A methanol synthesis and hydrogen reforming hydrogenation system

Abstract

The application discloses a methanol synthesis and hydrogen reforming hydrogenation system, which comprises a hydrogen input branch, a carbon dioxide input branch, a methanol synthesis device, a methanol output branch, a methanol storage tank, a methanol reforming reactor, a methanol input branch, a water vapor input branch, a methanol hydrogen separation branch, a waste heat recovery branch, a hydrogenation machine, a hydrogenation branch and a co-production unit. Based on the hydrogen carrier and energy carrier of methanol, by scientifically and reasonably coupling process links such as methanol synthesis, methanol evaporation, methanol reforming, methanol separation, hydrogenation and methanol combustion, comprehensive and efficient supply of multiple energy forms of hydrogen, electricity, heat and cold can be realized, and therefore, efficient utilization of methanol energy is realized.

Description

Technical Field

[0001] This application relates to the field of methanol energy utilization technology, and in particular to a methanol synthesis and reforming hydrogen production and hydrogenation system. Background Technology

[0002] Hydrogen energy has attracted significant attention due to its potential for decarbonization in heavy industry and heavy-duty transportation sectors that are difficult to electrify, as well as its ability to facilitate the large-scale integration of renewable energy sources such as wind and solar power. Currently, refueling hydrogen fuel cell vehicles at hydrogen refueling stations is the most common application of hydrogen energy. However, the low volumetric energy density of hydrogen and high storage and transportation costs are the main bottlenecks to its development.

[0003] Methanol is abundant and inexpensive, and its liquid nature at room temperature and pressure makes it easy to store and transport. Compared to other hydrogen production methods, such as industrial hydrogen production, methanol-based hydrogen production has lower energy consumption and cost. Methanol holds great potential as a means to overcome the bottlenecks in hydrogen energy development. Summary of the Invention

[0004] This application provides a methanol synthesis and reforming hydrogen production and hydrogenation system, which improves the utilization efficiency of methanol energy by scientifically and rationally coupling methanol synthesis, methanol evaporation, methanol reforming, methanol separation, hydrogenation, and methanol combustion processes.

[0005] The methanol synthesis and reforming hydrogen production and hydrogenation system includes: a hydrogen input branch, a carbon dioxide input branch, a methanol synthesis unit, a methanol output branch, a methanol storage tank, a methanol reforming reactor, a methanol input branch, a steam input branch, a methanol-hydrogen separation branch, a waste heat recovery branch, a hydrogenator, a hydrogenation branch, and a co-production unit. The methanol synthesis unit utilizes hydrogen input from the hydrogen input branch and carbon dioxide input from the carbon dioxide input branch to synthesize methanol, and outputs the synthesized methanol from the methanol output branch. The methanol storage tank is connected to the methanol output branch, and the methanol storage tank is connected to the methanol inlet of the methanol reforming reactor via the methanol input branch. The steam input branch is connected to the steam inlet of the methanol reforming reactor. The input end of the methanol-hydrogen separation branch... The methanol reforming reactor's product outlet is connected to the methanol-hydrogen separation branch's carbon dioxide outlet, which is connected to the carbon dioxide input branch. The methanol-hydrogen separation branch's hydrogen outlet outputs hydrogen. The methanol reforming reactor's tail gas outlet is connected to the waste heat recovery branch, which transfers heat from the methanol reforming reactor's tail gas to the steam input branch and the methanol input branch. The hydrogen inlet of the hydrogenation branch is connected to the hydrogen outlet of the methanol-hydrogen separation branch, and the hydrogen outlet of the hydrogenation branch is connected to the hydrogen dispenser, which is used to fill hydrogen fuel cell vehicles with hydrogen. The co-production unit is connected to the methanol storage tank, used to obtain methanol from the methanol storage tank, and to produce at least one of electrical energy, thermal energy, and cold energy through the heat generated from burning methanol.

[0006] In some embodiments, the methanol input branch includes a methanol evaporator and a fuel mixing tank, the waste heat recovery branch includes a methanol preheater, the methanol preheater includes a first cold fluid channel and a first hot fluid channel, wherein the methanol inlet of the methanol evaporator is connected to the methanol storage tank, the methanol outlet of the methanol evaporator is connected to the inlet of the first cold fluid channel and the methanol inlet of the fuel mixing tank, the outlet of the first cold fluid channel is connected to the methanol inlet of the methanol reforming reactor, the first hot fluid channel is connected to the tail gas outlet of the methanol reforming reactor, the hydrogen outlet of the methanol-hydrogen separation branch is connected to the hydrogen inlet of the fuel mixing tank and the hydrogenation branch, and the fuel outlet of the fuel mixing tank is connected to the fuel inlet of the methanol reforming reactor.

[0007] In some embodiments, a heat exchange medium channel is provided between the methanol evaporator and the hydrogenator, the heat exchange medium channel being able to transfer the heat from the hydrogenator to the methanol evaporator through the heat exchange medium, so that the methanol evaporator can carry out the methanol evaporation process.

[0008] In some embodiments, the methanol-hydrogen separation branch includes a methanol separation and recovery device and a first separator. The inlet of the methanol separation and recovery device is the input end of the methanol-hydrogen separation branch. The non-methanol outlet of the methanol separation and recovery device is connected to the inlet of the first separator. The methanol outlet of the methanol separation and recovery device is connected to the methanol inlet of the methanol reforming reactor via a check valve. The first outlet of the first separator is the carbon dioxide outlet of the methanol-hydrogen separation branch, and the second outlet of the first separator is the hydrogen outlet of the methanol-hydrogen separation branch.

[0009] In some embodiments, when the cogeneration unit produces electricity, heat, and cold energy, the methanol separation and recovery equipment and the first separator operate using the electricity, heat, and cold energy obtained from the cogeneration unit.

[0010] In some embodiments, the waste heat recovery branch further includes a superheater, a vaporizer, and a steam preheater. The superheater includes a second cold fluid channel and a second hot fluid channel. The vaporizer includes a third cold fluid channel and a third hot fluid channel. The steam preheater includes a fourth cold fluid channel and a fourth hot fluid channel. The tail gas outlet of the methanol reforming reactor is connected to the fourth hot fluid channel in sequence via the second hot fluid channel, the first hot fluid channel, and the third hot fluid channel. The steam input branch is connected to the steam inlet of the methanol reforming reactor via the fourth cold fluid channel. The condensate outlet of the co-production unit is connected to the inlet of the third cold fluid channel. The outlet of the third cold fluid channel is connected to the inlet of the second cold fluid channel. The outlet of the second cold fluid channel of the superheater is connected to the superheated steam inlet of the co-production unit.

[0011] In some embodiments, the hydrogen refueling branch includes a hydrogen storage unit and a first compressor, the inlet of the first compressor being the hydrogen inlet of the hydrogen refueling branch, the outlet of the first compressor being connected to the inlet of the hydrogen storage unit, and the outlet of the hydrogen storage unit being the hydrogen outlet of the hydrogen refueling branch.

[0012] In some embodiments, when the cogeneration unit produces electricity, the hydrogen refueling machine and the first compressor operate using the electricity obtained from the cogeneration unit.

[0013] In some embodiments, the methanol synthesis equipment includes a synthesis reactor, a methanol separator, and a second separator. The methanol output branch includes a distillation column. The hydrogen inlet of the synthesis reactor is connected to the hydrogen input branch and the hydrogen outlet of the second separator. The carbon dioxide inlet of the synthesis reactor is connected to the carbon dioxide input branch and the carbon dioxide outlet of the second separator. The product outlet of the synthesis reactor is connected to the inlet of the methanol separator. The methanol outlet of the methanol separator is connected to the inlet of the distillation column. The non-methanol outlet of the methanol separator is connected to the inlet of the second separator. The outlet of the distillation column is connected to the methanol storage tank.

[0014] In some embodiments, the hydrogen input branch includes a new energy power generation system, an electric hydrogen production cluster, and a second compressor; the carbon dioxide input branch includes a third compressor; the electric hydrogen production cluster uses the electricity generated by the new energy power generation system to produce hydrogen and inputs the produced hydrogen into the inlet of the second compressor; the outlet of the second compressor is connected to the hydrogen inlet of the synthesis reactor; the inlet of the third compressor is connected to the inlet of the carbon dioxide input branch; and the outlet of the third compressor is connected to the carbon dioxide inlet of the synthesis reactor.

[0015] By applying the above technical solutions, based on methanol as a hydrogen and energy carrier, and through the scientific and rational coupling of processes such as methanol synthesis, methanol evaporation, methanol reforming, methanol separation, hydrogenation, and methanol combustion, a comprehensive and efficient supply of multiple energy forms, including hydrogen, electricity, heat, and cold, can be achieved, thereby realizing the efficient utilization of methanol energy. Attached Figure Description

[0016] To more clearly illustrate the technical solutions of this application, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the accompanying drawings described below are only some embodiments recorded in this application. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0017] Figure 1 This is a schematic diagram of the structure of the methanol synthesis and reforming hydrogen production and hydrogenation system according to an embodiment of this application. Figure 1 ;

[0018] Figure 2 This is a schematic diagram of the structure of the methanol synthesis and reforming hydrogen production and hydrogenation system according to an embodiment of this application. Figure 2 ;

[0019] Figure 3 This is a schematic diagram of the structure of the methanol synthesis and reforming hydrogen production and hydrogenation system according to an embodiment of this application. Figure 3 ;

[0020] Figure 4This is a schematic diagram of the structure of the methanol synthesis and reforming hydrogen production and hydrogenation system according to an embodiment of this application. Figure 4 .

[0021] Figures 1-4 In the diagram, 10. Hydrogen input branch; 11. New energy power generation system; 12. Electric hydrogen production cluster; 13. Second compressor; 20. Carbon dioxide input branch; 21. Third compressor; 30. Methanol synthesis equipment; 31. Synthesis reactor; 32. Methanol separator; 33. Second separator; 40. Methanol output branch; 41. Distillation column; 50. Methanol storage tank; 60. Methanol reforming reactor; 70. Methanol input branch; 71. Methanol evaporator; 72. Fuel mixing... Combined tank; 80, steam input branch; 90, methanol-hydrogen separation branch; 91, methanol separation and recovery equipment; 92, first separator; 100, waste heat recovery branch; 101, methanol preheater; 102, superheater; 103, vaporizer; 104, steam preheater; 110, hydrogen dispenser; 120, hydrogen dispensing branch; 121, hydrogen storage unit; 122, first compressor; 130, cogeneration unit; 131, steam turbine; 132, reciprocating internal combustion engine. Detailed Implementation

[0022] Various embodiments and features of this application are described herein with reference to the accompanying drawings.

[0023] It should be understood that various modifications can be made to the embodiments described herein. Therefore, the above description should not be considered as limiting, but merely as an example of embodiments. Other modifications within the scope and spirit of this application will be apparent to those skilled in the art.

[0024] The accompanying drawings, which are included in and form part of this specification, illustrate embodiments of the present application and, together with the general description of the present application given above and the detailed description of the embodiments given below, serve to explain the principles of the present application.

[0025] These and other features of this application will become apparent from the following description of preferred forms of embodiments given as non-limiting examples, with reference to the accompanying drawings.

[0026] It should also be understood that although this application has been described with reference to some specific examples, those skilled in the art can certainly implement many other equivalent forms of this application.

[0027] The above and other aspects, features and advantages of this application will become more apparent when taken in conjunction with the accompanying drawings and in view of the following detailed description.

[0028] Specific embodiments of this application are described thereafter with reference to the accompanying drawings; however, it should be understood that the claimed embodiments are merely examples of this application, which can be implemented in various ways. Well-known and / or repeated functions and structures are not described in detail to avoid unnecessary or redundant details that could obscure the application. Therefore, the specific structural and functional details claimed herein are not intended to be limiting, but merely serve as the basis and representative basis for the claims to teach those skilled in the art to use this application in a variety of substantially any suitable detailed structures.

[0029] This specification may use the phrases “in one embodiment,” “in another embodiment,” “in yet another embodiment,” or “in other embodiments,” all of which may refer to one or more of the same or different embodiments according to this application.

[0030] This application discloses a methanol synthesis and reforming hydrogen production and hydrogenation system. Based on methanol as a hydrogen carrier and energy carrier, it achieves a comprehensive and efficient supply of multiple energy forms, including hydrogen, electricity, heat, and cold, by scientifically and rationally coupling methanol synthesis, methanol evaporation, methanol reforming, methanol separation, hydrogenation, and methanol combustion processes, thereby realizing the efficient utilization of methanol energy.

[0031] like Figure 1 As shown, the methanol synthesis and reforming hydrogen production and hydrogenation system includes a hydrogen input branch 10, a carbon dioxide input branch 20, a methanol synthesis unit 30, a methanol output branch 40, a methanol storage tank 50, a methanol reforming reactor 60, a methanol input branch 70, a steam input branch 80, a methanol-hydrogen separation branch 90, a waste heat recovery branch 100, a hydrogenator 110, a hydrogenation branch 120, and a co-production unit 130.

[0032] The methanol synthesis equipment 30 can synthesize methanol using hydrogen input from hydrogen input branch 10 and carbon dioxide input from carbon dioxide input branch 20, and output the synthesized methanol from methanol output branch 40.

[0033] Methanol storage tank 50 is connected to methanol output branch 40. Methanol storage tank 50 is connected to methanol inlet of methanol reforming reactor 60 via methanol input branch 70. Steam input branch 80 is connected to steam inlet of methanol reforming reactor 60. Input end of methanol-hydrogen separation branch 90 is connected to product outlet of methanol reforming reactor 60. Carbon dioxide outlet of methanol-hydrogen separation branch 90 is connected to carbon dioxide input branch 20. Hydrogen outlet of methanol-hydrogen separation branch 90 outputs hydrogen. Tail gas outlet of methanol reforming reactor 60 is connected to waste heat recovery branch 100. Waste heat recovery branch 100 can transfer the heat of tail gas of methanol reforming reactor 60 to steam input branch 80 and methanol input branch 70.

[0034] The hydrogen inlet of the hydrogen refueling branch 120 is connected to the hydrogen outlet of the methanol-hydrogen separation branch 90, and the hydrogen outlet of the hydrogen refueling branch 120 is connected to the hydrogen refueling machine 110, which is used to fill hydrogen fuel cell vehicles with hydrogen.

[0035] The cogeneration unit 130 is connected to the methanol storage tank 50 and is used to obtain methanol from the methanol storage tank 50 and to produce at least one of electrical energy, thermal energy and cold energy by using the heat generated from burning methanol.

[0036] In this embodiment, hydrogen input branch 10 inputs hydrogen (H2) into methanol synthesis equipment 30, and carbon dioxide input branch 20 inputs carbon dioxide (CO2) into methanol synthesis equipment 30, enabling methanol synthesis equipment 30 to synthesize methanol (CH3OH) using hydrogen and carbon dioxide. The synthesized methanol is then transported to methanol storage tank 50 via methanol output branch 40. The carbon dioxide outlet of methanol-hydrogen separation branch 90 is connected to carbon dioxide input branch 20. Since the carbon dioxide output from methanol-hydrogen separation branch 90 can participate in methanol synthesis, the amount of carbon dioxide obtained from outside the system can be reduced, thus lowering the cost of methanol synthesis.

[0037] Methanol storage tank 50 is used to store liquid methanol. It can be an atmospheric pressure cryogenic tank, an ambient temperature pressurized tank, or a pressurized cryogenic tank, so that the methanol in methanol storage tank 50 exists in liquid form. In some embodiments of this application, methanol storage tank 50 is an ambient temperature pressurized tank with a rated pressure of 1 MPa. Methanol in methanol storage tank 50 can be transported to methanol reforming reactor 60 to generate hydrogen. Specifically, on the one hand, methanol in methanol storage tank 50 is transported to methanol reforming reactor 60 via methanol input branch 70. On the other hand, water vapor is transported to methanol reforming reactor 60 via water vapor input branch 80. Methanol and water vapor react in methanol reforming reactor 60, and the reaction product is transported from product outlet of methanol reforming reactor 60 to methanol-hydrogen separation branch 90. Methanol-hydrogen separation branch 90 can separate hydrogen and carbon dioxide from the product of methanol reforming reactor 60, and transport hydrogen to hydrogenation branch 120 and carbon dioxide to carbon dioxide input branch 20, which will then participate in methanol synthesis. The high-temperature tail gas generated by the methanol reforming reactor 60 is transported from the tail gas outlet of the methanol reforming reactor 60 to the waste heat recovery branch 100. The waste heat recovery branch 100 can transfer the heat of the tail gas of the methanol reforming reactor 60 to the steam input branch 80 and the methanol input branch 70, so as to increase the temperature of the methanol and steam entering the reforming reactor 60, thereby realizing the recovery of waste heat from the tail gas and improving the reaction efficiency of the methanol reforming reactor 60.

[0038] In some embodiments of this application, the products of the methanol reforming reactor 60 mainly include hydrogen, carbon dioxide, and methanol, with volume fractions of 69%, 23%, and 8%, respectively.

[0039] The hydrogen refueling branch 120 delivers hydrogen obtained from the methanol-hydrogen separation branch 90 to the hydrogen refueling machine 110, enabling the hydrogen refueling machine 110 to fill the hydrogen fuel cell vehicle with hydrogen. The hydrogen fuel cell vehicle can be a hydrogen fuel cell vehicle or a hydrogen internal combustion engine vehicle.

[0040] The methanol in methanol storage tank 50 is also supplied to cogeneration unit 130, whereby cogeneration unit 130 produces at least one of the following: electricity, heat, and cold energy, using the heat generated from burning methanol. The cogeneration unit 130 utilizes methanol fuel to produce electricity via a reciprocating internal combustion engine 132 (e.g., Figure 4 (As shown in the diagram) and generator, or gas turbine and generator. The cogeneration unit 130 utilizes methanol fuel to produce electricity and heat by employing a gas turbine, generator, and multi-stage heat exchanger. The cogeneration unit 130 utilizes methanol fuel to produce cooling energy by employing a gas turbine, generator, and absorption refrigeration equipment. Specifically, it can utilize a methanol gas turbine to drive a compression refrigeration unit, or a methanol gas turbine to drive a generator which in turn drives an electrically driven compression refrigeration unit, or it can utilize the waste heat from the methanol gas turbine's exhaust gas as a heat source for the absorption refrigeration equipment.

[0041] The methanol synthesis and reforming hydrogen production and hydrogenation system of this application includes a hydrogen input branch 10, a carbon dioxide input branch 20, a methanol synthesis device 30, a methanol output branch 40, a methanol storage tank 50, a methanol reforming reactor 60, a methanol input branch 70, a steam input branch 80, a methanol-hydrogen separation branch 90, a waste heat recovery branch 100, a hydrogenator 110, a hydrogenation branch 120, and a co-production unit 130. Based on methanol as a hydrogen and energy carrier, by scientifically and rationally coupling methanol synthesis, methanol evaporation, methanol reforming, methanol separation, hydrogenation, and methanol combustion processes, a comprehensive and efficient supply of multiple energy forms such as hydrogen, electricity, heat, and cold can be achieved, thereby realizing the efficient utilization of methanol energy.

[0042] In some embodiments of this application, such as Figure 2 As shown, the methanol input branch 70 includes a methanol evaporator 71 and a fuel mixing tank 72, and the waste heat recovery branch 100 includes a methanol preheater 101. The methanol preheater 101 includes a first cold fluid channel and a first hot fluid channel, wherein...

[0043] The methanol inlet of the methanol evaporator 71 is connected to the methanol storage tank 50, the methanol outlet of the methanol evaporator 71 is connected to the inlet of the first cold fluid channel and the methanol inlet of the fuel mixing tank 72, the outlet of the first cold fluid channel is connected to the methanol inlet of the methanol reforming reactor 60, the first hot fluid channel is connected to the tail gas outlet of the methanol reforming reactor 60, the hydrogen outlet of the methanol-hydrogen separation branch 90 is connected to the hydrogen inlet of the fuel mixing tank 72, and the fuel outlet of the fuel mixing tank 72 is connected to the fuel inlet of the methanol reforming reactor 60.

[0044] In this embodiment, the methanol evaporator 71 evaporates the methanol input from the methanol storage tank 50 and sends the evaporated methanol to the methanol preheater 101. The methanol absorbs heat from the tail gas in the first hot fluid channel in the first cold fluid channel, thus increasing its temperature. The methanol output from the first cold fluid channel is then sent to the methanol reforming reactor 60, thereby improving the reforming reaction efficiency of the methanol reforming reactor 60. The fuel mixing tank 72 contains a mixture of hydrogen and methanol in any proportion, or pure hydrogen or pure methanol; the rated pressure of the fuel mixing tank 72 is atmospheric pressure. In some embodiments of this application, the fuel mixing tank 72 contains a mixture of hydrogen and methanol, with volume fractions of 15% and 85%, respectively.

[0045] In some embodiments of this application, such as Figure 2 As shown, a heat exchange medium channel is provided between the methanol evaporator 71 and the hydrogenator 110. The heat exchange medium channel can transfer the heat of the hydrogenator 110 to the methanol evaporator 71 through the heat exchange medium, so that the methanol evaporator 71 can carry out the methanol evaporation process.

[0046] In this embodiment, the hydrogen dispenser 110 generates heat during the hydrogen dispensing process because it needs to compress hydrogen. By setting a heat exchange medium channel between the methanol evaporator 71 and the hydrogen dispenser 110, the heat from the hydrogen dispenser 110 is transferred to the methanol evaporator 71 through the heat exchange medium channel, thereby improving the operating efficiency of the methanol evaporator 71.

[0047] In some embodiments of this application, the methanol-hydrogen separation branch 90 includes a methanol separation and recovery device 91 and a first separator 92. The inlet of the methanol separation and recovery device 91 is the input end of the methanol-hydrogen separation branch 90. The non-methanol outlet of the methanol separation and recovery device 91 is connected to the inlet of the first separator 92. The methanol outlet of the methanol separation and recovery device 91 is connected to the methanol inlet of the methanol reforming reactor 60 via a check valve. The first outlet of the first separator 92 is the carbon dioxide outlet of the methanol-hydrogen separation branch 90, and the second outlet of the first separator 92 is the hydrogen outlet of the methanol-hydrogen separation branch 90.

[0048] In this embodiment, the methanol separation and recovery device 91 is used to recover methanol from the product of the methanol reforming reactor 60 via the methanol outlet to the methanol inlet of the methanol reforming reactor 60. A check valve is provided between the methanol outlet of the methanol separation and recovery device 91 and the methanol inlet of the methanol reforming reactor 60 to prevent methanol output from the methanol storage tank 50 from directly reaching the methanol separation and recovery device 91. The methanol separation and recovery device 91 also transports hydrogen and carbon dioxide from the product via the non-methanol outlet to the first separator 92 for further separation. The first separator 92 transports the separated carbon dioxide to the carbon dioxide input branch 20 and the separated hydrogen to the hydrogenation branch 120. In some embodiments of this application, the first separator 92 also transports the separated hydrogen to the hydrogen inlet of the fuel mixing tank 72.

[0049] By setting up methanol separation and recovery equipment 91 and first separator 92, more reliable methanol separation and recovery can be achieved, and carbon dioxide and hydrogen can be separated.

[0050] In some embodiments of this application, the volume fraction of methanol at the outlet of the methanol separation and recovery device 91 is less than 0.1%. The methanol separation and recovery device 91 can be any one of a pressure swing adsorption-desorption device, a temperature swing adsorption-desorption device, a cryogenic separation device, or a membrane separation device. When using a temperature swing adsorption-desorption device, water is used as the adsorbent, which can reduce the volume fraction of methanol at the outlet of the temperature swing adsorption-desorption device to less than 0.06%. The first separator 92 can be a membrane separator, which requires no energy input to operate; the membrane separator uses the membrane separation principle; the volume fraction of hydrogen at the outlet of the first separator 92 is greater than 99.97%; the tail gas of the first separator 92 is mainly carbon dioxide.

[0051] In some embodiments of this application, such as Figure 2 As shown, when the cogeneration unit 130 produces electrical energy, heat energy and cold energy, the methanol separation and recovery equipment 91 and the first separator 92 operate using the electrical energy, heat energy and cold energy obtained from the cogeneration unit 130, thereby enabling the methanol separation and recovery equipment 91 and the first separator 92 to operate without the need for additional energy input, thus improving energy utilization efficiency.

[0052] In some embodiments of this application, the waste heat recovery branch 100 further includes a superheater 102, a vaporizer 103, and a steam preheater 104. The superheater 102 includes a second cold fluid channel and a second hot fluid channel, the vaporizer 103 includes a third cold fluid channel and a third hot fluid channel, and the steam preheater includes a fourth cold fluid channel and a fourth hot fluid channel.

[0053] The tail gas outlet of the methanol reforming reactor 60 is connected to the fourth hot fluid channel via the second hot fluid channel, the first hot fluid channel, and the third hot fluid channel in sequence. The steam input branch 80 is connected to the steam inlet of the methanol reforming reactor 60 via the fourth cold fluid channel. The condensate outlet of the co-production unit 130 is connected to the inlet of the third cold fluid channel. The outlet of the third cold fluid channel is connected to the inlet of the second cold fluid channel. The outlet of the second cold fluid channel of the superheater 102 is connected to the superheated steam inlet of the co-production unit 130.

[0054] In this embodiment, the tail gas outlet temperature of the methanol reforming hydrogen production reaction can reach 270°C, thus sequentially meeting the heat exchange requirements of superheater 102, methanol preheater 101, vaporizer 103, and steam preheater 104. By setting up the steam preheater 104, the temperature of the steam entering the methanol reforming reactor 60 can be increased, thereby improving the reaction efficiency of the methanol reforming reactor 60. The tail gas in the fourth hot fluid channel of the steam preheater 104 mainly includes carbon dioxide, water, and oxygen. By setting up the vaporizer 103 and superheater 102, the condensate output from the co-production unit 130 can be sequentially heated and converted into saturated steam and superheated steam. The superheated steam can drive the steam turbine 131 in the co-production unit 130 (e.g., [missing information]). Figure 4 (as shown) and generator; superheated steam can also be input into the multi-stage heat exchanger in the cogeneration unit 130 to produce heat energy; superheated steam can also drive the absorption refrigeration equipment in the cogeneration unit 130 to generate cold energy, thereby realizing flexible and efficient utilization of superheated steam.

[0055] In some embodiments of this application, the hydrogen refueling branch 120 includes a hydrogen storage unit 121 and a first compressor 122. The inlet of the first compressor 122 is the hydrogen inlet of the hydrogen refueling branch 120, and the outlet of the first compressor 122 is connected to the inlet of the hydrogen storage unit 121. The outlet of the hydrogen storage unit 121 is the hydrogen outlet of the hydrogen refueling branch 120.

[0056] In this embodiment, the rated discharge pressure of the first compressor 122 can be 45-90 MPa, and the hydrogen storage unit 121 can be composed of a group of hydrogen storage cylinders or a hydrogen storage tank with a rated hydrogen storage pressure of 25-90 MPa. In some embodiments of this application, the hydrogen storage unit 121 is composed of a group of hydrogen storage cylinders with a rated hydrogen storage pressure of 25 MPa and a rated pressure of 45 MPa. By setting up the hydrogen storage unit 121 and the first compressor 122, hydrogen can be supplied to the hydrogen dispenser 110 more efficiently and reliably.

[0057] In some embodiments of this application, such as Figure 2 As shown, when the cogeneration unit 130 produces electrical energy, the hydrogen refueling machine 110 and the first compressor 122 operate using the electrical energy obtained from the cogeneration unit 130.

[0058] In this embodiment, the cogeneration unit 130 can provide electrical energy to the hydrogen refueling machine 110 and the first compressor 122, thereby enabling the operation of the hydrogen refueling machine 110 and the first compressor 122 without the need for external electrical energy input, thus improving energy utilization efficiency.

[0059] In some embodiments of this application, the hydrogen dispenser 110 has a dispensing pressure of 35 MPa or 70 MPa.

[0060] In some embodiments of this application, such as Figure 3 As shown, the methanol synthesis equipment 30 includes a synthesis reactor 31, a methanol separator 32, and a second separator 33. The methanol output branch 40 includes a distillation column 41.

[0061] The hydrogen inlet of the synthesis reactor 31 is connected to the hydrogen input branch 10 and the hydrogen outlet of the second separator 33. The carbon dioxide inlet of the synthesis reactor 31 is connected to the carbon dioxide input branch 20 and the carbon dioxide outlet of the second separator 33. The product outlet of the synthesis reactor 31 is connected to the inlet of the methanol separator 32. The methanol outlet of the methanol separator 32 is connected to the inlet of the distillation column 41. The non-methanol outlet of the methanol separator 32 is connected to the inlet of the second separator 33. The outlet of the distillation column 41 is connected to the methanol storage tank 50.

[0062] In this embodiment, hydrogen and carbon dioxide are synthesized into methanol in the synthesis reactor 31. The products of the synthesis reactor 31 (including hydrogen, carbon dioxide, methanol, and water) enter the methanol separator 32. The methanol separator sends the separated methanol to the distillation column 41 for distillation. The methanol separator 32 sends the separated non-methanol working fluid to the second separator 33, where the second separator 33 further separates carbon dioxide and hydrogen. The hydrogen output from the second separator 33 is sent back to the hydrogen inlet of the synthesis reactor 31, and the carbon dioxide separated by the second separator 33 is sent back to the carbon dioxide inlet of the synthesis reactor 31, realizing the recovery and utilization of hydrogen and carbon dioxide. The distillation column 41 sends the methanol to the methanol storage tank 50, and the methanol in the methanol storage tank 50 is subsequently used to generate hydrogen and provide fuel for the cogeneration unit 130.

[0063] In some embodiments of this application, such as Figure 3 As shown, the hydrogen input branch 10 includes a new energy power generation system 11, an electric hydrogen production cluster 12, and a second compressor 13; the carbon dioxide input branch 20 includes a third compressor 21.

[0064] The electric hydrogen production cluster 12 uses the electricity generated by the new energy power generation system 11 to produce hydrogen, and inputs the produced hydrogen into the inlet of the second compressor 13. The outlet of the second compressor 13 is connected to the hydrogen inlet of the synthesis reactor 31. The inlet of the third compressor 21 is connected to the inlet of the carbon dioxide input branch 20, and the outlet of the third compressor 21 is connected to the carbon dioxide inlet of the synthesis reactor 31.

[0065] In this embodiment, the power generation method of the new energy power generation system 11 may include at least one of photovoltaic power generation and wind power generation. The electricity generated by the new energy power generation system 11 drives the electro-hydrogen production cluster 12 to produce hydrogen, achieving low-cost hydrogen production while absorbing renewable energy. The second compressor 13 ensures efficient and reliable delivery of hydrogen to the synthesis reactor 31. The third compressor 21 ensures efficient and reliable delivery of carbon dioxide to the synthesis reactor 31, thereby further improving the methanol synthesis efficiency.

[0066] By applying the above technical solutions, the following technical effects can be achieved:

[0067] 1) It provides a novel terminal energy supply system implementation method for future scenarios where methanol is the main hydrogen carrier and energy carrier;

[0068] 2) This system fully couples the electrical, thermal, and cold flows of methanol synthesis, methanol evaporation, methanol reforming, methanol separation, hydrogenation, and methanol combustion processes, which can achieve high system energy efficiency and improve system economy;

[0069] 3) This system can achieve the combined output of multiple energy forms, including electricity, hydrogen, heat, and cooling, thereby enhancing the diversity of energy supply;

[0070] 4) The system can flexibly adjust the output ratio of different energy forms such as electricity, hydrogen, heat and cold according to the needs of the terminal, which can achieve high flexibility and improve the reliability of the energy system.

[0071] Furthermore, although exemplary embodiments have been described herein, their scope includes any and all embodiments based on this disclosure that have equivalent elements, modifications, omissions, combinations (e.g., schemes involving intersections of various embodiments), adaptations, or alterations. Elements in the claims will be interpreted broadly based on the language used in the claims and are not limited to the examples described in this specification or during the implementation of this application, and such examples will be interpreted as non-exclusive. Therefore, this specification and examples are intended to be considered illustrative only, and the true scope and spirit are indicated by the full scope of the following claims and their equivalents.

[0072] The above description is intended to be illustrative and not restrictive. For example, the above examples (or one or more thereof) can be used in combination with each other. Other embodiments may be used by those skilled in the art upon reading the above description. Furthermore, in the above detailed description, various features may be grouped together to simplify the disclosure. This should not be construed as an intention that a feature of the disclosure that is not claimed is necessary for any claim. Rather, the subject matter of this disclosure may be less than all the features of a particular disclosed embodiment. Thus, the following claims are incorporated herein by reference as examples or embodiments, wherein each claim is an independent, separate embodiment, and these embodiments are contemplated to be combined with each other in various combinations or arrangements. The scope of this disclosure should be determined by reference to the appended claims and the full scope of their equivalents.

[0073] The foregoing has provided a detailed description of several embodiments of this disclosure. However, this disclosure is not limited to these specific embodiments. Those skilled in the art can make various variations and modifications based on the concept of this disclosure, and all such variations and modifications should fall within the scope of protection claimed by this disclosure.

Claims

1. A methanol synthesis and reforming hydrogen production and hydrogenation system, characterized in that, This includes hydrogen input branch, carbon dioxide input branch, methanol synthesis equipment, methanol output branch, methanol storage tank, methanol reforming reactor, methanol input branch, steam input branch, methanol-hydrogen separation branch, waste heat recovery branch, hydrogenator, hydrogenation branch, and co-production unit. The methanol synthesis equipment is capable of synthesizing methanol using hydrogen input from the hydrogen input branch and carbon dioxide input from the carbon dioxide input branch, and outputting the synthesized methanol from the methanol output branch. The methanol storage tank is connected to the methanol output branch, and the methanol storage tank is connected to the methanol inlet of the methanol reforming reactor via the methanol input branch. The steam input branch is connected to the steam inlet of the methanol reforming reactor. The input end of the methanol-hydrogen separation branch is connected to the product outlet of the methanol reforming reactor. The carbon dioxide outlet of the methanol-hydrogen separation branch is connected to the carbon dioxide input branch. The hydrogen outlet of the methanol-hydrogen separation branch outputs hydrogen. The tail gas outlet of the methanol reforming reactor is connected to the waste heat recovery branch, which can transfer the heat of the tail gas of the methanol reforming reactor to the steam input branch and the methanol input branch. The hydrogen inlet of the hydrogen refueling branch is connected to the hydrogen outlet of the methanol-hydrogen separation branch, and the hydrogen outlet of the hydrogen refueling branch is connected to the hydrogen dispenser, which is used to fill hydrogen fuel cell vehicles with hydrogen. The co-production unit is connected to the methanol storage tank and is used to obtain methanol from the methanol storage tank and produce at least one of electrical energy, thermal energy, and cold energy by using the heat generated from burning methanol.

2. The methanol synthesis and reforming hydrogen production system as described in claim 1, characterized in that, The methanol input branch includes a methanol evaporator and a fuel mixing tank, and the waste heat recovery branch includes a methanol preheater, which includes a first cold fluid channel and a first hot fluid channel, wherein... The methanol inlet of the methanol evaporator is connected to the methanol storage tank, the methanol outlet of the methanol evaporator is connected to the inlet of the first cold fluid channel and the methanol inlet of the fuel mixing tank, the outlet of the first cold fluid channel is connected to the methanol inlet of the methanol reforming reactor, the first hot fluid channel is connected to the tail gas outlet of the methanol reforming reactor, the hydrogen outlet of the methanol-hydrogen separation branch is connected to the hydrogen inlet of the fuel mixing tank and the hydrogenation branch, and the fuel outlet of the fuel mixing tank is connected to the fuel inlet of the methanol reforming reactor.

3. The methanol synthesis and reforming hydrogen production system as described in claim 2, characterized in that, A heat exchange medium channel is provided between the methanol evaporator and the hydrogenator. The heat exchange medium channel can transfer the heat from the hydrogenator to the methanol evaporator through the heat exchange medium, so that the methanol evaporator can carry out the methanol evaporation process.

4. The methanol synthesis and reforming hydrogen production system as described in claim 1, characterized in that, The methanol-hydrogen separation branch includes a methanol separation and recovery device and a first separator. The inlet of the methanol separation and recovery device is the input end of the methanol-hydrogen separation branch. The non-methanol outlet of the methanol separation and recovery device is connected to the inlet of the first separator. The methanol outlet of the methanol separation and recovery device is connected to the methanol inlet of the methanol reforming reactor via a check valve. The first outlet of the first separator is the carbon dioxide outlet of the methanol-hydrogen separation branch, and the second outlet of the first separator is the hydrogen outlet of the methanol-hydrogen separation branch.

5. The methanol synthesis and reforming hydrogen production system as described in claim 4, characterized in that, When the cogeneration unit produces electricity, heat, and cold energy, the methanol separation and recovery equipment and the first separator operate using the electricity, heat, and cold energy obtained from the cogeneration unit.

6. The methanol synthesis and reforming hydrogen production and hydrogenation system as described in claim 2, characterized in that, The waste heat recovery branch also includes a superheater, a vaporizer, and a steam preheater. The superheater includes a second cold fluid channel and a second hot fluid channel. The vaporizer includes a third cold fluid channel and a third hot fluid channel. The steam preheater includes a fourth cold fluid channel and a fourth hot fluid channel. The tail gas outlet of the methanol reforming reactor is connected to the fourth hot fluid channel via the second hot fluid channel, the first hot fluid channel, and the third hot fluid channel in sequence. The steam input branch is connected to the steam inlet of the methanol reforming reactor via the fourth cold fluid channel. The condensate outlet of the co-production unit is connected to the inlet of the third cold fluid channel. The outlet of the third cold fluid channel is connected to the inlet of the second cold fluid channel. The outlet of the second cold fluid channel of the superheater is connected to the superheated steam inlet of the co-production unit.

7. The methanol synthesis and reforming hydrogen production and hydrogenation system as described in claim 1, characterized in that, The hydrogen refueling branch includes a hydrogen storage unit and a first compressor. The inlet of the first compressor is the hydrogen inlet of the hydrogen refueling branch, and the outlet of the first compressor is connected to the inlet of the hydrogen storage unit. The outlet of the hydrogen storage unit is the hydrogen outlet of the hydrogen refueling branch.

8. The methanol synthesis and reforming hydrogen production and hydrogenation system as described in claim 7, characterized in that, When the cogeneration unit produces electricity, the hydrogen refueling machine and the first compressor operate using the electricity obtained from the cogeneration unit.

9. The methanol synthesis and reforming hydrogen production and hydrogenation system as described in claim 1, characterized in that, The methanol synthesis equipment includes a synthesis reactor, a methanol separator, and a second separator; the methanol output branch includes a distillation column. The hydrogen inlet of the synthesis reactor is connected to the hydrogen input branch and the hydrogen outlet of the second separator; the carbon dioxide inlet of the synthesis reactor is connected to the carbon dioxide input branch and the carbon dioxide outlet of the second separator; the product outlet of the synthesis reactor is connected to the inlet of the methanol separator; the methanol outlet of the methanol separator is connected to the inlet of the distillation column; the non-methanol outlet of the methanol separator is connected to the inlet of the second separator; and the outlet of the distillation column is connected to the methanol storage tank.

10. The methanol synthesis and reforming hydrogen production and hydrogenation system as described in claim 9, characterized in that, The hydrogen input branch includes a new energy power generation system, an electric hydrogen production cluster, and a second compressor; the carbon dioxide input branch includes a third compressor. The electro-hydrogen production cluster uses the electricity generated by the new energy power generation system to produce hydrogen, and inputs the produced hydrogen into the inlet of the second compressor. The outlet of the second compressor is connected to the hydrogen inlet of the synthesis reactor. The inlet of the third compressor is connected to the inlet of the carbon dioxide input branch, and the outlet of the third compressor is connected to the carbon dioxide inlet of the synthesis reactor.

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