire mesh frother 402 at the narrow opening between the secondary gas-liquid separation chamber 401 and the multi-hydrocarbon adsorption chamber 408, the wire mesh frother 402 can prevent tiny liquid from entering the multi-hydrocarbon adsorption chamber 408 with the gas, thereby further realizing gas-liquid separation. A drain pipe 23 is provided at the bottom of the secondary gas-liquid separation chamber 401, and an exhaust pipe 22 is provided at the top of the multi-hydrocarbon adsorption chamber 408. Solenoid valves 18 are provided on the exhaust pipe 22 and the drain pipe 23. The drain pipe 23 discharges the separated liquid, and the exhaust pipe 22 discharges the hydrogen. Exhaust and liquid discharge cannot be carried out at the same time.

[0049] like Figure 4As shown, a fine-porous partition 403 is provided at the bottom of the multi-hydrocarbon adsorption chamber 408, and the fine-porous partition 403 is filled with a multi-hydrocarbon adsorbent 404 filler. The multi-hydrocarbon adsorbent 404 filler is granular and cannot pass through the fine-porous partition 403. A single-porous partition 405 is provided above the fine-porous partition 403 in the multi-hydrocarbon adsorption chamber 408, and the multi-hydrocarbon adsorbent 404 filler is filled between the fine-porous partition 403 and the single-porous partition 405. The multi-hydrocarbon adsorbent 404 filler uses C4~C8 hydrocarbons as absorbents, which can realize the separation of hydrogen and C2 and above hydrocarbons. The separated hydrogen has high purity, and its absorbent can be recycled, with low equipment investment and low energy consumption.

[0050] In a preferred embodiment, Figure 4 As shown, a V-shaped partition 406 is arranged on the single-hole partition 405, and a vent pipe 407 is arranged on the V-shaped partition 406. The vent pipe 407 and the hole body of the single-hole partition 405 are arranged alternately. The exhaust pipe 22 is connected to a three-way pipe joint 19. In addition to two interfaces of the three-way pipe joint 19 being the exhaust pipe 22, the other interface is connected to the recoil air pipe 20. The recoil air pipe 20 extends between the V-shaped partition 406 and the single-hole partition 405, and the gas outlet of the recoil air pipe 20 is blowing the hole body of the single-hole partition 405. It can be understood that by setting the recoil air pipe 20 to blow the hole body of the single-hole partition 405, the gas passing through the multi-hydrocarbon adsorbent 404 filler can be recoiled, and the gas circulation speed can be slowed down, thereby improving the absorption of multi-hydrocarbons, thereby improving the purity of hydrogen.

[0051] In addition, a gap cavity 409 is formed between the multi-hydrocarbon adsorption chamber 408 and the separation tank 4, and the interlayer chamber 304 also forms a second heat circulation loop with the gap cavity 409 through the second air inlet pipe 14 and the second air outlet pipe 13, and uses the waste heat generated by the reaction to dry the hydrogen.

[0052] In this embodiment, the reaction organic liquid is a mixture of one or more of unsaturated aromatic hydrocarbon compounds and / or heterocyclic unsaturated compounds and a solvent;

[0053] The unsaturated aromatic hydrocarbon compound is selected from benzene, toluene, ethylbenzene, propylbenzene, isopropylbenzene, o-xylene, p-xylene, m-xylene, styrene, naphthalene, anthracene, phenanthrene, phenol, aniline and derivatives thereof;

[0054] The heterocyclic unsaturated compound is selected from carbazole, indole, N-methylcarbazole, N-ethylcarbazole, N-n-propylcarbazole, N-isopropylcarbazole, N-n-butylcarbazole, N-methylindole, N-ethylindole, pyrazine, furan, pyrrole, thiazole, pyridine, cyclopentylpyrazine, benzothiazole and derivatives thereof;

[0055] The solvent is selected from one or more of methanol, ethanol, isopropanol, ethylene glycol, n-propanol, n-butanol, ethyl ether, methyl ether, acetonitrile, formic acid, acetic acid, ethyl acetate, methyl acetate, ethyl formate, n-butyl ether, isopropyl ether, dichloromethane, chloroform, tetrachloromethane, dichloroethane, n-hexane, cyclohexane, n-pentane, n-octane, carbon disulfide, and petroleum ether.

[0056] In summary, the dehydrogenation reactor provided in the embodiment of the present application has the following working process:

[0057] The reaction organic liquid is delivered to the preheating tank 2 through the first delivery pump 15, and the reaction organic liquid entering the preheating tank 2 is preheated by the residual heat after the dehydrogenation reaction. After the preheated reaction organic liquid enters the reaction chamber 301 to complete the dehydrogenation reaction, the reaction liquid flows out from the fourth material pipe 9, and the produced gas passes through the gas-liquid separation chamber 302 to complete the first gas-liquid separation. The gas escapes from the gas-liquid separation chamber 302 and rises to contact the heat conductor 309. After completing the heat exchange with the heat conductor 309, the heat conductor 309 heats the air in the interlayer chamber 304 for preheating the preheating tank 2. The gas enters the secondary gas-liquid separation chamber 401 through the third material pipe 8, and the gas is separated from the gas again by the wire mesh sparger 402. The gas enters the multi-hydrocarbon adsorption chamber 408 to purify the hydrogen, thereby obtaining hydrogen with higher purity.

[0058] The above description is only a preferred embodiment of the present application and is not intended to limit the present application. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present application should be included in the protection scope of the present application.

Claims

1. A dehydrogenation reactor, characterized in that: include: Raw material tank; A preheating tank, wherein the preheating tank is connected to the raw material tank via a first material pipe; A reaction tank, wherein the reaction tank comprises a reaction chamber and a gas-liquid separation chamber, the preheating tank is connected to the reaction chamber via a second material pipe, the first material pipe and the second material pipe are connected via a connecting pipe, an interlayer chamber is provided between the gas-liquid separation chamber and the outer wall of the reaction tank, a heat conductor is provided between the interlayer chamber and the gas-liquid separation chamber, and the interlayer chamber is connected to the preheating tank via a first air inlet pipe and a first air outlet pipe to form a first heat circulation loop; A separation tank, the separation tank comprises a secondary gas-liquid separation chamber and a multi-hydrocarbon adsorption chamber, the gas-liquid separation chamber is connected to the secondary gas-liquid separation chamber through a third material pipe, the multi-hydrocarbon adsorption chamber is provided with an exhaust pipe, and the secondary gas-liquid separation chamber is provided with a liquid discharge pipe.

2. The dehydrogenation reactor according to claim 1, characterized in that The connecting pipe is distributed in the preheating tank in the form of a serpentine pipe.

3. The dehydrogenation reactor according to claim 1 or 2, characterized in that: An exhaust fan is arranged in the preheating tank at one end of the first air outlet pipe.

4. The dehydrogenation reactor according to claim 1, characterized in that A multi-layer partition is arranged in the reaction chamber, and channel holes are arranged alternately at the bottom and top of the multi-layer partition to form a serpentine liquid flow channel in the reaction chamber, and a catalyst filler is arranged in the liquid flow channel.

5. The dehydrogenation reactor according to claim 1 or 4, characterized in that: A heating coil is arranged outside the chamber wall of the reaction chamber, and a temperature control unit electrically connected to the heating coil is arranged outside the reaction tank.

6. The dehydrogenation reactor according to claim 5, characterized in that It also includes a recovery tank, the reaction chamber is connected to the recovery tank through a fourth material pipe, and the recovery tank is connected to the raw material tank through a fifth material pipe.

7. The dehydrogenation reactor according to claim 1, characterized in that An upper arched partition and a lower arc-shaped partition are arranged in the gas-liquid separation chamber, the lower arc-shaped partition is provided with an air inlet, the upper arched partition is provided with an air outlet, and the air inlet and the air outlet are arranged alternately.

8. The dehydrogenation reactor according to claim 1 or 7, characterized in that: The gas-liquid separation chamber is located above the reaction chamber, and the chamber diameter of the gas-liquid separation chamber gradually decreases from the reaction chamber side to the third material pipe side.

9. The dehydrogenation reactor according to claim 7, characterized in that The heat conductor is arranged on the upper arched partition, and the gas-liquid separation chamber is provided with a through hole leading to the interlayer chamber. The heat conductor is led from the through hole to the interlayer chamber. The diameter of the heat conductor located in the gas-liquid separation chamber is larger than the diameter of the heat conductor located in the interlayer chamber.

10. The dehydrogenation reactor according to claim 1, characterized in that The chamber diameter of the secondary gas-liquid separation chamber gradually decreases from the side of the third material pipe to the side of the multi-hydrocarbon adsorption chamber. The secondary gas-liquid separation chamber is connected to the multi-hydrocarbon adsorption chamber through a narrow opening. A wire mesh foam collector is provided at the narrow opening. The multi-hydrocarbon adsorption chamber is filled with a multi-hydrocarbon adsorbent.

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