A dehydrogenation system and method

Abstract

The application provides a dehydrogenation system and method. The dehydrogenation system comprises a vaporizer, a superheater, a mixer, a dehydrogenation reactor, a heat conducting medium circulating unit and a separator, the shell side inlet of the dehydrogenation reactor is connected to the outlet of the mixer, the superheater and the shell side outlet of the vaporizer in sequence, the tube side outlet of the dehydrogenation reactor is connected to the tube side inlet of the superheater and the vaporizer in sequence, and the shell side inlet and the shell side outlet of the dehydrogenation reactor are connected to the heat conducting medium circulating unit. The dehydrogenation method comprises the following steps: after the dehydrogenation raw material is vaporized, superheated and mixed with a carrier gas, the dehydrogenation raw material is introduced into the dehydrogenation reactor to react; the dehydrogenation reactor is supplied with heat by the heat conducting medium circulating unit; after the material after the dehydrogenation reaction enters the superheater and the vaporizer to provide heat for the superheating and vaporization of the dehydrogenation raw material, the dehydrogenation product and hydrogen are obtained. The dehydrogenation system and method provided by the application improve the utilization rate of the catalyst, realize the step-by-step utilization of heat, and have the advantages of high efficiency, low energy consumption and the like.

Description

TECHNICAL FIELD

[0001] The present application relates to a dehydrogenation system and method, in particular to an organic liquid hydrogen storage medium dehydrogenation system and method, belonging to the technical field of hydrogen storage medium dehydrogenation. BACKGROUND

[0002] Hydrogen is a recognized clean energy, and stands out in the energy field as a low-carbon and zero-carbon energy. The industry chain for utilizing hydrogen energy includes hydrogen production, hydrogen storage and transportation, and hydrogen application. In the process of hydrogen storage and transportation, due to the mismatch between hydrogen production and application, hydrogen needs to be transported over a long distance. However, hydrogen is flammable and explosive, and is difficult to store and transport. Therefore, it is urgent to find a large-scale hydrogen storage technology with low energy consumption, high hydrogen storage density, and safe operation and transportation at normal temperature and pressure.

[0003] Currently, the main hydrogen storage methods include low-temperature liquid hydrogen storage, high-pressure gaseous hydrogen storage, metal hydride hydrogen storage, and organic liquid hydrogen storage. Among them, low-temperature liquid hydrogen storage and high-pressure gaseous hydrogen storage are the most common. However, low-temperature liquid hydrogen storage is limited by the extremely low temperature (-252℃), and requires extremely harsh requirements for the material and processing and manufacturing of the storage equipment, and the storage and transportation cost is extremely high, and currently it is still not possible to achieve large-scale application. High-pressure gaseous hydrogen storage is a relatively widely used hydrogen storage and transportation method, and the hydrogen transportation of the hydrogen refueling station built in the market is basically gaseous transportation by high-pressure tank trucks. However, the transportation cost of high-pressure gaseous hydrogen storage is high, and the transportation pressure is too high (above 20 MPaG), which leads to poor transportation safety, and restricts the development of large-scale and long-distance storage and transportation.

[0004] Organic liquid hydrogen storage is to store and release hydrogen by reversible chemical reaction of specific organic unsaturated compounds (i.e., storage oil) such as olefins, alkynes or aromatic hydrocarbons, and hydrogen gas under the action of a catalyst to generate alkane compounds (i.e., hydrogen oil). The storage oil and hydrogen oil are both liquid at normal temperature and pressure, and are fully compatible with petroleum-based storage and transportation facilities, which can greatly reduce the hydrogen transportation cost and improve the safety of hydrogen storage and transportation. In some scenarios, it can effectively solve the current problems faced by the hydrogen energy industry in storage and transportation, and has a broad development prospect. Therefore, the organic liquid hydrogen storage technology has the advantages of low hydrogen storage pressure, small long-distance transportation loss, high safety, and low cost, and is a promising hydrogen storage and transportation technology. The dehydrogenation process of the organic liquid hydrogen storage medium is an important link of the organic liquid hydrogen storage technology. However, the current dehydrogenation technology of the organic liquid hydrogen storage medium usually faces problems such as catalyst carbon deposition, unstable conversion rate during dehydrogenation, high energy consumption, and high cost.

[0005] Therefore, it is one of the problems to be solved in the field to develop a new dehydrogenation system and method, in particular a new organic liquid hydrogen storage medium dehydrogenation system and method. SUMMARY

[0006] To solve the above technical problems, the present application aims to provide a dehydrogenation system and method. The dehydrogenation system and method provided by the present application can improve the utilization rate of catalyst and realize the step-by-step utilization of heat, having the advantages of high efficiency, low energy consumption, etc.

[0007] To achieve the above-mentioned purpose, the present application provides a dehydrogenation system, which at least comprises a vaporizer, a superheater, a mixer, a dehydrogenation reactor, a heat conducting medium circulating unit and a separator.

[0008] The vaporizer is provided with a shell inlet, a first shell outlet, a first tube inlet and a first tube outlet.

[0009] The superheater is provided with a shell inlet, a shell outlet, a first tube inlet and a first tube outlet.

[0010] The mixer is provided with a dehydrogenation raw material inlet, a carrier gas inlet and a mixed material outlet.

[0011] The dehydrogenation reactor is provided with a tube inlet at the top and a tube outlet at the bottom, and the side wall of the dehydrogenation reactor is provided with a shell inlet and a shell outlet.

[0012] The separator is provided with a material inlet, a gas phase outlet and a liquid phase outlet.

[0013] The shell inlet of the vaporizer is connected with a dehydrogenation raw material conveying pipeline, the first shell outlet of the vaporizer is connected to the shell inlet of the superheater through a pipeline, the shell outlet of the superheater is connected to the dehydrogenation raw material inlet of the mixer through a pipeline, the carrier gas inlet of the mixer is connected with a carrier gas conveying pipeline, the mixed material outlet of the mixer is connected to the tube inlet at the top of the dehydrogenation reactor through a pipeline, the tube outlet at the bottom of the dehydrogenation reactor is connected to the first tube inlet of the superheater through a pipeline, the first tube outlet of the superheater is connected to the first tube inlet of the vaporizer through a pipeline, and the first tube outlet of the vaporizer is connected to the material inlet of the separator through a pipeline.

[0014] The dehydrogenation reactor is provided with a catalyst bed in the tube.

[0015] The shell inlet and the shell outlet of the dehydrogenation reactor are connected to the heat conducting medium circulating unit for circulating heat supply to the dehydrogenation reactor by using heat conducting medium.

[0016] According to the embodiment of the present application, preferably, the dehydrogenation system further comprises a dehydrogenation feedstock buffer tank, which is connected to the dehydrogenation feedstock delivery pipeline, and a metering pump is arranged on the dehydrogenation feedstock delivery pipeline. In an embodiment of the present application, a booster pump can be further arranged on the dehydrogenation feedstock delivery pipeline. The dehydrogenation feedstock from outside the boundary can first enter the dehydrogenation feedstock buffer tank, and then, after being pressurized and metered, be delivered into the vaporizer through the dehydrogenation feedstock delivery pipeline.

[0017] According to the embodiment of the present application, preferably, the dehydrogenation system further comprises a vaporizer temperature control pipeline, one end of which is in communication with the pipeline connecting the first tube pass outlet of the superheater and the first tube pass inlet of the vaporizer, and the other end of which is in communication with the pipeline connecting the first tube pass outlet of the vaporizer and the material inlet of the separator, for adjusting the amount of material after dehydrogenation reaction entering the tube pass of the vaporizer, and further adjusting the temperature of the vaporizer for vaporizing the dehydrogenation feedstock.

[0018] According to the embodiment of the present application, preferably, the dehydrogenation system further comprises a first cooler, and the first tube pass outlet of the vaporizer is connected to the material inlet of the separator through the first cooler.

[0019] In the dehydrogenation system described above, preferably, the superheater further comprises a second tube pass inlet and a second tube pass outlet, for allowing other heat-conducting medium to enter the superheater as a heat source to provide heat for the superheating of the dehydrogenation feedstock. More preferably, the other heat-conducting medium comprises one or a combination of several of heat-conducting oil, molten salt and superheated medium-pressure steam. In an embodiment of the present application, the pressure of the superheated medium-pressure steam can be 2-8 MPaG.

[0020] In the dehydrogenation system described above, preferably, the vaporizer further comprises a second tube pass inlet and a second tube pass outlet, for allowing other heat-conducting medium to enter the vaporizer as a heat source to provide heat for the vaporization of the dehydrogenation feedstock. More preferably, the other heat-conducting medium comprises one or a combination of several of heat-conducting oil, molten salt and superheated medium-pressure steam. In an embodiment of the present application, the pressure of the superheated medium-pressure steam can be 2-8 MPaG. Further preferably, the second tube pass inlet of the vaporizer is connected to the second tube pass outlet of the superheater through a pipeline.

[0021] In the above dehydrogenation system, preferably, the vaporizer is further provided with a second shell side outlet, which is connected with a heavy component discharge line. More preferably, the above dehydrogenation system further comprises a heavy component collection tank, which is connected to the heavy component discharge line for collecting the heavy components contained in the dehydrogenation feedstock, i.e. the heavy components difficult to be vaporized in the dehydrogenation feedstock.

[0022] In the above dehydrogenation system, preferably, a preheater is arranged on the carrier gas delivery line for preheating the carrier gas.

[0023] In the above dehydrogenation system, preferably, the mixer comprises a static mixer.

[0024] In the above dehydrogenation system, preferably, the dehydrogenation reactor comprises a multi-stage isothermal dehydrogenation reactor.

[0025] Specifically, the dehydrogenation reactor comprises a reactor shell, a reaction tube, a tube side inlet arranged at the top of the reactor shell, a tube side outlet arranged at the bottom of the reactor shell, a shell side inlet arranged at the sidewall of the reactor shell and a shell side outlet arranged at the sidewall of the reactor shell.

[0026] The reactor shell comprises a plurality of reaction zones and at least one non-reaction zone, which separates the plurality of reaction zones;

[0027] The reaction tube is arranged in the plurality of reaction zones in the reactor shell; the reaction tube in each reaction zone is arranged above an upper tube plate and below a lower tube plate for supporting and fixing the reaction tube; the upper tube plate in each reaction zone is arranged above a gas distributor; a catalyst bed is arranged in the reaction tube; the tube side inlet arranged at the top of the reactor shell and the tube side outlet arranged at the bottom of the reactor shell are in communication with the reaction tube.

[0028] In the plurality of reaction zones, the region between the reaction tube and the reactor shell is a shell side, and the sidewall of the reactor shell in each reaction zone is arranged with at least one shell side inlet and at least one shell side outlet.

[0029] In some embodiments of the present application, in the dehydrogenation reactor, the number of the plurality of reaction zones is more than two; specifically, the number of the plurality of reaction zones is 2, 3, 4, 5 or 6; preferably, the number of the plurality of reaction zones is 3-5.

[0030] In some embodiments of the present application, in the dehydrogenation reactor, the number of the reaction tube in each reaction zone can be adjusted according to the size of the dehydrogenation reactor, and the number is generally 1-1000. Generally, the number of the reaction tube in each reaction zone is the same.

[0031] In some specific embodiments of the present invention, the reaction tubes in the dehydrogenation reactor are arranged in a triangular, square, or rhomboid pattern, etc. The arrangement of the reaction tubes refers to the equidistant spacing between several adjacent tubes (three or four) according to the above-described pattern.

[0032] In some specific embodiments of the present invention, in the dehydrogenation reactor, the inner wall of the reaction tube is provided with a plurality of baffles to create turbulent flow of fluid within the cavity of the reaction tube, thereby promoting a complete reaction. Preferably, the baffles include a plurality of first baffles and a plurality of second baffles. Viewed from a cross-section of the reaction tube in the vertical direction, the first baffles may be configured to have a portion perpendicular to the inner wall of the reaction tube and a portion parallel to the inner wall, and the second baffles may be configured to have a portion perpendicular to the inner wall of the reaction tube and a portion intersecting the inner wall on an extended line. This allows turbulent flow of fluid to be created within the cavity of the reaction tube, promoting a complete reaction.

[0033] In some specific embodiments of the present invention, in the dehydrogenation reactor, a catalyst loading port is further provided on the side wall of the reactor shell, and the catalyst loading port is located in the non-reaction zone. The catalyst can be loaded into the reaction tube through this catalyst loading port.

[0034] In some specific embodiments of the present invention, in the dehydrogenation reactor, the gas distributor includes a distribution plate with a plurality of vent holes arranged in a ring around the center of the distribution plate. Specifically, the distribution plate may be circular in shape, with the vent holes arranged in a ring around the center of the distribution plate.

[0035] In some specific embodiments of the present invention, the dehydrogenation reactor is further provided with a plurality of temperature measuring instruments. Specifically, the number of temperature measuring instruments can be two, respectively located at the tube inlet and tube outlet of the dehydrogenation reactor. Alternatively, the number of temperature measuring instruments can be three or more, respectively located at the tube inlet and tube outlet of the dehydrogenation reactor and in the catalyst bed of each reaction zone. The multi-stage isothermal dehydrogenation reactor of the present invention can be equipped with two or three or more multi-point temperature measuring instruments, which facilitates monitoring the isothermal reaction process of each reaction zone, and can timely control the flow rate and temperature of the heat transfer medium entering the shell side of the dehydrogenation reactor based on the monitored data, thereby precisely controlling the isothermal reaction process of each reaction zone.

[0036] The multi-section isothermal dehydrogenation reactor of the present application is designed with multiple reaction sections, and by controlling the heating temperature of each reaction section, the isothermal reaction of each reaction section can be realized, and the heat can be reasonably utilized, so that the reaction is more thorough, and the catalyst loading amount can be reduced, the investment can be reduced, and the catalyst utilization rate can be more efficient. Furthermore, the upper tube plate of each reaction section of the multi-section isothermal dehydrogenation reactor of the present application is provided with a gas distributor above, and the two adjacent reaction sections are separated by the non-reaction section formed between the lower tube plate of the upper reaction section and the upper tube plate of the lower reaction section. The gas distributor is beneficial to the uniform entry of the mixed gas of the dehydrogenation raw material and the carrier gas into the reaction tube, and the gas is redistributed by the gas distributor provided above the upper tube plate in the non-reaction section, so that the reaction material is redistributed, which is beneficial to the dehydrogenation reaction and improves the conversion efficiency. At the same time, the multi-section isothermal dehydrogenation reactor of the present application can be provided with two or more multi-point temperature measuring instruments, so that by using the multi-section isothermal dehydrogenation reactor specially designed in the present application, the progress of the isothermal reaction can be controlled by the different heating temperature of each reaction section, so that a higher conversion efficiency can be realized.

[0037] In some embodiments of the present application, the catalyst can be a dehydrogenation catalyst commonly used in dehydrogenation technology, and the present application does not make special limitations thereon.

[0038] In the above-mentioned dehydrogenation system, preferably, the heat-conducting medium circulation unit at least comprises a heat-conducting medium storage device, a heat-conducting medium heating device and a heat-conducting medium conveying pump; the heat-conducting medium heating device is connected with the heat-conducting medium storage device and used for heating the heat-conducting medium; the heat-conducting medium storage device is provided with at least a heat-conducting medium inlet and a heat-conducting medium outlet, the heat-conducting medium outlet of the heat-conducting medium storage device is connected with the shell inlet of the dehydrogenation reactor through a pipeline and the heat-conducting medium conveying pump, and the shell outlet of the dehydrogenation reactor is connected with the heat-conducting medium inlet of the heat-conducting medium storage device through a pipeline. In some embodiments of the present application, since the dehydrogenation reactor is a multi-section isothermal dehydrogenation reactor, the shell inlets of each reaction section can be converged into a total pipeline through branch pipelines and valves and then connected with the heat-conducting medium outlet of the heat-conducting medium storage device, and similarly, the shell outlets of each reaction section can also be converged into a total pipeline through branch pipelines and valves and then connected with the heat-conducting medium inlet of the heat-conducting medium storage device.

[0039] In some embodiments of the present application, the heat-conducting medium circulation unit further comprises a second cooler, and the shell outlet of the dehydrogenation reactor is connected with the inlet of the heat-conducting medium storage device through a pipeline and the second cooler.

[0040] In some embodiments of the present application, the heat-conducting medium comprises one or more of a combination of heat-conducting oil, molten salt, and superheated medium-pressure steam. The superheated medium-pressure steam can have a pressure of 2-8 MPaG.

[0041] In some embodiments of the present application, the heat-conducting medium heating device comprises a direct heating device and / or an indirect heating device, which can specifically comprise one or more of a combination of an electric heater, a combustion furnace, and a heat exchanger. The heat exchanger can specifically comprise a regenerative heat exchanger. In an embodiment of the present application, the combustion furnace preferably uses a combustion furnace with an air distribution device to provide heat for the heat-conducting medium through the fuel (heat source) and the air distribution device.

[0042] In some embodiments of the present application, the heat source of the heat-conducting medium heating device comprises one or more of a combination of fuel, waste heat, and electricity. The fuel can comprise one or more of a combination of natural gas, coal, heavy oil, and low-calorific-value gas. Preferably, the heavy oil in the fuel comprises heavy components from the heavy component collection tank. Common low-calorific-value gas mainly comprises low-calorific-value tail gas in chemical processes, blast furnace gas, petroleum chemical smelting tail gas, and low-concentration coal gas in coal mines. The waste heat can comprise plant waste heat, which can specifically comprise waste heat generated by pyrolysis carbonization or incineration in a plant. More specifically, the waste heat can comprise waste heat generated by pyrolysis carbonization or incineration of one or more of a combination of sludge, garbage, hazardous waste, organic matter, and organic solid waste. For example, waste heat from a garbage incineration plant and / or waste heat from a solid waste disposal plant.

[0043] In some embodiments of the present application, when the heat source of the heat-conducting medium heating device comprises waste heat and / or electricity, the heat-conducting medium circulation unit further comprises a coupler connected with a waste heat medium input pipeline and connected with the heat-conducting medium heating device. Specifically, the coupler can comprise a regenerative waste heat power generation device and / or a regenerative waste heat conversion device, which can be conventional devices in the field. The present application can use plant waste heat coupling as the heat source of the heat-conducting medium heating device, so that the plant waste heat heats the heat-conducting medium after passing through the coupler, effectively achieving cascade utilization of energy and solving the problems of high energy consumption and high cost in heating the heat-conducting medium.

[0044] In some embodiments of the present application, the heat-conducting medium circulation unit can further comprise a PLC control module for monitoring and controlling the heating and circulation process of the heat-conducting medium.

[0045] According to the embodiments of the present application, the dehydrogenation system preferably further comprises a liquid phase storage device connected to the liquid phase outlet of the separator through a pipeline.

[0046] According to the specific embodiment of the present application, preferably, the dehydrogenation system further comprises a gas phase purification and storage device connected to the gas phase outlet of the separator by a pipeline. More preferably, the liquid phase storage device is connected to the gas phase purification and storage device by a pipeline for discharging the gas phase components in the liquid phase storage device to the gas phase purification and storage device.

[0047] In the dehydrogenation system described above, preferably, the gas phase purification and storage device is in communication with the carrier gas delivery pipeline for recycling the carrier gas.

[0048] According to the specific embodiment of the present application, the dehydrogenation system described above can further comprise conventional valves such as pressure regulating valves, temperature regulating valves, flow regulating valves, and conventional pumps and other components, which can be arranged according to actual conditions by those skilled in the art.

[0049] The second aspect of the present application provides a dehydrogenation method using the dehydrogenation system described above, which comprises at least the following steps:

[0050] (1) The dehydrogenation raw material is vaporized in the shell side of the vaporizer, superheated in the shell side of the superheater, mixed with the carrier gas in the mixer, and then enters the tube side of the dehydrogenation reactor for dehydrogenation reaction under the action of the catalyst;

[0051] (2) The heat conducting medium from the heat conducting medium circulation unit enters the shell side of the dehydrogenation reactor to provide heat for the dehydrogenation reaction, and the heated heat conducting medium flows out of the shell side of the dehydrogenation reactor and enters the heat conducting medium circulation unit to provide cyclic heat for the dehydrogenation reactor;

[0052] (3) The dehydrogenation reaction material flows out of the tube side of the dehydrogenation reactor, enters the tube side of the superheater to provide heat for the superheating of the dehydrogenation raw material, and then enters the tube side of the vaporizer to provide heat for the vaporization of the dehydrogenation raw material, so that the heated dehydrogenation reaction material enters the separator for gas-liquid separation to obtain the dehydrogenation product and hydrogen.

[0053] In the dehydrogenation method described above, preferably, the dehydrogenation raw material comprises methylcyclohexane, and the dehydrogenation product comprises toluene.

[0054] According to the specific embodiment of the present application, preferably, the dehydrogenation method described above further comprises the following step: the dehydrogenation raw material first enters the dehydrogenation raw material buffer tank, is metered and selectively pressurized, and then enters the shell side of the vaporizer for vaporization.

[0055] In the dehydrogenation method described above, preferably, the carrier gas comprises hydrogen.

[0056] According to the specific embodiment of the present application, preferably, the dehydrogenation method further comprises the step of preheating the carrier gas before entering the mixer. More preferably, the preheating temperature of the carrier gas is 200-400℃. After the carrier gas is preheated and mixed with the dehydrogenation raw material, the production of carbon deposition can be effectively inhibited when the carrier gas enters the catalyst bed, thereby prolonging the service life of the catalyst.

[0057] In the dehydrogenation method described above, preferably, the mass ratio of the carrier gas to the dehydrogenation raw material is 0.3-0.5.

[0058] In the dehydrogenation method described above, preferably, the temperature of the dehydrogenation reaction is 300-400℃, and the pressure of the dehydrogenation reaction is 0.5-1.5 barG, more preferably 0.2-1.0 barG.

[0059] In the dehydrogenation method described above, preferably, a part of the dehydrogenation reaction material flowing out of the tube side of the superheater enters the tube side of the vaporizer to provide heat for the vaporization of the dehydrogenation raw material, and another part of the dehydrogenation reaction material flowing out of the tube side of the superheater enters the separator for gas-liquid separation.

[0060] In the dehydrogenation method described above, preferably, the temperature in the shell side of the vaporizer is controlled at 110-200℃, and the pressure of the vaporizer is controlled at 0.05-3 MPaG.

[0061] According to the specific embodiment of the present application, preferably, the dehydrogenation method further comprises the step of cooling the dehydrogenation reaction material after heat supply through the first cooler and then entering the separator for gas-liquid separation. Specifically, the dehydrogenation reaction material flowing out of the first tube side of the vaporizer and the another part of the dehydrogenation reaction material flowing out of the tube side of the superheater are cooled through the first cooler and then enter the separator for gas-liquid separation. More preferably, the temperature of the material cooled through the first cooler is 20-60℃.

[0062] The present application uses the waste heat of the dehydrogenation reaction material to vaporize the dehydrogenation raw material, and at the same time, a temperature control pipeline of the vaporizer is provided to adjust the amount of the dehydrogenation reaction material entering the tube side of the vaporizer, thereby achieving temperature control and regulation of the vaporization process while realizing heat cascade utilization. The dehydrogenation reaction material supplies heat to the superheater and the vaporizer, and after energy cascade utilization, it is cooled to a separable temperature and then subjected to gas-liquid separation. After the cooled dehydrogenation reaction material is subjected to gas-liquid separation by the separator, the materials with different phases can be effectively separated to achieve the purpose of collecting the product.

[0063] According to the specific embodiment of the present application, preferably, the dehydrogenation method further comprises the following step: other heat-conducting medium is introduced into the superheater as a heat source to provide heat for superheating the dehydrogenation raw material.

[0064] According to the specific embodiment of the present application, preferably, the dehydrogenation method further comprises the following step: other heat-conducting medium is introduced into the superheater as a heat source to provide heat for superheating the dehydrogenation raw material.

[0065] In some specific embodiments of the present application, the dehydrogenation method further comprises the following step: other heat-conducting medium is introduced into the superheater as a heat source to provide heat for superheating the dehydrogenation raw material, and then the heated other medium is introduced into the vaporizer as a heat source to provide heat for vaporizing the dehydrogenation raw material.

[0066] In some specific embodiments of the present application, the other heat-conducting medium comprises one or a combination of heat-conducting oil, molten salt and superheated medium-pressure steam. The pressure of the superheated medium-pressure steam can be 2-8 MPaG.

[0067] According to the specific embodiment of the present application, preferably, the dehydrogenation method further comprises the following step: the heavy components in the vaporizer shell side are periodically discharged into a heavy component collection tank. The period of discharge can be routinely adjusted by those skilled in the art according to the actual situation. The collected heavy components in the heavy component collection tank can be used as fuel for the heat-conducting medium circulation unit.

[0068] In some specific embodiments of the present application, the temperature of the dehydrogenation reaction material flowing out from the tube side of the dehydrogenation reactor is 300-400℃. The dehydrogenation reaction material is a gas-phase material, which is used as a heat source for superheating and vaporizing the dehydrogenation raw material, thereby realizing the cascade utilization of heat.

[0069] In the above-mentioned dehydrogenation method, preferably, the temperature of the heat-conducting medium introduced into the shell side of the dehydrogenation reactor is 300-400℃, more preferably 350-400℃. In some specific embodiments of the present application, the temperature of the heated heat-conducting medium flowing out from the shell side of the dehydrogenation reactor is reduced by 5-20℃ compared to the temperature of the heat-conducting medium introduced into the shell side of the dehydrogenation reactor, thereby ensuring isothermal reaction in each reaction zone.

[0070] In some specific embodiments of the present application, in the dehydrogenation reactor, the number of the multiple reaction zones is 3, and the uppermost, middle and lowermost three reaction zones are the first reaction zone, the second reaction zone and the third reaction zone, respectively. The temperature of the heat-conducting medium introduced into the shell side of the first reaction zone is 380-400℃, the temperature of the heat-conducting medium introduced into the shell side of the second reaction zone is 370-380℃, and the temperature of the heat-conducting medium introduced into the shell side of the third reaction zone is 350-370℃.

[0071] According to the specific embodiment of the present application, the reaction zone near the inlet of the tube side in the dehydrogenation reactor is designed to be high-temperature heat supply, the reaction zone near the outlet of the tube side is designed to be low-temperature heat supply, and the temperature gradient decreases from top to bottom, so that the heat can be reasonably utilized according to the different heat supply temperatures, the isothermal reaction of each reaction zone can be ensured, the reaction is more thorough, and the loading amount of the catalyst can be reduced, and the investment can be reduced.

[0072] In some specific embodiments of the present application, in the dehydrogenation reactor, the number of the reaction zones is 5, and the 5 reaction zones from top to bottom are the I reaction zone, the II reaction zone, the III reaction zone, the IV reaction zone and the V reaction zone, respectively. The temperature of the heat conduction medium entering the shell side of the I reaction zone is 390-400°C, the temperature of the heat conduction medium entering the shell side of the II reaction zone is 380-390°C, the temperature of the heat conduction medium entering the shell side of the III reaction zone is 370-380°C, the temperature of the heat conduction medium entering the shell side of the IV reaction zone is 360-370°C, and the temperature of the heat conduction medium entering the shell side of the V reaction zone is 350-360°C. According to the specific embodiment of the present application, the heat supply design of the 5 reaction zones can further reduce the loading amount of the catalyst, and the utilization rate of the catalyst can be more efficient.

[0073] In the above dehydrogenation method, preferably, step (2) specifically comprises: making the heat conduction medium enter the heat conduction medium storage device, heating the heat conduction medium by using the heat source of the heat conduction medium heat supply device, then making the heat conduction medium carrying heat enter the shell side of the dehydrogenation reactor to supply heat for the dehydrogenation reaction, and making the heat conduction medium after heat supply flow out from the shell side of the dehydrogenation reactor and re-enter the heat conduction medium storage device to supply heat for the dehydrogenation reactor by the heat conduction medium circulating unit. More preferably, the heat conduction medium is heated to 350-450°C by using the heat source of the heat conduction medium heat supply device, and further preferably to 380-450°C. More preferably, step (2) further comprises: after the heat conduction medium after heat supply flows out from the shell side of the dehydrogenation reactor, the heat conduction medium first enters the second cooler for cooling, and then re-enters the heat conduction medium storage device.

[0074] In the above dehydrogenation method, preferably, the heat conduction medium comprises one or a combination of several of heat conduction oil, molten salt and superheated medium-pressure steam. The pressure of the superheated medium-pressure steam can be 2-8 MPaG. In some specific embodiments of the present application, when the heat conduction medium is heat conduction oil, step (2) further comprises: boiling and exhausting the heat conduction oil in the heat conduction medium storage device. The boiling and exhausting of the heat conduction oil in the present application can avoid the problem of explosive boiling that may be caused when the heat conduction oil is heated by using the heat conduction medium heat supply device.

[0075] In the dehydrogenation method, preferably, the heat supply device for the heat-conducting medium comprises a direct heating device and / or an indirect heating device, which can specifically comprise one or a combination of electric heater, combustion furnace and heat exchanger. The heat exchanger can specifically comprise a regenerative heat exchanger.

[0076] In the dehydrogenation method, preferably, the heat source of the heat supply device for the heat-conducting medium comprises one or a combination of fuel, waste heat and electricity. The fuel can comprise one or a combination of natural gas, coal, heavy oil and low-calorific-value gas. Preferably, the heavy oil in the fuel comprises heavy components from the heavy component collection tank. Common low-calorific-value gas mainly comprises low-calorific-value tail gas in chemical processes, blast furnace gas, smelting tail gas in petroleum chemical industry, low-concentration coal gas in coal mines and the like. The waste heat can comprise plant waste heat, which can specifically comprise waste heat generated by pyrolysis carbonization or incineration of the plant. More specifically, the waste heat can comprise waste heat generated by pyrolysis carbonization or incineration of one or a combination of sludge, garbage, hazardous waste, organic matter and organic solid waste and the like. For example, waste heat from a garbage incineration plant and / or waste heat from a solid waste disposal plant and the like.

[0077] In the dehydrogenation method, preferably, when the heat source of the heat supply device for the heat-conducting medium comprises waste heat and / or electricity, step (2) further comprises: allowing the waste heat medium to enter the coupler and then heat the heat-conducting medium as the heat source of the heat supply device for the heat-conducting medium. More specifically, the waste heat medium is converted into electric energy after entering the coupler and then input into the heat supply device for the heat-conducting medium, so as to heat the heat-conducting medium.

[0078] According to the specific embodiments of the present application, the plant waste heat can be directly exchanged with the heat-conducting medium (the heat supply device for the heat-conducting medium adopts a heat exchanger), so as to heat the heat-conducting medium. Alternatively, the plant waste heat can be converted into electric energy through the coupler, and then the electric energy is used to heat the heat-conducting medium (the heat supply device for the heat-conducting medium adopts an electric heater).

[0079] In the dehydrogenation method, preferably, step (2) further comprises: monitoring and controlling the heating and circulation process of the heat-conducting medium by using a PLC control module.

[0080] The present application can utilize plant waste gas, plant waste heat and heavy oil in the heavy component collection tank to provide heat for the heat-conducting medium, so as to solve the problems of high cost and high energy consumption in heating the heat-conducting medium, and meanwhile, the heat-conducting medium carrying heat can uninterruptedly provide heat for the dehydrogenation reaction.

[0081] According to the specific embodiment of the present application, preferably, the dehydrogenation method further comprises the step of: purifying the obtained hydrogen gas in a gas phase purification and storage device, and the purity of the purified hydrogen gas is more than 99%.

[0082] According to the specific embodiment of the present application, preferably, the dehydrogenation method further comprises the step of: purifying the obtained hydrogen gas in a gas phase purification and storage device, and the purity of the purified hydrogen gas is more than 99%.

[0083] According to the specific embodiment of the present application, preferably, the dehydrogenation method further comprises the step of: purifying the obtained hydrogen gas in a gas phase purification and storage device, and the purity of the purified hydrogen gas is more than 99%.

[0084] The present application provides a dehydrogenation system and method, in particular, an organic liquid hydrogen storage medium dehydrogenation system and method. The dehydrogenation system and method of the present application have at least the following beneficial technical effects:

[0085] 1. By adding the carrier gas, the possibility of local contact overheating of the organic dehydrogenation raw material and the catalyst and the occurrence of side reactions is reduced, the carbon deposition problem in the catalyst reaction process is effectively inhibited, the service life of the catalyst is prolonged, and the economic benefit is improved;

[0086] 2. Through the special design of the multi-stage isothermal dehydrogenation reactor, in view of the large amount of heat absorption required for the dehydrogenation reaction of the dehydrogenation raw material in the gaseous state, the heating temperature of each reaction zone can be controlled, the isothermal reaction of each reaction zone can be realized, the heat can be reasonably utilized, the reaction can be more thorough, the reaction temperature can be adjusted at different stages of the reaction, and the catalyst loading amount can be reduced, the investment can be reduced, the conversion rate instability problem in the dehydrogenation process can be effectively solved, and the utilization rate of the catalyst can be improved;

[0087] 3. The material after the dehydrogenation reaction provides heat for the overheating and vaporization of the dehydrogenation raw material, the heat is utilized in stages, the resource integration in the system is realized, the energy consumption is effectively reduced, and the problems of high energy consumption and high cost in the existing organic liquid hydrogen storage medium dehydrogenation technology are solved;

[0088] 4. The heat-conducting medium is heated by using factory waste gas, factory waste heat, heavy oil in a heavy component collection tank, etc., especially the waste heat generated by pyrolysis carbonization or incineration of one or a combination of several of the following: sludge, garbage, hazardous waste, organic matter, and organic solid waste, which is used as the heat-conducting medium. Through cross-industry coupling of resources, the energy cascade utilization is effectively realized, and the problems of high energy consumption and high cost of the current heating of the heat-conducting medium are solved.

[0089] In summary, the technical scheme of the present application solves the problems of long-distance transportation of hydrogen, low safety, high cost, etc. in the prior art, has the advantages of low hydrogen storage pressure, small long-distance transportation loss, high safety, low cost, etc. It also solves the problem of catalyst carbon deposition in the dehydrogenation technology of organic liquid hydrogen storage medium, effectively solves the problem of unstable conversion rate in the dehydrogenation process, improves the utilization rate of the catalyst, realizes the cascade utilization of heat, solves the problems of high energy consumption and high cost in the dehydrogenation technology of organic liquid hydrogen storage medium, and effectively realizes the cascade utilization of energy through cross-industry coupling of resources, solves the problems of high energy consumption and high cost of the current heating of the heat-conducting medium. Therefore, the dehydrogenation system and method provided by the present application realize efficient and low-energy dehydrogenation of organic liquid hydrogen storage medium, and provide an effective solution for hydrogen storage and transportation. BRIEF DESCRIPTION OF DRAWINGS

[0090] Figure 1 The structure diagram of the dehydrogenation system provided by one embodiment of the present application is shown.

[0091] Figure 2 The structure diagram of the dehydrogenation reactor in the dehydrogenation system provided by one embodiment of the present application is shown.

[0092] Figure 3 The structure diagram of the reaction tube arranged in a triangular shape provided by one embodiment of the present application is shown.

[0093] Figure 4 The structure diagram of the reaction tube arranged in a diamond shape provided by one embodiment of the present application is shown.

[0094] Figure 5 The structure diagram of the baffle arranged on the inner wall of the reaction tube provided by one embodiment of the present application is shown.

[0095] Figure 6 The structure diagram of the gas distributor provided by one embodiment of the present application is shown.

[0096] Figure 7 The structure diagram of the heat-conducting medium circulation unit provided by one embodiment of the present application is shown.

[0097] Explanation of reference numerals:

[0098] 1 - dehydrogenation feed buffer tank; 2 - vaporizer; 3 - superheater; 4 - mixer; 5 - dehydrogenation reactor; 6 - heat transfer medium circulation unit; 7 - heavy component collection tank; 8 - separator; 9 - liquid phase storage device; 10 - gas phase purification and storage device; 11 - vaporizer temperature control line; 12 - preheater; 13 - first cooler;

[0099] 501 - reactor shell; 502 - reaction tube; 503 - reaction zone; 504 - non-reaction zone; 505 - upper tube sheet; 506 - lower tube sheet; 507 - gas distributor; 508 - catalyst loading port;

[0100] 5021 - first baffle; 5022 - second baffle;

[0101] 601 - heat transfer medium storage device; 602 - heat transfer medium heating device; 603 - heat transfer medium delivery pump; 604 - second cooler; 605 - coupler. DETAILED DESCRIPTION

[0102] In order to have a clearer understanding of the technical features, objectives and beneficial effects of the present application, the technical solutions of the present application are described in detail as follows, but it should not be understood as a limitation on the implementable scope of the present application.

[0103] It should be noted that, under the premise of not conflicting, each embodiment described below or each technical feature can be combined to form a new embodiment.

[0104] In the description of the present application, it should be understood that the terms "first", "second" and the like are only for the purpose of description and should not be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features, so the features with "first", "second" and the like can explicitly or implicitly include one or more of the features.

[0105] In the description of the present application, it should be understood that, unless otherwise explicitly specified and limited, the terms "connected", "connected" should be understood in a broad sense, for example, it can be fixedly connected, or it can be detachably connected, or integrally connected; it can be mechanically connected, or it can be electrically connected; it can be directly connected, or indirectly connected through an intermediate medium, or the communication inside two elements. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances.

[0106] Example 1

[0107] The present embodiment provides a dehydrogenation system, the structure of which is as shown in Figure 1As shown, the dehydrogenation system comprises a dehydrogenation raw material buffer tank 1, a vaporizer 2, a superheater 3, a mixer 4, a dehydrogenation reactor 5, a heat conducting medium circulating unit 6 (not shown), a heavy component collecting tank 7, a separator 8, a liquid phase storage device 9, a gas phase purification and storage device 10, a vaporizer temperature control pipeline 11, a preheater 12 and a first cooler 13. Figure 1

[0108] The vaporizer 2 is provided with a shell side inlet, a first shell side outlet, a second shell side outlet, a first tube side inlet and a first tube side outlet.

[0109] The superheater 3 is provided with a shell side inlet, a shell side outlet, a first tube side inlet and a first tube side outlet.

[0110] The mixer 4 is provided with a dehydrogenation raw material inlet, a carrier gas inlet and a mixed material outlet.

[0111] The dehydrogenation reactor 5 is provided with a tube side inlet at the top and a tube side outlet at the bottom, and the sidewall of the dehydrogenation reactor 5 is provided with a shell side inlet and a shell side outlet.

[0112] The separator 8 is provided with a material inlet, a gas phase outlet and a liquid phase outlet.

[0113] The shell side inlet of the vaporizer 2 is connected with a dehydrogenation raw material delivery pipeline, the dehydrogenation raw material buffer tank 1 is connected to the dehydrogenation raw material delivery pipeline, and a metering pump is arranged on the dehydrogenation raw material delivery pipeline. A booster pump can be further arranged on the dehydrogenation raw material delivery pipeline. Dehydrogenation raw material from outside the boundary region can first enter the dehydrogenation raw material buffer tank 1, and then can be sent into the vaporizer 2 through the dehydrogenation raw material delivery pipeline after being pressurized and metered.

[0114] The first shell side outlet of the vaporizer 2 is connected to the shell side inlet of the superheater 3 through a pipeline, the second shell side outlet of the vaporizer 2 is connected to the heavy component collecting tank 7 through a heavy component discharge pipeline, the shell side outlet of the superheater 3 is connected to the dehydrogenation raw material inlet of the mixer 4 through a pipeline, the carrier gas inlet of the mixer 4 is connected with a carrier gas delivery pipeline, the carrier gas delivery pipeline is provided with the preheater 12 for preheating the carrier gas, the mixed material outlet of the mixer 4 is connected to the tube side inlet at the top of the dehydrogenation reactor 5 through a pipeline, the tube side outlet at the bottom of the dehydrogenation reactor 5 is connected to the first tube side inlet of the superheater 3 through a pipeline, the first tube side outlet of the superheater 3 is connected to the first tube side inlet of the vaporizer 2 through a pipeline, and the first tube side outlet of the vaporizer 2 is connected to the material inlet of the separator 8 through a pipeline and the first cooler 13.

[0115] ​The dehydrogenation system further comprises a vaporizer temperature control pipeline 11, one end of which is in communication with the pipeline connecting the first tube pass outlet of the superheater 3 with the first tube pass inlet of the vaporizer 2, and the other end of which is in communication with the pipeline connecting the first tube pass outlet of the vaporizer 2 with the first cooler 13, for adjusting the amount of material after dehydrogenation reaction entering the tube pass of the vaporizer 2, and further adjusting the temperature of the vaporizer 2 vaporizing the dehydrogenation raw material.

[0116] The liquid phase storage device 9 is connected to the liquid phase outlet of the separator 8 through a pipeline. The gas phase purification and storage device 10 is connected to the gas phase outlet of the separator 8 through a pipeline. The liquid phase storage device 9 is connected to the gas phase purification and storage device 10 through a pipeline and a pressure regulating valve, for discharging the gas phase components entering the liquid phase storage device 9 to the gas phase purification and storage device 10. The gas phase purification and storage device 10 can be in communication with the carrier gas delivery pipeline, for reusing the carrier gas.

[0117] The shell pass inlet and the shell pass outlet of the dehydrogenation reactor 5 are connected to the heat conducting medium circulating unit 6, for circulating heat supply to the dehydrogenation reactor 5 by using heat conducting medium.

[0118] The vaporizer 2 is a special vaporizer for methylcyclohexane dehydrogenation, with a pressure range of 0.05-3 MPaG.

[0119] The mixer 4 is a static mixer.

[0120] The separator 8 is a gas-liquid separator.

[0121] As shown in Figure 2 The dehydrogenation reactor 5 is a multi-stage isothermal dehydrogenation reactor.

[0122] Specifically, the dehydrogenation reactor 5 comprises a reactor shell 501, a reaction tube 502, a tube pass inlet arranged at the top of the reactor shell 501, a tube pass outlet arranged at the bottom of the reactor shell 501, a shell pass inlet and a shell pass outlet arranged at the side wall of the reactor shell 501;

[0123] The reactor shell 501 comprises 3 reaction zones 503 and 2 non-reaction zones 504, and the non-reaction zones 504 separate the reaction zones 503;

[0124] The reaction tube 502 is arranged in the reaction zone 503 in the reactor shell 501; the upper tube plate 505 and the lower tube plate 506 are arranged above and below the reaction tube 502 of each reaction zone 503, for supporting and fixing the reaction tube 502; the gas distributor 507 is arranged above the upper tube plate 505 of each reaction zone 503; the catalyst bed is arranged in the reaction tube 502; the tube pass inlet arranged at the top of the reactor shell 501 and the tube pass outlet arranged at the bottom of the reactor shell 501 are communicated with the reaction tube 502.

[0125] In the reaction zone 503, the area between the reaction tube 502 and the reactor shell 501 is the shell pass; the shell pass inlet and the shell pass outlet are arranged on the side wall of the reactor shell 501 of each reaction zone 503; in each reaction zone 503, the shell pass inlet and the shell pass outlet are oppositely arranged on the side wall of the reactor shell 501, and the shell pass inlet is arranged above the shell pass outlet in the vertical direction.

[0126] In each reaction zone 503, the number of the reaction tubes 502 is 1000. In this embodiment, as shown in Figure 3 and Figure 4 , the arrangement mode of the reaction tubes 502 includes triangular arrangement or rhombic arrangement.

[0127] The side wall of the reactor shell 501 is further provided with the catalyst loading port 508, and the catalyst loading port 508 is located in the non-reaction zone 504. The catalyst can be loaded into the reaction tube 502 through the catalyst loading port 508.

[0128] As shown in Figure 5 , in order to make the dehydrogenation raw material fully react in the reaction tube 502, the first baffle 5021 and the second baffle 5022 are arranged on the inner wall of the reaction tube 502. The first baffle 5021 and the second baffle 5022 are arranged in the vertical direction along the inner wall of the reaction tube, and from the cross section of the reaction tube 502 in the vertical direction, the first baffle 5021 can be arranged to have a part perpendicular to the inner wall of the reaction tube and a part parallel to the inner wall, and in addition, the second baffle 5022 can be arranged to have a part perpendicular to the inner wall of the reaction tube and a part intersecting with the inner wall on the extension line. In this way, the fluid can form a turbulent flow in the cavity of the reaction tube 502, so as to promote the reaction to occur fully.

[0129] As shown in Figure 6 , the gas distributor 507 includes a distribution plate, the shape of the distribution plate is circular, a plurality of air holes are arranged on the distribution plate, and the air holes are arranged in a ring shape around the center of the distribution plate.

[0130] In the present embodiment, the dehydrogenation reactor 5 is further provided with five temperature measuring instruments (not shown) respectively arranged at the tube side inlet and outlet of the dehydrogenation reactor 5 and the catalyst bed of the three reaction zones 503. Figure 2

[0131] In the present embodiment, the catalyst is a dehydrogenation catalyst commonly used in dehydrogenation technology.

[0132] As shown in the figure, the heat conducting medium circulating unit 6 comprises a heat conducting medium storage device 601, a heat conducting medium heating device 602, a heat conducting medium conveying pump 603, a second cooler 604 and a coupler 605. Figure 7

[0133] The coupler 605 is connected with a waste heat medium input pipeline, and the coupler 605 is connected with the heat conducting medium heating device 602; the heat conducting medium heating device 602 is connected with the heat conducting medium storage device 601 for heating the heat conducting medium; the heat conducting medium storage device 601 is provided with at least a heat conducting medium inlet and a heat conducting medium outlet, the heat conducting medium outlet of the heat conducting medium storage device 601 is connected with the shell side inlet of the dehydrogenation reactor 5 through a pipeline and the heat conducting medium conveying pump 603, and the shell side outlet of the dehydrogenation reactor 5 is connected with the heat conducting medium inlet of the heat conducting medium storage device 601 through a pipeline and the second cooler 604.

[0134] Specifically, since the dehydrogenation reactor 5 is a multi-stage isothermal dehydrogenation reactor, the shell side inlets of the reaction zones 503 can be converged into a total pipeline through branch pipelines and valves and then connected with the heat conducting medium outlet of the heat conducting medium storage device 601, and similarly, the shell side outlets of the reaction zones 503 can also be converged into a total pipeline through branch pipelines and valves and then connected with the heat conducting medium inlet of the heat conducting medium storage device 601.

[0135] In the present embodiment, the heat conducting medium is heat conducting oil.

[0136] In the present embodiment, the heat conducting medium heating device 602 is an electric heater, for example, a 34 MJ electric heater.

[0137] In the present embodiment, the coupler 605 is a small-sized heat storage type waste heat power generation device or a heat storage type waste heat conversion device. The waste heat can include waste heat generated by pyrolysis carbonization or incineration of one or a combination of sludge, garbage, hazardous waste, organic matter and organic solid waste. After the waste heat medium (generally flue gas) passes through the coupler 605, it is converted into electric energy and input into the heat conducting medium heating device 602, thereby heating the heat conducting medium.

[0138] ​​In the present embodiment, the heat conducting medium circulation unit 6 can further comprise a PLC control module (not shown) for monitoring and controlling the heating and circulation of the heat conducting medium. Figure 7

[0139] Embodiment 2

[0140] The present embodiment provides a dehydrogenation method, which is a method of dehydrogenation using the dehydrogenation system provided in Embodiment 1. In the present embodiment, the dehydrogenation raw material is methylcyclohexane (MCH), the dehydrogenation product is toluene, and the carrier gas is hydrogen. The method of the present embodiment can produce 10 tons of hydrogen per year.

[0141] The method comprises at least the following steps:

[0142] (1) The dehydrogenation raw material from the tank area is pumped into the dehydrogenation raw material buffer tank 1 for temporary storage, and the liquid level of the dehydrogenation raw material buffer tank 1 is maintained at 60-80%. 20-40 kg of dehydrogenation raw material is sent to the shell side of the vaporizer 2 for vaporization after passing through the metering pump. The flow rate of the metering pump can be adjusted and controlled by the main control frequency, or it can be adjusted manually on site. The temperature in the shell side of the vaporizer 2 is controlled at 110-200°C, the pressure is controlled at 0.05-3 MPaG, and the liquid level is controlled at 20-50%. The gas phase in the shell side of the vaporizer 2 enters the shell side of the superheater 3 for superheating, and then enters the mixer 4 to mix with 0.24 kg / h of preheated carrier gas. The carrier gas can come from the external area and the gas phase purification and storage device 10. The preheating temperature of the carrier gas is 200-400°C. After mixing, the material enters the tube side of the dehydrogenation reactor 5, where it undergoes dehydrogenation reaction under the action of the catalyst. The dehydrogenation raw material (methylcyclohexane) decomposes to form the dehydrogenation product (toluene) and hydrogen. This reaction is an endothermic reaction, and heat needs to be continuously supplied by the heat conducting medium to maintain the reaction and conversion rate. The heavy components accumulated in the shell side of the vaporizer 2 are periodically discharged into the heavy component collection tank 7;

[0143] (2) The heat conducting medium from the heat conducting medium circulation unit 6 enters the shell side of the dehydrogenation reactor 5 to provide heat for the dehydrogenation reaction. The heated heat conducting medium flows out of the shell side of the dehydrogenation reactor 5 and enters the heat conducting medium circulation unit 6, which circulates and provides heat for the dehydrogenation reactor 5;

[0144] ​(3) The material after dehydrogenation reaction flows out from the tube side of the dehydrogenation reactor 5, enters the tube side of the superheater 3 to provide heat for superheating the dehydrogenation raw material, and controls the temperature of the superheated dehydrogenation raw material at 300-400℃, and then enters the tube side of the vaporizer 2 to provide heat for vaporizing the dehydrogenation raw material. The flow of the material after dehydrogenation reaction of the dehydrogenation reactor 5 can be adjusted by the pressure regulating valve of the dehydrogenation reactor 5 to ensure that the vaporization amount of the dehydrogenation raw material of the vaporizer 2 is 22 kg / h, so that the dehydrogenation raw material after heating is cooled to 40℃ by the first cooler 13, and then enters the separator 8 for gas-liquid separation to obtain dehydrogenation products and hydrogen. The obtained hydrogen enters the gas phase purification and storage device 10 for purification, and the purity of the purified hydrogen is more than 99%, and part of the hydrogen obtained after purification by the gas phase purification and storage device 10 is preheated and then enters the mixer 4 to reuse the carrier gas, and the other part of the hydrogen can be transported to the boundary area to complete the storage and transportation of hydrogen. The obtained dehydrogenation products enter the liquid phase storage device 9, and the gas phase components in the liquid phase storage device 9 are discharged to the gas phase purification and storage device 10 through the pressure regulating valve. The purity of the dehydrogenation products is more than 97%, and the dehydrogenation products can be transported to the corresponding product tank area.

[0145] The temperature of the dehydrogenation reaction is 300-400℃, and the pressure of the dehydrogenation reaction is 0.5-1.5 barG, preferably 0.2-1.0 barG.

[0146] Specifically, in the dehydrogenation reactor 5, the number of the multi-stage reaction zones 503 is 3, and the upper to lower three-stage reaction zones 503 are respectively the first-stage reaction zone, the second-stage reaction zone and the third-stage reaction zone. The temperature of the heat conducting medium entering the shell side of the first-stage reaction zone is 380-400℃, the temperature of the heat conducting medium entering the shell side of the second-stage reaction zone is 370-380℃, and the temperature of the heat conducting medium entering the shell side of the third-stage reaction zone is 350-370℃. The reaction temperature of each stage reaction zone 503 of the dehydrogenation reactor 5 is controlled by the heat conducting medium, and the reaction pressure is controlled by the pressure regulating valve of the dehydrogenation reactor 5.

[0147] In the embodiment, step (2) specifically comprises: 450 kg of heat-conducting medium, which is heat-conducting oil, enters the heat-conducting medium storage device 601, the heat-conducting oil is boiled and degassed in the heat-conducting medium storage device 601, a heat source (in the embodiment, the heat source is electricity) of the heat-conducting medium heating device 602 is used to heat the heat-conducting medium, so that the heat-conducting medium is slowly heated to 380-450°C, the heat-conducting medium heating device 602 is a waste heat generated by pyrolysis carbonization or incineration of one or a combination of sludge, garbage, hazardous waste, organic matter, organic solid waste, etc., which enters the coupler 605 and is converted into electric energy as a heat source, then the heat-conducting medium carrying heat enters the shell side of the dehydrogenation reactor 5 through the heat-conducting medium conveying pump 603 to provide heat for the dehydrogenation reaction, the temperature of the heat-conducting medium entering the third reaction zone 503 can be adjusted to be in the above range through the adjusting valve arranged on the pipeline, the heat-conducting medium after heating flows out from the shell side of the dehydrogenation reactor 5, and the temperature of the heat-conducting medium after heating is reduced by about 10°C compared with the temperature of the heat-conducting medium entering the shell side of the dehydrogenation reactor 5, the heat-conducting medium after heating enters the second cooler 604 for cooling, and then reenters the heat-conducting medium storage device 601 to be circulated and heated for the dehydrogenation reactor 5 through the heat-conducting medium circulating unit 6. Step (2) further comprises: monitoring and controlling the heating and circulation process of the heat-conducting medium by using the PLC control module.

[0148] Embodiment 3

[0149] The embodiment provides a dehydrogenation system, which has basically the same structure as the dehydrogenation system provided in Embodiment 1, and the difference lies in that, in each reaction zone 503, the number of the reaction tubes 502 is 800.

[0150] In the embodiment, the coupler 605 is a regenerative waste heat power generation device. The waste heat is sludge pyrolysis carbonization waste heat, and the waste heat medium is flue gas with a ring gap outlet temperature of 650°C from a sludge pyrolysis carbonization plant (or device). In the embodiment, the waste heat of the plant is coupled to serve as the heat source of the heat-conducting medium heating device 602, so that the waste heat medium enters the coupler 605 and is converted into electric energy, and then is input into the heat-conducting medium heating device 602 to heat the heat-conducting medium.

[0151] Embodiment 4

[0152] The embodiment provides a dehydrogenation method, which is a method for dehydrogenation by using the dehydrogenation system provided in Embodiment 3. In the embodiment, the dehydrogenation raw material is methylcyclohexane (MCH), the dehydrogenation product is toluene, and the carrier gas is hydrogen. The method in the embodiment can produce 200 tons of hydrogen per year.

[0153] The method at least comprises the following steps:

[0154] (1) The dehydrogenation raw material from the tank area is pumped into the dehydrogenation raw material buffer tank 1 for temporary storage, and the liquid level of the dehydrogenation raw material buffer tank 1 is maintained at 60-80%. 500 kg of dehydrogenation raw material is sent to the shell side of the vaporizer 2 after passing through the metering pump to be vaporized. The flow rate of the metering pump can be adjusted and controlled by the main control frequency, or it can be adjusted manually on site. The temperature in the shell side of the vaporizer 2 is controlled at 110-200°C, the pressure is controlled at 0.05-3 MPaG, and the liquid level is controlled at 20-50%. The gas phase in the shell side of the vaporizer 2 enters the shell side of the superheater 3 to be superheated, and then enters the mixer 4 to be mixed with 4 kg / h of preheated carrier gas. The carrier gas can come from the external area and the gas phase purification and storage device 10. The preheating temperature of the carrier gas is 200-400°C. After mixing, the material enters the tube side of the dehydrogenation reactor 5, where it undergoes dehydrogenation reaction under the action of the catalyst. The dehydrogenation raw material (methylcyclohexane) decomposes to form dehydrogenation product (toluene) and hydrogen. This reaction is an endothermic reaction, and heat needs to be continuously supplied through a heat transfer medium to maintain the reaction and conversion rate. The heavy components accumulated in the shell side of the vaporizer 2 are periodically discharged into the heavy component collection tank 7.

[0155] (2) The heat transfer medium from the heat transfer medium circulation unit 6 enters the shell side of the dehydrogenation reactor 5 to provide heat for the dehydrogenation reaction. The heated heat transfer medium flows out of the shell side of the dehydrogenation reactor 5 and enters the heat transfer medium circulation unit 6, which circulates and provides heat for the dehydrogenation reactor 5.

[0156] (3) The material after dehydrogenation reaction flows out of the tube side of the dehydrogenation reactor 5, enters the tube side of the superheater 3 to provide heat for the superheating of the dehydrogenation raw material, and controls the temperature of the superheated dehydrogenation raw material at 300-400°C. Then it enters the tube side of the vaporizer 2 to provide heat for the vaporization of the dehydrogenation raw material. The flow rate of the material after dehydrogenation reaction in the dehydrogenation reactor 5 can be adjusted by the pressure regulating valve to ensure that the vaporization amount of the dehydrogenation raw material in the vaporizer 2 is 450 kg / h. After the heated material after dehydrogenation reaction is cooled to 40°C by the first cooler 13, it enters the separator 8 for gas-liquid separation to obtain dehydrogenation product and hydrogen. The obtained hydrogen enters the gas phase purification and storage device 10 for purification, and the purity of the purified hydrogen is more than 99%. Part of the hydrogen obtained after purification in the gas phase purification and storage device 10 is preheated and enters the mixer 4 as carrier gas, thereby recycling the carrier gas. The other part of the hydrogen can be transported to the external area to complete the storage and transportation of hydrogen. The obtained dehydrogenation product enters the liquid phase storage device 9, and the gas phase components in the liquid phase storage device 9 are discharged into the gas phase purification and storage device 10 through a pressure regulating valve. The purity of the dehydrogenation product is more than 97%, and the dehydrogenation product can be transported to the corresponding finished product tank area.

[0157] The temperature of the dehydrogenation reaction is 300℃-400℃, and the pressure of the dehydrogenation reaction is 0.5-1.5 barG, preferably 0.2-1.0 barG.

[0158] Specifically, in the dehydrogenation reactor 5, the multi-stage reaction zone 503 has three stages, namely, stage I, stage II, and stage III, from top to bottom. The temperature of the heat-conducting medium entering the shell side of stage I is 380℃-400℃, the temperature of the heat-conducting medium entering the shell side of stage II is 370℃-380℃, and the temperature of the heat-conducting medium entering the shell side of stage III is 350℃-370℃. The reaction temperature of each stage of the dehydrogenation reactor 5 is controlled by the heat-conducting medium, and the reaction pressure is controlled by the pressure regulating valve built into the dehydrogenation reactor 5.

[0159] In this embodiment, step (2) specifically includes: introducing a heat-conducting medium into a heat-conducting medium storage device 601, wherein the heat-conducting medium is heat-conducting oil; in the heat-conducting medium storage device 601, boiling and venting the heat-conducting oil; and using a heat source (in this embodiment, the heat source is electricity) of a heat-conducting medium heating device 602 to heat the heat-conducting medium, causing it to slowly rise to 380-450°C. The heat-conducting medium heating device 602 uses flue gas with an annular outlet temperature of 650°C from a sludge pyrolysis carbonization plant (or device) as a waste heat medium, which enters the coupler 605 and is converted into electrical energy to serve as a heat source. Then, the heat-carrying heat transfer medium is introduced into the shell side of the dehydrogenation reactor 5 by the heat transfer medium transfer pump 603 to heat the dehydrogenation reaction. The temperature of the heat transfer medium entering the three-stage reaction zone 503 can be adjusted within the above range by the regulating valve installed on the pipeline. After being heated, the heat transfer medium flows out from the shell side of the dehydrogenation reactor 5, and its temperature is about 10°C lower than that of the heat transfer medium entering the shell side of the dehydrogenation reactor 5. After being heated, the heat transfer medium enters the second cooler 604 for cooling, and then re-enters the heat transfer medium storage device 601. The heat transfer medium circulation unit 6 circulates heat to the dehydrogenation reactor 5. Step (2) further includes: using a PLC control module to monitor and control the heating and circulation process of the heat transfer medium.

Claims

1. A dehydrogenation system comprising at least: Vaporizer, superheater, mixer, dehydrogenation reactor, heat transfer medium circulation unit, and separator, characterized in that: The vaporizer is provided with a shell-side inlet, a first shell-side outlet, a first tube-side inlet, and a first tube-side outlet; The superheater is provided with a shell-side inlet, a shell-side outlet, a first tube-side inlet, and a first tube-side outlet; The mixer is equipped with a dehydrogenation feedstock inlet, a carrier gas inlet, and a mixed material outlet. The dehydrogenation reactor is provided with a tube-side inlet at the top and a tube-side outlet at the bottom, and a shell-side inlet and a shell-side outlet on the side wall of the dehydrogenation reactor. The separator is provided with a material inlet, a gas phase outlet, and a liquid phase outlet; The shell-side inlet of the vaporizer is connected to a dehydrogenation feedstock pipeline. The first shell-side outlet of the vaporizer is connected to the shell-side inlet of the superheater via a pipeline. The shell-side outlet of the superheater is connected to the dehydrogenation feedstock inlet of the mixer via a pipeline. The carrier gas inlet of the mixer is connected to a carrier gas pipeline. The mixed material outlet of the mixer is connected to the tube-side inlet at the top of the dehydrogenation reactor via a pipeline. The tube-side outlet at the bottom of the dehydrogenation reactor is connected to the first tube-side inlet of the superheater via a pipeline. The first tube-side outlet of the superheater is connected to the first tube-side inlet of the vaporizer via a pipeline. The first tube-side outlet of the vaporizer is connected to the material inlet of the separator via a pipeline. A catalyst bed is provided in the tube side of the dehydrogenation reactor; The shell-side inlet and shell-side outlet of the dehydrogenation reactor are connected to the heat transfer medium circulation unit for circulating heat to the dehydrogenation reactor using the heat transfer medium.

2. The dehydrogenation system according to claim 1, characterized in that, The dehydrogenation system further includes a dehydrogenation feed buffer tank, which is connected to the dehydrogenation feed delivery pipeline, and a metering pump is installed on the dehydrogenation feed delivery pipeline.

3. The dehydrogenation system according to claim 2, characterized in that, A booster pump is further installed on the dehydrogenation feedstock delivery pipeline.

4. The dehydrogenation system according to claim 1, characterized in that, The dehydrogenation system further includes a vaporizer temperature control line. One end of the vaporizer temperature control line is connected to a line that connects the outlet of the first tube side of the superheater to the inlet of the first tube side of the vaporizer. The other end of the vaporizer temperature control line is connected to a line that connects the outlet of the first tube side of the vaporizer to the material inlet of the separator. This line is used to adjust the amount of material after the dehydrogenation reaction entering the tube side of the vaporizer, thereby adjusting the temperature at which the vaporizer vaporizes the dehydrogenation feedstock.

5. The dehydrogenation system according to claim 1, characterized in that, The dehydrogenation system further includes a first cooler, and the first tube outlet of the vaporizer is connected to the material inlet of the separator via a pipeline and the first cooler.

6. The dehydrogenation system according to claim 1, characterized in that, The superheater further includes a second tube inlet and a second tube outlet, used to allow other heat-conducting media to enter the superheater as a heat source to heat the superheated dehydrogenation feedstock.

7. The dehydrogenation system according to claim 6, characterized in that, The vaporizer further includes a second tube inlet and a second tube outlet for allowing other heat-conducting media to enter the vaporizer as a heat source to heat the vaporization of the dehydrogenation feedstock.

8. The dehydrogenation system according to claim 7, characterized in that, The second tube inlet of the vaporizer is connected to the second tube outlet of the superheater via a pipeline.

9. The dehydrogenation system according to claim 6 or 7, characterized in that, The other heat transfer media include one or a combination of heat transfer oil, molten salt, and superheated medium-pressure steam.

10. The dehydrogenation system according to claim 1, characterized in that, The vaporizer further includes a second shell-side outlet connected to a heavy component discharge line.

11. The dehydrogenation system according to claim 10, characterized in that, The dehydrogenation system further includes a heavy component collection tank connected to the heavy component discharge pipeline for collecting heavy components contained in the dehydrogenation feedstock.

12. The dehydrogenation system according to claim 1, characterized in that, A preheater is installed on the carrier gas delivery pipeline to preheat the carrier gas.

13. The dehydrogenation system according to claim 1, characterized in that, The mixer includes a static mixer.

14. The dehydrogenation system according to claim 1, characterized in that, The dehydrogenation reactor includes a multi-stage isothermal dehydrogenation reactor.

15. The dehydrogenation system according to claim 1, characterized in that, The dehydrogenation reactor includes: a reactor shell, a reaction tube, a tube-side inlet at the top of the reactor shell and a tube-side outlet at the bottom of the reactor shell, and a shell-side inlet and a shell-side outlet on the side wall of the reactor shell. The reactor shell includes multiple reaction zones and at least one non-reaction zone, wherein the non-reaction zone separates the multiple reaction zones. The reaction tube is disposed in multiple reaction zones within the reactor shell; each reaction zone has an upper tube sheet above the reaction tube and a lower tube sheet below it for supporting and fixing the reaction tube; a gas distributor is disposed above the upper tube sheet of each reaction zone; a catalyst bed is disposed inside the reaction tube; the tube inlet at the top of the reactor shell and the tube outlet at the bottom are connected to the reaction tube; Within the multiple reaction zones, the area between the reaction tube and the reactor shell is the shell side, and each reaction zone has at least one shell side inlet and at least one shell side outlet on the reactor shell sidewall.

16. The dehydrogenation system according to claim 15, characterized in that, In the dehydrogenation reactor, the number of stages in the multi-stage reaction zone is two or more.

17. The dehydrogenation system according to claim 16, characterized in that, The number of segments in the multi-segment reaction zone is 3-5.

18. The dehydrogenation system according to claim 15, characterized in that, In the dehydrogenation reactor, the number of reaction tubes in each reaction zone is 1-1000.

19. The dehydrogenation system according to claim 15, characterized in that, In the dehydrogenation reactor, the reaction tubes are arranged in a triangular, square, or rhomboid pattern.

20. The dehydrogenation system according to claim 15, characterized in that, In the dehydrogenation reactor, the inner wall of the reaction tube is provided with several baffles to create turbulence in the fluid within the cavity of the reaction tube, thereby promoting a full reaction.

21. The dehydrogenation system according to claim 20, characterized in that, The baffle includes a plurality of first baffles and a plurality of second baffles. Viewed from a cross-section of the reaction tube in the vertical direction, the first baffles are configured to have a portion perpendicular to the inner wall of the reaction tube and a portion parallel to the inner wall. The second baffles are configured to have a portion perpendicular to the inner wall of the reaction tube and a portion intersecting the inner wall on an extended line.

22. The dehydrogenation system according to claim 15, characterized in that, In the dehydrogenation reactor, the side wall of the reactor shell is further provided with a catalyst loading port, and the catalyst loading port is located in the non-reaction zone.

23. The dehydrogenation system according to claim 15, characterized in that, In the dehydrogenation reactor, the gas distributor includes a distribution plate with multiple vent holes arranged in a ring around the center of the distribution plate.

24. The dehydrogenation system according to claim 15, characterized in that, The dehydrogenation reactor is further equipped with several temperature measuring instruments.

25. The dehydrogenation system according to claim 24, characterized in that, The number of temperature measuring instruments is two, respectively installed at the tube inlet and tube outlet of the dehydrogenation reactor; or the number of temperature measuring instruments is three or more, respectively installed at the tube inlet and tube outlet of the dehydrogenation reactor and in the catalyst bed of each reaction zone.

26. The dehydrogenation system according to claim 1, characterized in that, The heat transfer medium circulation unit includes at least a heat transfer medium storage device, a heat transfer medium heating device, and a heat transfer medium delivery pump; The heat transfer medium heating device is connected to the heat transfer medium storage device and is used to heat the heat transfer medium; The heat transfer medium storage device is provided with at least a heat transfer medium inlet and a heat transfer medium outlet. The heat transfer medium outlet of the heat transfer medium storage device is connected to the shell-side inlet of the dehydrogenation reactor via a pipeline and the heat transfer medium delivery pump. The shell-side outlet of the dehydrogenation reactor is connected to the heat transfer medium inlet of the heat transfer medium storage device via a pipeline.

27. The dehydrogenation system according to claim 26, characterized in that, The heat transfer medium circulation unit further includes a second cooler, and the shell-side outlet of the dehydrogenation reactor is connected to the inlet of the heat transfer medium storage device via a pipeline and the second cooler.

28. The dehydrogenation system according to claim 1, characterized in that, The heat transfer medium includes one or a combination of heat transfer oil, molten salt, and superheated medium-pressure steam.

29. The dehydrogenation system according to claim 26, characterized in that, The heat transfer medium heating device includes one or a combination of several of the following: electric heater, combustion furnace, and heat exchanger.

30. The dehydrogenation system according to claim 26, characterized in that, The heat source of the heat transfer medium heating device includes one or a combination of fuel, waste heat and electricity.

31. The dehydrogenation system according to claim 30, characterized in that, The fuel includes one or a combination of natural gas, coal, heavy oil, and low-calorific-value fuel gas.

32. The dehydrogenation system according to claim 31, characterized in that, The heavy oil in the fuel includes heavy components from the heavy component collection tank.

33. The dehydrogenation system according to claim 30, characterized in that, The waste heat includes waste heat from the factory.

34. The dehydrogenation system according to claim 33, characterized in that, The waste heat includes waste heat generated during pyrolysis, carbonization, or incineration at the factory.

35. The dehydrogenation system according to claim 34, characterized in that, The waste heat includes waste heat generated from the pyrolysis, carbonization, or incineration of one or more of the following: sludge, garbage, hazardous waste, organic matter, and organic solid waste.

36. The dehydrogenation system according to claim 30, characterized in that, When the heat source of the heat-conducting medium heating device includes waste heat and / or electricity, the heat-conducting medium circulation unit further includes a coupler connected to a waste heat medium input pipeline, and the coupler is connected to the heat-conducting medium heating device.

37. The dehydrogenation system according to claim 36, characterized in that, The coupler includes a thermal storage waste heat power generation device and / or a thermal storage waste heat conversion device.

38. The dehydrogenation system according to claim 26, characterized in that, The heat transfer medium circulation unit further includes a PLC control module for monitoring and controlling the heating and circulation process of the heat transfer medium.

39. The dehydrogenation system according to claim 1, characterized in that, The dehydrogenation system further includes a liquid phase storage device connected to the liquid phase outlet of the separator via a pipeline.

40. The dehydrogenation system according to claim 39, characterized in that, The dehydrogenation system further includes a gas phase purification and storage device, which is connected to the gas phase outlet of the separator via a pipeline.

41. The dehydrogenation system according to claim 40, characterized in that, The liquid phase storage device is connected to the gas phase purification and storage device via a pipeline, and is used to discharge the gas phase components entering the liquid phase storage device to the gas phase purification and storage device.

42. The dehydrogenation system according to claim 40, characterized in that, The gas phase purification and storage device is connected to the carrier gas delivery pipeline and is used to reuse the carrier gas.

43. A dehydrogenation method, characterized in that, The method is a dehydrogenation process using the dehydrogenation system according to any one of claims 1-42, the method comprising at least the following steps: (1) After the dehydrogenation feedstock enters the shell side of the vaporizer for vaporization, it enters the shell side of the superheater for superheating, and then enters the mixer to mix with the carrier gas. After mixing, the material enters the tube side of the dehydrogenation reactor and undergoes dehydrogenation reaction under the action of the catalyst. (2) The heat transfer medium from the heat transfer medium circulation unit enters the shell side of the dehydrogenation reactor to provide heat for the dehydrogenation reaction. After being heated, the heat transfer medium flows out from the shell side of the dehydrogenation reactor and enters the heat transfer medium circulation unit to provide circulating heat for the dehydrogenation reactor. (3) The material after the dehydrogenation reaction flows out from the tube side of the dehydrogenation reactor and enters the tube side of the superheater to provide heat for the superheating of the dehydrogenation feedstock. Then it enters the tube side of the vaporizer to provide heat for the vaporization of the dehydrogenation feedstock. After the material after the dehydrogenation reaction is heated, it enters the separator for gas-liquid separation to obtain dehydrogenation products and hydrogen.

44. The dehydrogenation method according to claim 43, characterized in that, The dehydrogenation feedstock includes methylcyclohexane, and the dehydrogenation product includes toluene.

45. The dehydrogenation method according to claim 43, characterized in that, The dehydrogenation method further includes the following steps: the dehydrogenation feedstock first enters the dehydrogenation feedstock buffer tank, and after being metered and selectively pressurized, it enters the shell side of the vaporizer for vaporization.

46. ​​The dehydrogenation method according to claim 43, characterized in that, The carrier gas includes hydrogen.

47. The dehydrogenation method according to claim 43, characterized in that, The dehydrogenation method further includes the following steps: preheating the carrier gas before it enters the mixer; the preheating temperature of the carrier gas is 200℃-400℃.

48. The dehydrogenation method according to claim 43, characterized in that, The mass ratio of the carrier gas to the dehydrogenation feedstock is 0.3-0.

5.

49. The dehydrogenation method according to claim 43, characterized in that, The dehydrogenation reaction is carried out at a temperature of 300℃-400℃ and at a pressure of 0.5-1.5 barG.

50. The dehydrogenation method according to claim 49, characterized in that, The pressure of the dehydrogenation reaction is 0.2-1.0 barG.

51. The dehydrogenation method according to claim 43, characterized in that, A portion of the dehydrogenated material flowing out of the tube side of the superheater enters the tube side of the vaporizer to provide heat for the vaporization of the dehydrogenated feedstock, while another portion of the dehydrogenated material flowing out of the tube side of the superheater enters the separator for gas-liquid separation.

52. The dehydrogenation method according to claim 43, characterized in that, The temperature inside the shell side of the vaporizer is controlled at 110℃-200℃, and the pressure of the vaporizer is controlled at 0.05-3MPaG.

53. The dehydrogenation method according to claim 43, characterized in that, The dehydrogenation method further includes the following steps: the material after the dehydrogenation reaction after heating is cooled by a first cooler and then enters the separator for gas-liquid separation.

54. The dehydrogenation method according to claim 43, characterized in that, The dehydrogenation method further includes the following steps: introducing other heat-conducting media into the superheater as a heat source to heat the superheated dehydrogenation feedstock.

55. The dehydrogenation method according to claim 43, characterized in that, The dehydrogenation method further includes the following steps: introducing other heat-conducting media into the vaporizer as a heat source to heat the vaporization of the dehydrogenation feedstock.

56. The dehydrogenation method according to claim 43, characterized in that, The dehydrogenation method further includes the following steps: introducing other heat-conducting media into the superheater as a heat source to heat the superheated dehydrogenation feedstock, and then introducing the heated other media into the vaporizer as a heat source to heat the vaporization of the dehydrogenation feedstock.

57. The dehydrogenation method according to any one of claims 54, 55 and 56, characterized in that, The other heat transfer media include one or a combination of heat transfer oil, molten salt, and superheated medium-pressure steam.

58. The dehydrogenation method according to claim 43, characterized in that, The dehydrogenation method further includes the following steps: periodically discharging heavy components from the vaporizer shell side into a heavy component collection tank.

59. The dehydrogenation method according to claim 43, characterized in that, The temperature of the heat transfer medium entering the shell side of the dehydrogenation reactor is 300℃-400℃.

60. The dehydrogenation method according to claim 59, characterized in that, The temperature of the heat transfer medium entering the shell side of the dehydrogenation reactor is 350-400°C. o C.

61. The dehydrogenation method according to claim 43, characterized in that, In the dehydrogenation reactor, there are three reaction zones, from top to bottom: Reaction Zone I, Reaction Zone II, and Reaction Zone III. The temperature of the heat transfer medium entering the shell side of Reaction Zone I is 380℃-400℃, the temperature of the heat transfer medium entering the shell side of Reaction Zone II is 370℃-380℃, and the temperature of the heat transfer medium entering the shell side of Reaction Zone III is 350℃-370℃.

62. The dehydrogenation method according to claim 43, characterized in that, In the dehydrogenation reactor, there are 5 multi-stage reaction zones, which are designated as Reaction Zone I, Reaction Zone II, Reaction Zone III, Reaction Zone IV, and Reaction Zone V from top to bottom. The temperature of the heat transfer medium entering the shell side of Reaction Zone I is 390℃-400℃, the temperature of the heat transfer medium entering the shell side of Reaction Zone II is 380℃-390℃, the temperature of the heat transfer medium entering the shell side of Reaction Zone III is 370℃-380℃, the temperature of the heat transfer medium entering the shell side of Reaction Zone IV is 360℃-370℃, and the temperature of the heat transfer medium entering the shell side of Reaction Zone V is 350℃-360℃.

63. The dehydrogenation method according to claim 43, characterized in that, Step (2) specifically includes: allowing the heat transfer medium to enter the heat transfer medium storage device, using the heat source of the heat transfer medium heating device to heat the heat transfer medium, and then using the heat transfer medium transfer pump to allow the heat-carrying heat transfer medium to enter the shell side of the dehydrogenation reactor to provide heat for the dehydrogenation reaction. After being heated, the heat transfer medium flows out from the shell side of the dehydrogenation reactor and re-enters the heat transfer medium storage device, and circulates heat to the dehydrogenation reactor through the heat transfer medium circulation unit.

64. The dehydrogenation method according to claim 63, characterized in that, The heat source of the heat-conducting medium is used to heat the heat-conducting medium to 350-450°C.

65. The dehydrogenation method according to claim 64, characterized in that, The heat source of the heat-conducting medium heating device heats the heat-conducting medium to 380-450℃.

66. The dehydrogenation method according to claim 63, characterized in that, Step (2) further includes: after the heat transfer medium flows out of the shell side of the dehydrogenation reactor, it first enters the second cooler for cooling, and then re-enters the heat transfer medium storage device.

67. The dehydrogenation method according to claim 63, characterized in that, The heat transfer medium includes one or a combination of heat transfer oil, molten salt, and superheated medium-pressure steam.

68. The dehydrogenation method according to claim 67, characterized in that, When the heat transfer medium is heat transfer oil, step (2) further includes: boiling the heat transfer oil and venting it in the heat transfer medium storage device.

69. The dehydrogenation method according to claim 63, characterized in that, The heat source of the heat transfer medium heating device includes one or a combination of fuel, waste heat and electricity.

70. The dehydrogenation method according to claim 69, characterized in that, When the heat source of the heat-conducting medium heating device includes waste heat and / or electricity, step (2) further includes: allowing the waste heat medium to enter the coupler and then use it as the heat source of the heat-conducting medium heating device to heat the heat-conducting medium.

71. The dehydrogenation method according to claim 63, characterized in that, Step (2) further includes: using a PLC control module to monitor and control the heating and circulation process of the heat transfer medium.

72. The dehydrogenation method according to claim 43, characterized in that, The dehydrogenation method further includes the following steps: purifying the obtained hydrogen gas by introducing it into a gas phase purification and storage device, wherein the purity of the purified hydrogen gas is above 99%.

73. The dehydrogenation method according to claim 43, characterized in that, The dehydrogenation method further includes the following steps: introducing the obtained dehydrogenation product into a liquid phase storage device, and selectively discharging the gas phase components in the liquid phase storage device to a gas phase purification and storage device; the purity of the dehydrogenation product is above 97%.

74. The dehydrogenation method according to claim 72, characterized in that, The dehydrogenation method further includes the following steps: allowing hydrogen obtained after purification by a gas phase purification and storage device to enter a mixer, thereby reusing the hydrogen as a carrier gas.

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