Hydrogen production purification system and method

Abstract

The invention relates to a hydrogen production purification system and method. The system comprises a composite heat exchanger, a deaerator, a first condenser, an adsorption unit and a finished hydrogen collection unit. According to the hydrogen production purification system and method, all the parts of the hydrogen production purification system are reasonably arranged, the flow directions of material flows of all the parts are reasonably designed, and energy generated in the purification and regeneration process can be secondarily absorbed and utilized in cooperation with the composite heat exchanger and the gas heat exchanger; the composite heat exchanger is used for reheating the cooled and condensed raw material hydrogen, and the heated hydrogen reaches or is close to the temperature during oxygen removal, so that the energy consumption of the deaerator during working can be reduced; and the gas subjected to heat exchange on the high-temperature regenerated hydrogen in the gas heat exchanger enters a second heat exchange process, secondary energy reutilization is performed on the gas, and the energy recycling rate is high.

Description

Technical Field

[0001] The present application relates to the technical field of hydrogen production, and in particular to a hydrogen production and purification system and method. Background Art

[0002] The development of hydrogen energy can fundamentally alleviate the energy security problems caused by my country's large-scale import of oil and gas resources. Its special properties as an energy storage medium can promote the rapid development of large-scale renewable energy. It is an important means for my country to achieve its "dual carbon goals".

[0003] In recent years, the field of hydrogen production has made great progress, and the energy consumption required for hydrogen production has become increasingly higher, requiring more energy-efficient hydrogen production equipment. The purification systems of traditional hydrogen production equipment all have the regeneration function of deoxygenation / dehydrogenation devices and adsorbers. However, the traditional hydrogen production purification system does not pre-treat the gas before deoxygenation / dehydrogenation, resulting in a short service life of the catalyst inside the dehydrogenation / deoxygenator; and large energy loss. Summary of the invention

[0004] In a first aspect, the present application provides a hydrogen production and purification system, comprising:

[0005] A composite heat exchanger comprising:

[0006] The first heat exchange zone comprises:

[0007] A condensation chamber, with a closed cavity inside;

[0008] A ventilation pipeline is arranged in the closed cavity, and the ventilation pipeline is provided with an air inlet and an air outlet, and the air inlet and the air outlet are both connected to the outer wall of the condensation bin; wherein,

[0009] The air inlet is used to introduce the raw hydrogen flow into the first heat exchange zone, and the air outlet is used to discharge the first zone hydrogen flow that has been condensed in the first heat exchange zone; and

[0010] The condensation pipe is used for the circulation of the condensation medium and for heat exchange with the ventilation pipe;

[0011] The second heat exchange zone comprises:

[0012] A heat exchange chamber, wherein a first channel and a second channel isolated from each other are provided in the heat exchange chamber;

[0013] The heat exchange bin is provided with a transfer inlet and a heat exchange bin hydrogen flow outlet, the transfer inlet is communicated with the outlet; the first channel is communicated with the transfer inlet and the heat exchange bin hydrogen flow outlet, so that the first zone hydrogen flow from the first heat exchange zone passes through the second heat exchange zone and then passes through the heat exchange zone.

[0014] The hot storehouse hydrogen gas flow outlet is discharged from the composite heat exchanger;

[0015] The heat exchange bin is also provided with a heat exchange hydrogen gas inlet and a heat exchange hydrogen gas outlet, and the second channel is connected with the heat exchange hydrogen gas inlet and the heat exchange hydrogen gas outlet, and is used to transport the heat exchange hydrogen gas to the second heat exchange zone through the second channel, and output the heat exchanged hydrogen gas;

[0016] A deaerator, which is connected to the hydrogen flow outlet of the heat exchange bin of the second heat exchange zone, so that the second zone hydrogen flow heated by the second heat exchange zone enters the deaerator for deoxygenation treatment;

[0017] A first condenser, wherein the first condenser is connected to the hydrogen flow outlet of the deaerator, so that the deaerator hydrogen flow that has been deoxygenated by the deaerator enters the first condenser for a first condensation treatment; and

[0018] An adsorption unit is used to process the first condenser hydrogen flow from the first condenser; the adsorption unit includes a gas heat exchanger and a second condenser, and a first adsorption tower, a second adsorption tower and a third adsorption tower; wherein,

[0019] The hydrogen flow inlet of the first adsorption tower is connected to the hydrogen flow outlet of the first condenser, so as to transport the hydrogen flow of the first condenser to the first adsorption tower for the first adsorption treatment;

[0020] The first pass inlet of the gas heat exchanger is connected to the hydrogen flow outlet of the first adsorption tower, so that the hydrogen flow from the first adsorption tower treated by the first adsorption tower flows through the first pass of the gas heat exchanger; the second pass inlet of the gas heat exchanger is connected to the heat exchange hydrogen flow inlet, so that the heat exchanged hydrogen flow from the second heat exchange zone flows through the second pass of the gas heat exchanger; thereby, the hydrogen flow from the second heat exchange zone flows through the second pass of the gas heat exchanger.

[0021] The first adsorption tower hydrogen flow of the first adsorption tower and the heat-exchanged hydrogen flow from the second heat exchange zone are heat exchanged in a gas heat exchanger;

[0022] The first pass outlet of the gas heat exchanger is connected to the hydrogen flow inlet of the second adsorption tower, so that the first pass output hydrogen flow heated by the gas heat exchanger is transported to the second adsorption tower to regenerate the second adsorption tower;

[0023] The hydrogen gas outlet of the second adsorption tower is connected to the heat exchange hydrogen gas inlet of the second heat exchange zone, so that the regenerated hydrogen gas discharged from the second adsorption tower flows through the second heat exchange zone and is used as the heat exchange hydrogen gas to heat the first zone hydrogen gas from the first heat exchange zone;

[0024] The second pass outlet of the gas heat exchanger is connected to the hydrogen flow inlet of the second condenser, so that the second pass output hydrogen flow cooled by the gas heat exchanger is transported to the second condenser for second condensation treatment;

[0025] The hydrogen flow inlet of the third adsorption tower is connected to the hydrogen flow outlet of the second condenser, so as to transport the hydrogen flow of the second condenser cooled by the second condenser to the third adsorption tower for second adsorption treatment; and

[0026] The finished hydrogen collection unit is used to collect the finished hydrogen flow processed by the adsorption unit.

[0027] In one embodiment, the hydrogen gas outlet of the first adsorption tower, the hydrogen gas outlet of the second adsorption tower, and the hydrogen gas outlet of the third adsorption tower are connected by an outlet pneumatic three-way valve;

[0028] The hydrogen production and purification system further comprises a filter, which is connected to the outlet pneumatic three-way valve so that the finished hydrogen gas flow processed by the adsorption unit flows through the filter.

[0029] In one embodiment, the hydrogen production and purification system further includes a condensing medium circulation unit, which is respectively connected to the condensing pipe of the first heat exchange zone, the first condenser and the second condenser, and is used to circulate the condensing medium in the first heat exchange zone, the first condenser and the second condenser.

[0030] In one embodiment, the hydrogen production and purification system further includes a condensate tank.

[0031] A drain port is provided at the bottom of the first heat exchange zone, and the drain port of the first heat exchange zone is connected to the condensate tank;

[0032] The first condenser and the second condenser are provided with drain ports, and the drain ports of the first condenser and the second condenser are connected to the condensation tank;

[0033] The hydrogen production and purification system further comprises a drainage liquid seal, and the drainage liquid seal is connected to the condensate tank.

[0034] In one embodiment, the gas passage formed in the ventilation pipeline includes a condensation section and a liquid capture section, and the gas to be condensed flows from the air inlet, sequentially through the condensation section and the liquid capture section, and is discharged from the air outlet;

[0035] The liquid collecting section is provided with a liquid collecting member for assisting in collecting condensed water; and

[0036] The liquid-catching section is provided with a downward condensation port for discharging condensed water.

[0037] In one embodiment, the condensation pipeline is located in the condensation section; the condensation pipeline is wrapped around the outer periphery of the liquid capture section.

[0038] In one embodiment, a ventilation gap is provided between the ventilation pipeline and the interior of the condensation bin; the ventilation gap is the condensation section, the channel in the ventilation pipeline is the liquid catching section, and the end of the liquid catching section away from the air outlet is a condensation outlet for discharging condensed water.

[0039] In one embodiment, the ventilation pipeline includes an inner tube and an outer tube sleeved outside the inner tube;

[0040] The cross section of the inner tube is rectangular, and the cross section of the outer tube is circular;

[0041] The condensation pipeline is coated on the outer tube.

[0042] In one embodiment, the liquid-catching member comprises a plurality of baffles arranged at intervals;

[0043] The plurality of baffles separate the liquid-catching section into a plurality of baffle channels extending in a serpentine shape.

[0044] In one embodiment, the condensation section is directly connected to each of the baffle channels.

[0045] In a second aspect, the present application further provides a hydrogen production and purification method, which is performed in the above-mentioned hydrogen production and purification system of the present application, and comprises:

[0046] S1 introduces the raw hydrogen flow into the first heat exchange zone of the composite heat exchanger through the air inlet, and after condensation treatment in the first heat exchange zone, the obtained first zone hydrogen flow is discharged from the air outlet; and the first zone hydrogen flow enters the second heat exchange zone of the composite heat exchanger through the transfer inlet, exchanges heat with the heat exchange hydrogen flow in the second heat exchange zone, and the obtained second zone hydrogen flow is discharged from the hydrogen flow outlet of the heat exchange bin;

[0047] S2 allows the second zone hydrogen gas flow to enter a deaerator, where it is deoxygenated;

[0048] S3 allows the deaerator hydrogen flow from the deaerator to enter the first condenser for a first condensation process;

[0049] S4 allows the first condenser hydrogen gas stream from the first condenser to be transported to an adsorption unit for treatment;

[0050] S5 enables the finished hydrogen gas stream treated by the adsorption unit to be transported to a finished hydrogen collection unit;

[0051] The treatment in the adsorption unit includes:

[0052] S41 allows the first condenser hydrogen flow from the first condenser to be transported to the first adsorption tower for first adsorption;

[0053] S42 allows at least a portion of the first adsorption tower hydrogen flow from the first adsorption tower to flow through the first pass of the gas heat exchanger, and allows the heat-exchanged hydrogen flow from the second heat exchange zone to flow through the second pass of the gas heat exchanger, so that the first adsorption tower hydrogen flow and the heat-exchanged hydrogen flow are heat exchanged in the gas heat exchanger;

[0054] S43 transports the first pass output hydrogen flow from the gas heat exchanger to the second adsorption tower to regenerate the second adsorption tower; the regenerated hydrogen flow discharged from the second adsorption tower is input into the second heat exchange zone through the heat exchange hydrogen flow inlet as the heat exchange hydrogen flow, and the heat exchanged hydrogen flow is discharged from the heat exchange hydrogen flow outlet; and

[0055] S44 transports the second-pass output hydrogen gas flow from the gas heat exchanger to the second condenser for second condensation treatment; transports the second condenser hydrogen gas flow cooled by the second condenser to the third adsorption tower for second adsorption treatment to obtain the finished hydrogen gas flow.

[0056] In one embodiment, the raw hydrogen gas stream comes from one or more hydrogen production systems, including one or more of an ALK hydrogen production system, a PEM hydrogen production system, an AEM hydrogen production system, and a SOEC hydrogen production system.

[0057] The hydrogen production and purification system and method of the present application, by providing a composite heat exchanger, connects the crude hydrogen (hydrogen raw material flow) to the air inlet before deoxygenating and purifying the hydrogen, so that the crude hydrogen flows through the ventilation pipeline, and introduces a condensing medium into the condensing pipeline, condenses the crude hydrogen, and condenses and precipitates the moisture and impurities therein, and then introduces the crude hydrogen into the deaerator for deoxygenation after the moisture and impurities are removed, which can reduce the problem of impurities in the crude hydrogen contaminating the catalyst, play a better protective role on the catalyst, and extend the service life of the catalyst; and the condensed gas is heated by the provided heat exchange chamber, so that the subsequent deoxygenation efficiency is higher, and the subsequent deoxygenation is reduced. The process requires heating to a certain temperature, which saves energy. At the same time, the various parts of the hydrogen production and purification system of the present application are reasonably laid out, and the flow direction of the material flow of each part is reasonably designed. In conjunction with the composite heat exchanger and the gas heat exchanger, the energy generated in the purification and regeneration process can be absorbed and utilized for a second time, which can reduce the overall energy consumption: the raw hydrogen after cooling and condensation is reheated in the composite heat exchanger, and the heated hydrogen reaches or approaches the temperature during deoxygenation, which can reduce the energy consumption of the deaerator during operation; the gas after heat exchange of the high-temperature regenerated hydrogen in the gas heat exchanger enters the second heat exchange process, and the gas is reused for secondary energy, with a high energy recovery rate. BRIEF DESCRIPTION OF THE DRAWINGS

[0058] In order to more clearly illustrate the technical solutions in the embodiments of the present application, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present application. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative labor.

[0059] Figure 1 A schematic diagram of the overall structure of a composite heat exchanger provided in some embodiments of the present application;

[0060] Figure 2 A perspective structural diagram of a composite heat exchanger provided in some embodiments of the present application;

[0061] Figure 3 A schematic diagram of the structure of a ventilation circuit portion provided in some embodiments of the present application;

[0062] Figure 4 A schematic diagram of the coordination relationship between the condensation pipeline and the ventilation pipeline provided in some embodiments of the present application;

[0063] Figure 5 A schematic diagram of the structure of a heat exchange chamber and a heat exchange tube provided in some embodiments of the present application;

[0064] Figure 6 A schematic diagram of the overall structure of a composite heat exchanger provided in some other embodiments of the present application;

[0065] Figure 7 A schematic diagram of a hydrogen production and purification system provided in some other embodiments of the present application;

[0066] Figure 8 Schematic diagram of the overall structure of the adsorption unit provided in other embodiments of the present application.

[0067] The reference numerals are as follows:

[0068] 1. Condensation chamber, 11. Drain port;

[0069] 2. ventilation pipeline, 21. condensation section, 22. liquid capture section, 23. inner tube, 24. outer tube;

[0070] 2a, air inlet, 2b, air outlet, 2c, condensation outlet;

[0071] 3. Condensation pipeline;

[0072] 4. Baffle;

[0073] 4a, baffle channel;

[0074] 5. heat exchange chamber, 51. transfer inlet, 52. exhaust port, 53. air inlet pipe, 54. air outlet pipe;

[0075] 6. Heat exchange tube;

[0076] 100. Composite heat exchanger, 101. Different hydrogen production systems 101;

[0077] 200. Deaerator;

[0078] 300, a first condenser;

[0079] 400, adsorption unit, 401, first adsorption tower, 402, second adsorption tower, 403, third adsorption tower, 404, gas heat exchanger, 405, second condenser;

[0080] 501, condensate tank, 502, drainage liquid seal, 503, drainer, 504, liquid replenisher, 505, gas exhaust device, 506, filter, 507, purity meter, 508, dew point meter, 509, unqualified hydrogen exhaust device;

[0081] 600, cooling medium circulation unit, 610, condensing medium water inlet tank, 620, condensing medium water return tank;

[0082] 700. Finished product hydrogen collection unit. DETAILED DESCRIPTION

[0083] The present application is further described in detail below through the accompanying drawings and embodiments. Through these descriptions, the characteristics and advantages of the present application will become clearer and more specific.

[0084] The word "exemplary" is used exclusively herein to mean "serving as an example, embodiment, or illustration." Any embodiment described herein as "exemplary" is not necessarily to be construed as preferred or advantageous over other embodiments. Although various aspects of the embodiments are shown in the drawings, the drawings are not necessarily drawn to scale unless otherwise noted.

[0085] In addition, the technical features involved in different embodiments of the present application described below can be combined with each other as long as they do not conflict with each other.

[0086] like Figure 7 As shown, the present application provides a hydrogen production and purification system, comprising:

[0087] Composite heat exchanger 100,

[0088] Deaerator 200,

[0089] The first condenser 300,

[0090] Adsorption unit 400, and

[0091] Finished product hydrogen collection unit 500.

[0092] The present application also provides a hydrogen production and purification method, which is performed in the above-mentioned hydrogen production and purification system, and comprises:

[0093] S1 introduces the raw hydrogen flow into the first heat exchange zone of the composite heat exchanger through the air inlet, and after condensation treatment in the first heat exchange zone, the obtained first zone hydrogen flow is discharged from the air outlet; and the first zone hydrogen flow enters the second heat exchange zone of the composite heat exchanger through the transfer inlet, exchanges heat with the heat exchange hydrogen flow in the second heat exchange zone, and the obtained second zone hydrogen flow is discharged from the hydrogen flow outlet of the heat exchange bin;

[0094] S2 allows the second zone hydrogen gas flow to enter a deaerator, where it is deoxygenated;

[0095] S3 allows the deaerator hydrogen flow from the deaerator to enter the first condenser for a first condensation process;

[0096] S4 allows the first condenser hydrogen gas stream from the first condenser to be transported to an adsorption unit for treatment;

[0097] S5 enables the finished hydrogen gas stream treated by the adsorption unit to be transported to a finished hydrogen collection unit;

[0098] The treatment in the adsorption unit includes:

[0099] S41 allows the first condenser hydrogen flow from the first condenser to be transported to the first adsorption tower for first adsorption;

[0100] S42 allows at least a portion of the first adsorption tower hydrogen flow from the first adsorption tower to flow through the first pass of the gas heat exchanger, and allows the heat-exchanged hydrogen flow from the second heat exchange zone to flow through the second pass of the gas heat exchanger, so that the first adsorption tower hydrogen flow and the heat-exchanged hydrogen flow are heat exchanged in the gas heat exchanger;

[0101] S43 transports the first pass output hydrogen flow from the gas heat exchanger to the second adsorption tower to regenerate the second adsorption tower; the regenerated hydrogen flow discharged from the second adsorption tower is input into the second heat exchange zone through the heat exchange hydrogen flow inlet as the heat exchange hydrogen flow, and the heat exchanged hydrogen flow is discharged from the heat exchange hydrogen flow outlet;

[0102] S44 transports the second-pass output hydrogen gas flow from the gas heat exchanger to the second condenser for second condensation treatment; transports the second condenser hydrogen gas flow cooled by the second condenser to the third adsorption tower for second adsorption treatment to obtain the finished hydrogen gas flow.

[0103] The following describes the various parts of the hydrogen production and purification system and the various steps of the hydrogen production and purification method. It should be noted that the description of the hydrogen production and purification system is also applicable to the hydrogen production and purification method when there is no contradiction, and vice versa.

[0104] The hydrogen production and purification system of the present application includes a composite heat exchanger 100. Figure 1 and Figure 2 The composite heat exchanger 100 includes a first heat exchange zone, which includes a condensing bin 1, a ventilation pipe 2 and a condensing pipe 3, wherein a closed cavity is provided inside the condensing bin 1. The closed cavity here means that a relatively independent space is formed inside. In actual use, the transfer of internal and external substances can be carried out through a closable channel such as an opening.

[0105] Combined with reference Figure 2 and 3 The ventilation pipeline 2 is arranged in the above-mentioned closed cavity, and is used for circulating the gas to be condensed. In the embodiment of the present application, the gas to be condensed is taken as crude hydrogen (i.e., raw hydrogen flow). The ventilation pipeline 2 is provided with an air inlet 2a and an air outlet 2b, and the air inlet 2a and the air outlet 2b are both connected to the outer wall of the condensation bin 1. The air inlet 2a is connected to the previous hydrogen preparation system, and is used to introduce the raw hydrogen flow into the first heat exchange zone. The condensed gas (first zone hydrogen flow) is transported to the subsequent processing process through the air outlet 2b.

[0106] The condensation pipeline 3 is used for circulating condensation medium, such as low temperature water, liquid nitrogen, etc. The condensation pipeline 3 performs heat exchange with the ventilation pipeline 2 to realize the condensation of crude hydrogen therein. The condensation pipe is provided with an inlet and an outlet, and both are also connected to the outer wall of the condensation bin 1, and connected to an external storage device, etc., to form a loop of the condensation medium.

[0107] refer to Figure 3 , the gas passage formed by the ventilation pipe 2 in the condensation bin 1 includes a condensation section 21 and a liquid catching section 22. It should be noted that the gas passage formed by the ventilation pipe 2 in the condensation bin 1 can be a passage formed by the ventilation pipe 2 itself, or a passage formed by the ventilation pipe 2 and the condensation bin 1. Crude hydrogen is input into the above-mentioned gas passage from the air inlet 2a, flows through the above-mentioned condensation section 21 and the liquid catching section 22 in sequence, and is discharged from the air outlet 2b; a liquid catching member for assisting in collecting condensed water is provided in the liquid catching section 22, and the liquid catching section 22 is provided with a downward condensation port 2c for the discharge of condensed water. The condensation port 2c referred to here as facing downward does not limit its opening to a vertical direction, and it can also have a certain inclination angle. It only needs to ensure that it will not hinder the smooth discharge of condensed water in the liquid catching section 22. In the embodiment of the present application, the condensation port 2c facing vertically downward is used as an example for explanation.

[0108] Correspondingly, after the condensed water is discharged from the liquid-catching section 22, it accumulates at the bottom of the condensation bin 1. A drain port 11 is provided at the bottom of the condensation bin 1 for draining the condensed water. The drain port 11 is opened or closed as needed. After the condensed water accumulates to a certain amount, the condensed water is discharged for unified treatment. In other embodiments, a receiving container may be provided at the condensation port 2c of the liquid-catching section 22 for temporarily storing the generated condensed water, and a drain port 11 is provided at the bottom of the receiving container to transport the condensed water to the outside of the condensation bin 1.

[0109] By setting up the composite heat exchanger, before deoxygenating and purifying the hydrogen, the crude hydrogen is connected to the air inlet 2a, so that the crude hydrogen flows through the ventilation pipeline 2, and the condensing medium is introduced into the condensation pipeline 3, and the crude hydrogen is condensed so that the moisture and impurities therein are condensed and precipitated. After the moisture is removed, the crude hydrogen is introduced into the deaerator for oxidation reaction, which can reduce the problem of impurities in the crude hydrogen causing pollution to the catalyst, play a better protective role on the catalyst, and extend the service life of the catalyst.

[0110] refer to Figure 3 and Figure 4 , the condensation pipeline 3 is located in the condensation section 21 and is wrapped around the outer periphery of the liquid-catching section 22. In this way, in the actual process of condensing the crude hydrogen, the crude hydrogen flows through the condensation section 21 and the liquid-catching section 22 from the air inlet 2a in sequence and is discharged from the air outlet 2b; in the process of crude hydrogen being transmitted in the condensation section 21, the crude hydrogen continues to exchange heat with the condensation pipeline 3 arranged in the condensation section 21, thereby reducing the temperature of the crude hydrogen, and the moisture and impurities therein are gradually condensed, and then transmitted to the liquid-catching section 22, so that the moisture and impurities cooled and condensed in the condensation section 21 are separated from the gas.

[0111] The above-mentioned coating setting method saves space compared to the structure in which the condensation section 21 and the liquid capture section 22 are arranged in the same set direction; and in the structure of the present application, the condensation pipeline 3 not only cools the crude hydrogen in the condensation section 21, but also can continuously cool the crude hydrogen transmitted in the liquid capture section 22, so that the crude hydrogen can always maintain a low temperature during the transmission process in the condensation bin 1; in contrast, the structure in the prior art requires that the condensation pipeline 3 be set on the entire stroke of the ventilation pipeline 2, otherwise the condensation effect of the gas to be condensed will be reduced.

[0112] Specifically, the condensation bin 1 is a can-shaped container, the ventilation pipe 2 is located in the can-shaped container, and a ventilation gap is provided between the ventilation pipe 2 and the inner wall of the condensation bin 1; wherein, the ventilation gap is the above-mentioned condensation section 21, and the channel formed inside the ventilation pipe 2 is the above-mentioned liquid capture section 22.

[0113] Taking the vertical placement of the condensation bin 1 as an example, the air inlet 2a and the air outlet 2b are both located on the upper side of the condensation bin 1. During the transmission of the condensed gas in the ventilation pipe 2, it is first transmitted downward in the condensation section 21 and then transmitted upward in the liquid capture section 22.

[0114] refer to Figure 3 The ventilation pipeline 2 includes an inner tube 23 and an outer tube 24 sleeved outside the inner tube 23, wherein the cross section of the inner tube 23 is rectangular, the cross section of the outer tube 24 is circular, and both ends of the outer tube 24 are sealed structures, forming a cavity isolated from the outside between the inner tube 23 and the outer tube 24. Both ends of the inner tube 23 are open structures, forming a channel for gas circulation, wherein the opening of the inner tube 23 toward the lower end is the above-mentioned condensation port 2c, and the opening of the inner tube 23 toward the upper end is the gas outlet 2b; the condensation pipeline 3 is wrapped around and covered on the outside of the outer tube 24.

[0115] After the crude hydrogen is transported into the condensation chamber 1 , it is first transmitted downward in the condensation section 21 , and then transmitted from the lower end opening of the inner tube 23 to the interior of the inner tube 23 and the liquid capture section 22 .

[0116] In addition, setting the cross section of the inner tube 23 to a rectangular shape makes it easier to set the liquid-catching part inside it. Compared with setting the cross section of the inner tube 23 to a circular shape, the rectangular structure is more conducive to connecting the liquid-catching part with the inner tube 21, and reduces the limitation of the characteristics of the circular structure itself, resulting in the high requirement that the size of each part of the liquid-catching part needs to be adapted to the different parts of the circle, which reduces the difficulty of processing the liquid-catching part and is more conducive to ensuring the adaptability of the liquid-catching part to the inner tube 21. Setting the cross section of the outer tube 22 to a circular shape is more conducive to winding the condensation pipeline 3 around the outside thereof than a rectangular or other polygonal shape, and can increase the contact area between the condensation pipeline 3 and the outer tube, resulting in higher heat transfer efficiency.

[0117] In addition, combined with reference Figure 3 and Figure 4 The transmission direction of the condensing medium in the condensing pipeline 3 is opposite to the transmission direction of the crude hydrogen in the condensing section 21. Taking the downward transmission of the crude hydrogen in the condensing section 21 as an example, the condensing medium is transmitted upward in the condensing pipeline 3. It should be noted that the condensing pipeline 3 is coated on the outside of the inner tube 23, the condensing pipeline 3 is wound around the outside of the ventilation pipeline 2, and the condensing medium in the condensing pipeline 3 has a spiral upward trend.

[0118] On the one hand, the condensing medium is transmitted from bottom to top in the condensing pipeline 3, which can ensure that the condensing medium fills the internal space of the condensing pipeline 3, and the condensing efficiency is higher. On the other hand, the temperature of the crude hydrogen gradually decreases from top to bottom in the condensing section 21, and correspondingly, the temperature of the condensing medium also tends to gradually decrease from top to bottom in the condensing pipeline 3, so that a high heat exchange efficiency can be maintained between the condensing medium and the crude hydrogen in all flow paths, and the overall condensation efficiency of the crude hydrogen is higher.

[0119] refer to Figure 1 , multiple air inlets 2a are provided, and the multiple air inlets 2a are respectively connected to different crude hydrogen sources, and crude hydrogen from different sources is introduced into the ventilation pipeline 2. Exemplarily, in the actual production process, there are many different preparation methods for preparing hydrogen, such as alkaline water electrolysis technology, proton exchange membrane water electrolysis technology, anion exchange membrane water electrolysis technology, high-temperature solid oxide water electrolysis technology, etc. The hydrogen prepared by different preparation systems is respectively connected to different air inlets 2a, and is introduced into the condensation section 21 for heat exchange, and the crude hydrogen from different sources is mixed in the condensation section 21, which can play a good buffering role.

[0120] Exemplarily, the multiple air inlets 2a are evenly spaced, which is beneficial to improving the uniformity of mixing of the multiple raw hydrogen gas flows in the condensation section 21 .

[0121] It should be noted that in other schematic diagrams, only one of the air inlets 2a is shown as an example to avoid blocking or interfering with the structure to be displayed and affecting understanding.

[0122] refer to Figure 3 The liquid-catching member includes a plurality of baffles 4 arranged at intervals, the baffles 4 are of a reciprocating bending structure, and the baffles 4 are fixedly connected to the inner wall of the outer tube 24 to separate the liquid-catching section 22 into a plurality of baffle channels 4a extending in a serpentine shape.

[0123] When the crude hydrogen is transmitted in the baffle channel 4a, it will continuously impact the bent part of the baffle plate 4. After the hydrogen impacts the bent part, it will change direction and continue to be transported upward. After the condensed water and impurities carried by the hydrogen impact the bent part of the baffle plate 4, they will adhere to the baffle plate 4. With the continuous transportation of the crude hydrogen, the condensed water and impurities accumulated on the baffle plate 4 gradually increase, flow downward along the baffle plate 4 and drip from the condensation port 2c. Compared with the case where the crude hydrogen is directly transmitted upward, the efficiency of separating the condensed water and impurities from the hydrogen can be improved, that is, after the crude hydrogen is condensed, the efficiency of removing the condensed water and impurities is higher.

[0124] refer to Figure 5 , and combined with reference Figure 2 The composite heat exchanger also includes a second heat exchange zone, which includes a heat exchange bin 5. The heat exchange bin 5 is also a cavity structure with a cavity inside. The heat exchange bin is provided with a first channel and a second channel isolated from each other. The heat exchange bin 5 is provided with a transfer inlet 51, which is respectively connected to the heat exchange bin hydrogen gas outlet 52 and the gas outlet 2b. The heat exchange bin hydrogen gas outlet 52 is connected to the subsequent equipment for deoxygenating hydrogen. The first channel is connected to the transfer inlet 51 and the heat exchange bin hydrogen gas outlet 52, and is used to transport the first zone hydrogen gas discharged from the gas outlet 2b; the first zone hydrogen gas is transported from the transfer inlet 51 to the first channel, and is transmitted to the heat exchange bin hydrogen gas outlet 52 for discharge.

[0125] In addition, the heat exchange bin 5 is also connected with a heat exchange hydrogen flow inlet 53 and a heat exchange hydrogen flow outlet 54, both of which are connected to the second channel, and are used to transport the heat exchange hydrogen flow to the second heat exchange zone through the second channel, and output the heat exchanged hydrogen flow. The heat exchange hydrogen flow in the second channel exchanges heat with the first zone hydrogen flow in the first channel to achieve heating of the first zone hydrogen flow.

[0126] refer to Figure 5 , a heat exchange element is arranged in the heat exchange bin 5, and a gas channel is arranged inside the heat exchange element. For example, the heat exchange element is a heat exchange tube 6, and there are multiple heat exchange tubes 6. The multiple heat exchange tubes 6 are evenly arranged in an array in the heat exchange bin 5, and heat exchange gaps for medium circulation are arranged between adjacent heat exchange tubes 6, and between the heat exchange tubes 6 and the inside of the heat exchange bin 5. Specifically, the heat exchange bin 5 is also a can-shaped structure, and the multiple heat exchange tubes 6 extend along the transfer inlet 51 toward the heat exchange bin hydrogen gas outlet 52.

[0127] The gas channel inside the heat exchange tube 6 is the first channel, which is connected to the transfer inlet 51 and the heat exchange bin hydrogen flow outlet 52, and is used to transmit the hydrogen that has been condensed; the above-mentioned heat exchange gap is the second channel, and the heat exchange hydrogen flow inlet 53 and the heat exchange hydrogen flow outlet 54 are connected to the heat exchange gap, and the heat exchange hydrogen flow is transported therein to heat the hydrogen transmitted inside the heat exchange tube 6.

[0128] After the crude hydrogen is condensed, water and impurities are removed from it, and then it is passed into the heat exchange chamber 5. The hydrogen after condensation, dehydration and impurity removal is heated by the heat exchange hydrogen flow in the heat exchange chamber 5, so that the discharged hydrogen is at a higher temperature. The subsequent deoxygenation process is carried out to catalyze the reaction of oxygen. A higher temperature is conducive to increasing the oxygen reaction rate. By heating in the heat exchange chamber 5, it is beneficial to improve the subsequent deoxygenation efficiency.

[0129] In the hydrogen purification process of the present application, an adsorbent is needed to purify the hydrogen and adsorb some impurities in the hydrogen; as the amount of adsorbed impurities increases, the adsorption capacity of the adsorbent decreases, and it needs to be regenerated, that is, the adsorbent is heated to precipitate the adsorbed impurities, and the adsorbent is purged with a clean gas to take away the precipitated impurities, so that the adsorbent can be reused. In the present application, a regenerated hydrogen flow from a regenerated adsorption tower is used as a heat exchange hydrogen flow. Clean gas, such as hydrogen, will be heated to a higher temperature to purge the adsorbent and take away impurities. This part of the high-temperature gas is introduced into the composite heat exchanger as a heat exchange hydrogen flow, and the hydrogen after the condensation treatment can be heated, which not only increases the temperature of the hydrogen and improves the efficiency of subsequent deoxygenation, but also can make reasonable use of energy in other processes and alleviate the problem of energy waste.

[0130] During specific use, hydrogen is transmitted in the heat exchange tube 6, and during the process, heat is exchanged with the heat exchange hydrogen flow in the heat exchange gap, the hydrogen flow in the second heat exchange zone is heated, and the temperature of the hydrogen flow is increased to improve the deoxygenation efficiency in the subsequent deoxygenation process; and multiple heat exchange tubes 6 are evenly arranged in an array in the heat exchange bin 5, which has a better heating effect on the hydrogen flow, and the heating of each part of the hydrogen flow is more uniform.

[0131] In another embodiment, the heat exchange gap is a first channel, the transfer inlet 51 and the heat exchange bin hydrogen flow outlet 52 are connected to the heat exchange gap, and the first zone hydrogen flow that has been condensed is transmitted through the heat exchange gap; the gas channel inside the heat exchange tube 6 is a second channel, the heat exchange hydrogen flow inlet 53 and the heat exchange hydrogen flow outlet 54 are connected to multiple heat exchange tubes 6, and the heat exchange hydrogen flow is transported to the heat exchange tube 6 to heat the first zone hydrogen flow transmitted in the heat exchange gap.

[0132] In other embodiments, two groups of ventilation pipes may be provided in the heat exchange chamber 5, wherein the internal passage of one group of ventilation pipes is the first passage, which is connected to the transfer inlet 51 and the heat exchange chamber hydrogen gas outlet 52, and is used to transmit the first zone hydrogen gas flow after condensation treatment; the internal passage of the other group of ventilation pipes is the second passage, which is connected to the heat exchange hydrogen gas inlet 53 and the heat exchange hydrogen gas outlet 54, and is used to transmit the heat exchange hydrogen gas flow; the first zone hydrogen gas flow is heated by the heat exchange hydrogen gas flow. For the two groups of ventilation pipes, one group may be spirally wound around the outside of the other group to improve the heat exchange efficiency.

[0133] In addition, combined with reference Figure 1 and Figure 6 In actual design, the condensing bin 1 and the heat exchange bin 5 can be set as an integrated structure or a split structure according to actual needs. For example, when set as an integrated structure, the condensing bin 1 and the heat exchange bin 5 are directly fixedly connected, and a flange is set at one end where the condensing bin 1 and the heat exchange bin 5 are connected, so that the two can be directly fixedly connected, and the air outlet 2b and the transfer inlet 51 are directly connected to each other to achieve gas transportation, which can enhance the integrity of the composite heat exchanger. When set as a split structure, the condensing bin 1 and the heat exchange bin 5 are two independent structures, and the air outlet 2b and the transfer inlet 51 are connected by a pipeline to achieve gas transportation. In this way, the condensing bin 1 and the heat exchange bin 5 can be arranged more conveniently according to actual conditions, thereby improving the convenience of use.

[0134] In one embodiment, the inlet of the condenser tube of the composite heat exchanger is connected to the return pipe of the first condenser 300 and / or the second condenser 405 described below, so that the reflux cooling medium (e.g., low-temperature cooling water return water, the temperature is about 7°C) from the first condenser 300 and / or the second condenser 405 is used as the cooling medium in the condenser tube of the composite heat exchanger. Through the composite heat exchanger, before deoxygenation and purification of hydrogen, the crude hydrogen is connected to the air inlet 2a, so that the crude hydrogen flows through the ventilation line 2, and the condensation medium is introduced into the condensation line 3, and the crude hydrogen is condensed to condense the water therein, so that the water therein is condensed and precipitated, and after the water is removed, it is introduced into the subsequent deaerator for deoxygenation. In this way, the raw hydrogen gas flow can be cooled to reduce its water content, and at the same time, the gas heating energy during subsequent deoxygenation can be reduced (water molecules have a large specific heat capacity). Moreover, the raw hydrogen gas flow usually contains trace amounts of alkali, which will adhere to the catalyst surface during deoxygenation in the deaerator and cannot be removed, affecting the service life of the catalyst. Reducing the water molecule content of the raw hydrogen gas flow can reduce the alkali content and increase the service life of the catalyst.

[0135] In the present application, the heat exchange hydrogen flow used as the heat exchange medium in the second heat exchange zone comes from the hydrogen flow after regeneration and heating (about 250°C). It is used as the heat exchange medium to heat the first zone hydrogen flow that has been cooled in the first heat exchange zone, and then enters the deaerator 200 for deoxygenation treatment. This can make the temperature of the hydrogen flow entering the deaerator reach or approach the temperature required for deoxygenation treatment, thereby saving energy in the deoxygenation process and performing the first heat recovery on the regenerated hydrogen flow.

[0136] refer to Figure 7, the hydrogen production and purification system of the present application also includes a deaerator 200, which is connected to the hydrogen gas outlet of the heat exchange bin of the second heat exchange zone, so that the second zone hydrogen gas heated by the second heat exchange zone enters the deaerator 200 for deoxygenation treatment. The deaerator 200 can use a catalytic deoxidation method to remove impurity oxygen to purify hydrogen. The deaerator 200 is filled with a room temperature catalytic deoxidizer, and a small amount of oxygen in the hydrogen is combined with hydrogen to generate water after catalysis by the catalyst, so that the oxygen content is less than 5ppm. An electric heating element can be installed in the deaerator 2 to increase the temperature of the deaerator 200, so that the water generated by the reaction is taken out of the deaerator 200 in a gaseous form. As described above, by using the hydrogen gas (about 250°C) from the regenerated heating as a heat exchange medium to heat the first zone hydrogen gas that has been cooled in the first heat exchange zone in the second heat exchange zone, the temperature can reach (or approach) the temperature of the deoxygenation treatment, and enter the deaerator for hydrogen deoxygenation treatment. Therefore, the crude hydrogen does not need to be heated during the deaerator treatment stage, and the heating function in the deaerator does not need to be turned on (or can be turned on at low power), and the crude hydrogen can be kept in a suitable higher temperature range, improving efficiency, reducing the energy consumption of the deaerator, and saving energy. Therefore, by utilizing the hydrogen gas stream heated by the regeneration tower for energy reuse, the heating energy during deoxygenation can be saved and unnecessary energy loss in the hydrogen production process can be reduced. In one embodiment, the deaerator hydrogen gas stream discharged from the deaerator 200 is about 120°C. In order to further improve its purity, it can be treated in subsequent processes in subsequent devices to reduce its water content.

[0137] refer to Figure 7 The hydrogen production and purification system of the present application also includes a first condenser 300, which is connected to the hydrogen flow outlet of the deaerator 200, so that the deaerator hydrogen flow that has been deoxygenated by the deaerator enters the first condenser 300 for a first condensation treatment, cools the hydrogen, condenses and removes water, and the cooling water is regularly emptied. As mentioned above, the deaerator hydrogen flow is about 120°C, which can be reduced to about 20°C by the first condenser 300.

[0138] The first condenser 300 is connected to the cooling medium circulation unit 600, which is used to circulate the condensing medium in the first condenser 300. The condensing medium can circulate in the tube of the first condenser 300, and the hydrogen gas flows through the shell of the first condenser 300. The condensing medium circulation unit 600 includes a condensing medium water inlet tank 610 for conveying the condensing medium to the first condenser 300, and a condensing medium water return tank 620 for recovering the condensing medium from the first condenser 300. The condensing medium water return tank 620 also needs to be processed, cooled, and conveyed to the condensing medium water inlet tank 610, so as to realize the circulation of the condensing medium. The condensing medium can be low-temperature cooling water.

[0139] As mentioned above, in one embodiment, the inlet of the condensing tube of the composite heat exchanger is connected to the return pipe of the first condenser 300, so that the return cooling medium (e.g., low-temperature cooling water return water, temperature of about 7°C) from the first condenser 300 is used as the cooling medium in the condensing tube of the composite heat exchanger. At this time, the outlet of the condensing tube of the composite heat exchanger is connected to the condensing medium return tank 620 for recovering the condensing medium from the composite heat exchanger, thereby forming a circulation loop of the condensing medium.

[0140] refer to Figure 7 and Figure 8 The hydrogen production and purification system of the present application further includes an adsorption unit 400, which is used to process the first condenser hydrogen flow from the first condenser to obtain a finished hydrogen flow with a purity that meets the requirements. The adsorption unit 400 includes a gas heat exchanger 404 and a second condenser 405, as well as a first adsorption tower 401, a second adsorption tower 402 and a third adsorption tower 403.

[0141] The hydrogen gas inlet of the first adsorption tower 401 is connected to the hydrogen gas outlet of the first condenser 300, so as to transport the hydrogen gas of the first condenser to the first adsorption tower 401 for the first adsorption treatment. The low-temperature hydrogen gas coming out of the first condenser 300 enters the first adsorption tower 401 to adsorb water vapor and impurities. The low-temperature hydrogen gas coming out of the first adsorption tower 401 is controlled by a pneumatic valve, and a part of it becomes finished hydrogen gas and enters the filter 506, and the other part enters the gas heat exchanger 404 for heat exchange heating.

[0142] The gas heat exchanger 404 has two independent fluid passages, the shell side and the tube side, which can be used for two different fluids to pass through and for the two different fluids to exchange heat in the gas heat exchanger 404. In the following, when the first pass of the gas heat exchanger 404 is the shell side, the second pass is the tube side; when the second pass of the gas heat exchanger 404 is the shell side, the first pass is the tube side.

[0143] The first pass inlet of the gas heat exchanger 404 is connected to the hydrogen flow outlet of the first adsorption tower 401, so that the first adsorption tower hydrogen flow treated by the first adsorption tower 401 flows through the first pass of the gas heat exchanger 404; the second pass inlet of the gas heat exchanger 404 is connected to the heat exchange hydrogen flow inlet, so that the heat-exchanged hydrogen flow from the second heat exchange zone flows through the second pass of the gas heat exchanger 400; thus, the first adsorption tower hydrogen flow from the first adsorption tower 401 and the heat-exchanged hydrogen flow from the second heat exchange zone are heat exchanged in the gas heat exchanger 404.

[0144] The first pass outlet of the gas heat exchanger 404 is connected to the hydrogen flow inlet of the second adsorption tower 402, so that the first pass output hydrogen flow heated by the gas heat exchanger 404 is transported to the second adsorption tower 402 to regenerate the second adsorption tower. In this way, the temperature of the hydrogen flow entering the second adsorption tower 402 (regeneration tower) can be increased, and the hydrogen flow is further heated in the second adsorption tower 402 (regeneration tower) to regenerate the adsorbent in the tower (partial gas regeneration).

[0145] At the same time, the hydrogen flow outlet of the second adsorption tower 402 is connected to the heat exchange hydrogen flow inlet of the second heat exchange zone, so that the regenerated hydrogen flow discharged from the second adsorption tower flows through the second heat exchange zone and is used as the heat exchange hydrogen flow to heat the first zone hydrogen flow from the first heat exchange zone.

[0146] The second pass outlet of the gas heat exchanger 404 is connected to the hydrogen flow inlet of the second condenser 405, so that the second pass output hydrogen flow cooled by the gas heat exchanger is transported to the second condenser for second condensation treatment. Hydrogen is cooled and cooled in the second condenser 405, condensed and dehydrated, and the cooling water is regularly emptied. The second condenser 405 is also connected to the cooling medium circulation unit 600, which is used to circulate the condensing medium in the second condenser 405. The condensing medium can circulate in the tube of the second condenser 405, and the hydrogen flow flows through the shell of the second condenser 405. The condensing medium circulation unit 600 includes a condensing medium water inlet tank 610 for conveying the condensing medium to the second condenser 405 respectively, and a condensing medium water return tank 620 for recovering the condensing medium from the second condenser 405. It is also necessary to treat and cool the condensing medium water return tank 620, and transport it to the condensing medium water inlet tank 610, so as to realize the circulation of the condensing medium. The condensing medium can be low-temperature cooling water. As mentioned above, in one embodiment, the inlet of the condensing tube of the composite heat exchanger is connected to the return pipe of the second condenser 405, so that the return cooling medium (e.g., low-temperature cooling water return water, temperature of about 7°C) from the second condenser 405 is used as the cooling medium in the condensing tube of the composite heat exchanger. At this time, the outlet of the condensing tube of the composite heat exchanger is connected to the condensing medium return tank 620 for recovering the condensing medium from the composite heat exchanger, thereby forming a circulation loop of the condensing medium.

[0147] The hydrogen gas inlet of the third adsorption tower 403 is connected to the hydrogen gas outlet of the second condenser 405, and is used to transport the second condenser hydrogen gas cooled by the second condenser to the third adsorption tower 403 for second adsorption treatment. The hydrogen gas coming out of the second condenser 405 enters the third adsorption tower 403 to adsorb water vapor and impurities, and the hydrogen gas coming out of the third adsorption tower 403 enters the filter 506, and the hydrogen gas coming out of the filter is the finished hydrogen gas.

[0148] As described above, the regenerated hydrogen gas flow from the second adsorption tower 402 has a high temperature of about 250°C, which can well heat the first zone hydrogen gas flow from the first heat exchange zone to a temperature suitable for deoxygenation treatment; at this time, the regenerated hydrogen gas flow undergoes the first cooling and is discharged from the second heat exchange zone as the heat exchanged hydrogen gas flow. As described above, the heat exchanged hydrogen gas flow flows through the second pass of the gas heat exchanger 400, and the first adsorption tower hydrogen gas flow from the first adsorption tower 401 and the heat exchanged hydrogen gas flow from the second heat exchange zone are heat exchanged in the gas heat exchanger 404. At this time, the regenerated hydrogen gas flow undergoes the second cooling and then enters the second condenser 405. In this way, the temperature of the hydrogen gas flow entering the second adsorption tower 402 (regeneration tower) is increased, and then enters the second adsorption tower 402 (regeneration tower) for heating (first heating and then heating); after reducing the temperature of the hydrogen gas flow to be condensed and cooled, it enters the second condenser 405 to cool and condense the hydrogen gas flow that needs to be cooled (first cooling and then cooling), which is a two-way energy-saving effect, and the energy-saving effect is more significant.

[0149] It should be noted that a plurality of pneumatic three-way ball valves can be provided in the adsorption unit 400 as required, so that the first adsorption tower 401, the second adsorption tower 402 and the third adsorption tower 403 can be switched between the three states of working, regeneration and adsorption as required. In a switching cycle, the three adsorption towers are respectively in the working, regeneration and adsorption working states, and the hydrogen flow from the first condenser 300 first enters the adsorption tower in the working state, then enters the adsorption tower in the regeneration state, and finally enters the adsorption tower in the adsorption state. Thus, the three adsorption towers switch between the above three working states to achieve the continuity of the operation of the whole set of equipment.

[0150] refer to Figure 7 In one embodiment, the hydrogen production and purification system further includes a filter 506 for removing dust contained in the product hydrogen flow, and finally the qualified product hydrogen flow is transported to the finished hydrogen collection unit 700 or downstream equipment and devices.

[0151] refer to Figure 7 In one embodiment, the hydrogen production and purification system further includes a condensate tank 501,

[0152] The bottom of the composite heat exchanger 100 is provided with a drain outlet, and the drain outlet of the composite heat exchanger 100 is connected to the condensate tank 501; the first condenser 300 and the second condenser 405 are provided with drain outlets, and the drain outlets of the first condenser 300 and the second condenser 405 are connected to the condensate tank 501, which are used to discharge the condensed water in the composite heat exchanger 100 and the first condenser 300 and the second condenser 405.

[0153] refer to Figure 7, the hydrogen production and purification system also includes a drainage liquid seal 502, and the drainage liquid seal 502 is connected to the condensate tank 501. The drainage liquid seal 502 can be connected to the gas emptying device 505 to discharge the gas accumulated in the drainage liquid seal 502. The drainage liquid seal 502 can also discharge condensed water through the drainer 503, and replenish the liquid seal water through the replenisher 504. Through the above settings, the purification system of the present application can have the function of automatically and regularly removing condensed water and impurities, and also has a drainage liquid seal function. After the condensed water is discharged, the liquid seal water can be automatically replenished to prevent air from entering the drainage pipe of the condensate tank.

[0154] refer to Figure 7 The purification system is also provided with a purity meter 507 and a dew point meter 508, so as to realize the function of automatically detecting the dew point and purity of hydrogen.

[0155] refer to Figure 7 The purification system is also provided with an unqualified hydrogen exhaust device 509 for automatically screening and exhausting unqualified quality hydrogen.

[0156] In one embodiment, the hydrogen flows from different hydrogen production systems 101 can be connected to the composite heat exchanger 100 and the unqualified hydrogen exhaust device 509 through a three-way valve. When the hydrogen flow is detected to be unqualified, it is directly passed into the unqualified hydrogen exhaust device 509 for exhaust to avoid affecting the purification efficiency and results of the hybrid purification system. The different hydrogen production systems 101 can be one or more of an ALK hydrogen production system, a PEM hydrogen production system, an AEM hydrogen production system, and a SOEC hydrogen production system.

[0157] The hydrogen production and purification system of the present application may also include some other components, such as pipes and fittings for liquid connection, valves (such as three-way valves, etc.), gas-liquid separation equipment, pumping equipment, control instruments (such as pressure gauges), etc., which are not repeated here.

[0158] By using a composite heat exchanger to cool and condense the hydrogen coming from the separation system, the water and water vapor entrained in the hydrogen can be greatly reduced, thereby reducing the alkali content in the hydrogen; reducing the alkali content in the hydrogen can reduce the alkali contamination of the catalyst in the deaerator, and increase the service life of the deaerator (for ALK and AEM) by more than 1 times. At the same time, the composite heat exchanger can be used as a coupler for hydrogen / oxygen produced by a variety of different hydrogen production modes, with coupling, buffering and caching functions, and can couple ALK, PEM, AEM, SOEC and other hydrogen production methods.

[0159] In combination with the composite heat exchanger and the gas heat exchanger, the energy generated during the purification and regeneration process can be absorbed and utilized for a second time, which can reduce the overall energy consumption: the heating medium of the composite heat exchanger comes from the high-temperature regenerated hydrogen (about 250°C) of the regeneration tower, and the raw hydrogen after cooling and condensation is reheated in the composite heat exchanger, which can achieve a heat exchange efficiency of ≥70%, and the heated hydrogen reaches or approaches the temperature during deoxygenation, which can reduce the energy consumption of the deaerator during operation; at the same time, the high-temperature regenerated hydrogen itself needs to be cooled in the subsequent process, so after heat exchange and cooling in the composite heat exchanger, the heat exchange power required for condensation and cooling is reduced by about 70%, which is an indirect manifestation of high efficiency and energy saving; the gas after heat exchange of the high-temperature regenerated hydrogen in the gas heat exchanger enters the second heat exchange process, and the gas is reused for secondary energy, which further improves the energy utilization efficiency.

[0160] In the description of this application, it should be noted that, unless otherwise clearly specified and limited, the terms "install", "connect" and "connect" should be understood in a broad sense. For ordinary technicians in this field, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0161] The present application has been described above in conjunction with preferred embodiments, but these embodiments are only exemplary and serve only as an illustration. On this basis, various replacements and improvements may be made to the present application, all of which fall within the scope of protection of the present application.

Claims

1. A hydrogen production and purification system, comprising: A composite heat exchanger comprising: The first heat exchange zone comprises: A condensation chamber having a closed cavity inside; A ventilation pipeline is arranged in the closed cavity, and the ventilation pipeline is provided with an air inlet and an air outlet, and the air inlet and the air outlet are both connected to the outer wall of the condensation bin; wherein the air inlet is used to introduce the raw hydrogen flow into the first heat exchange zone, and the air outlet is used to discharge the first zone hydrogen flow that has been condensed in the first heat exchange zone; and The condensation pipe is used for the circulation of the condensation medium and for heat exchange with the ventilation pipe; The second heat exchange zone comprises: A heat exchange chamber, wherein a first channel and a second channel isolated from each other are provided in the heat exchange chamber; The heat exchange bin is provided with a transfer inlet and a heat exchange bin hydrogen gas outlet, and the transfer inlet is communicated with the gas outlet; the first channel is communicated with the transfer inlet and the heat exchange bin hydrogen gas outlet, so that the first zone hydrogen gas from the first heat exchange zone flows through the second heat exchange zone and then discharges from the composite heat exchanger through the heat exchange bin hydrogen gas outlet; The heat exchange bin is also provided with a heat exchange hydrogen gas inlet and a heat exchange hydrogen gas outlet, and the second channel is connected with the heat exchange hydrogen gas inlet and the heat exchange hydrogen gas outlet, and is used to transport the heat exchange hydrogen gas to the second heat exchange zone through the second channel, and output the heat exchanged hydrogen gas; A deaerator, which is connected to the hydrogen flow outlet of the heat exchange bin of the second heat exchange zone, so that the second zone hydrogen flow heated by the second heat exchange zone enters the deaerator for deoxygenation treatment; A first condenser, wherein the first condenser is connected to the hydrogen flow outlet of the deaerator, so that the deaerator hydrogen flow that has been deoxygenated by the deaerator enters the first condenser for a first condensation treatment; and An adsorption unit is used to process the first condenser hydrogen flow from the first condenser; the adsorption unit includes a gas heat exchanger and a second condenser, and a first adsorption tower, a second adsorption tower and a third adsorption tower; wherein, The hydrogen flow inlet of the first adsorption tower is connected to the hydrogen flow outlet of the first condenser, so as to transport the hydrogen flow of the first condenser to the first adsorption tower for the first adsorption treatment; The first pass inlet of the gas heat exchanger is connected to the hydrogen flow outlet of the first adsorption tower, so that the first adsorption tower hydrogen flow treated by the first adsorption tower flows through the first pass of the gas heat exchanger; the second pass inlet of the gas heat exchanger is connected to the heat exchange hydrogen flow inlet, so that the heat exchanged hydrogen flow from the second heat exchange zone flows through the second pass of the gas heat exchanger; thus, the first adsorption tower hydrogen flow from the first adsorption tower and the heat exchanged hydrogen flow from the second heat exchange zone perform heat exchange in the gas heat exchanger; The first pass outlet of the gas heat exchanger is connected to the hydrogen flow inlet of the second adsorption tower, so that the first pass output hydrogen flow heated by the gas heat exchanger is transported to the second adsorption tower to regenerate the second adsorption tower; The hydrogen gas outlet of the second adsorption tower is connected to the heat exchange hydrogen gas inlet of the second heat exchange zone, so that the regenerated hydrogen gas discharged from the second adsorption tower flows through the second heat exchange zone and is used as the heat exchange hydrogen gas to heat the first zone hydrogen gas from the first heat exchange zone; The second pass outlet of the gas heat exchanger is connected to the hydrogen flow inlet of the second condenser, so that the second pass output hydrogen flow cooled by the gas heat exchanger is transported to the second condenser for second condensation treatment; The hydrogen flow inlet of the third adsorption tower is connected to the hydrogen flow outlet of the second condenser, so as to transport the hydrogen flow of the second condenser cooled by the second condenser to the third adsorption tower for second adsorption treatment; and The finished hydrogen collection unit is used to collect the finished hydrogen flow processed by the adsorption unit.

2. The hydrogen production and purification system according to claim 1, characterized in that: The hydrogen gas outlet of the first adsorption tower, the hydrogen gas outlet of the second adsorption tower and the hydrogen gas outlet of the third adsorption tower are connected by an outlet pneumatic three-way valve; The hydrogen production and purification system further comprises a filter, which is connected to the outlet pneumatic three-way valve so that the finished hydrogen gas flow processed by the adsorption unit flows through the filter.

3. The hydrogen production and purification system according to claim 1, characterized in that: The hydrogen production and purification system also includes a condensing medium circulation unit, which is respectively connected to the condensing pipe of the first heat exchange zone, the first condenser and the second condenser, and is used to circulate the condensing medium in the first heat exchange zone, the first condenser and the second condenser.

4. The hydrogen production and purification system according to claim 1, characterized in that: The hydrogen production and purification system further includes a condensate tank, A drain port is provided at the bottom of the first heat exchange zone, and the drain port of the first heat exchange zone is connected to the condensate tank; The first condenser and the second condenser are provided with drain ports, and the drain ports of the first condenser and the second condenser are connected to the condensation tank; The hydrogen production and purification system further comprises a drainage liquid seal, and the drainage liquid seal is connected to the condensate tank.

5. The hydrogen production and purification system according to claim 1, characterized in that: The gas passage formed in the ventilation pipeline includes a condensation section and a liquid capture section, and the gas to be condensed flows from the air inlet, sequentially through the condensation section and the liquid capture section, and is discharged from the air outlet; The liquid collecting section is provided with a liquid collecting member for assisting in collecting condensed water; and The liquid-catching section is provided with a downward condensation port for discharging condensed water.

6. The hydrogen production and purification system according to claim 5, characterized in that: The condensation pipeline is located in the condensation section; the condensation pipeline is covered on the periphery of the liquid catching section.

7. The hydrogen production and purification system according to claim 6, characterized in that: A ventilation gap is provided between the ventilation pipeline and the interior of the condensation bin; the ventilation gap is the condensation section, the passage in the ventilation pipeline is the liquid catching section, and the end of the liquid catching section away from the air outlet is a condensation outlet for discharging condensed water.

8. The hydrogen production and purification system according to claim 7, characterized in that: The ventilation pipeline includes an inner tube and an outer tube sleeved outside the inner tube; The cross section of the inner tube is rectangular, and the cross section of the outer tube is circular; The condensation pipeline is coated on the outer tube.

9. The hydrogen production and purification system according to claim 5, characterized in that: The liquid-catching member comprises a plurality of baffles arranged at intervals; The plurality of baffles separate the liquid-catching section into a plurality of baffle channels extending in a serpentine shape.

10. The hydrogen production and purification system according to claim 9, characterized in that: The condensation section is directly connected to each of the baffle channels.

11. A method for producing and purifying hydrogen, carried out in the hydrogen producing and purifying system according to any one of claims 1 to 10, comprising: S1 introduces the raw hydrogen flow into the first heat exchange zone of the composite heat exchanger through the air inlet, and after condensation treatment in the first heat exchange zone, the obtained first zone hydrogen flow is discharged from the air outlet; and the first zone hydrogen flow enters the second heat exchange zone of the composite heat exchanger through the transfer inlet, exchanges heat with the heat exchange hydrogen flow in the second heat exchange zone, and the obtained second zone hydrogen flow is discharged from the hydrogen flow outlet of the heat exchange bin; S2 allows the second zone hydrogen gas flow to enter a deaerator, where it is deoxygenated; S3 allows the deaerator hydrogen flow from the deaerator to enter the first condenser for a first condensation process; S4 allows the first condenser hydrogen gas stream from the first condenser to be transported to an adsorption unit for treatment; S5 enables the finished hydrogen gas stream treated by the adsorption unit to be transported to a finished hydrogen collection unit; The treatment in the adsorption unit includes: S41 allows the first condenser hydrogen flow from the first condenser to be transported to the first adsorption tower for first adsorption; S42 allows at least a portion of the first adsorption tower hydrogen flow from the first adsorption tower to flow through the first pass of the gas heat exchanger, and allows the heat-exchanged hydrogen flow from the second heat exchange zone to flow through the second pass of the gas heat exchanger, so that the first adsorption tower hydrogen flow and the heat-exchanged hydrogen flow are heat exchanged in the gas heat exchanger; S43 transports the first pass output hydrogen flow from the gas heat exchanger to the second adsorption tower to regenerate the second adsorption tower; the regenerated hydrogen flow discharged from the second adsorption tower is input into the second heat exchange zone through the heat exchange hydrogen flow inlet as the heat exchange hydrogen flow, and the heat exchanged hydrogen flow is discharged from the heat exchange hydrogen flow outlet; and S44 transports the second-pass output hydrogen gas flow from the gas heat exchanger to the second condenser for second condensation treatment; transports the second condenser hydrogen gas flow cooled by the second condenser to the third adsorption tower for second adsorption treatment to obtain the finished hydrogen gas flow.

12. The method for producing and purifying hydrogen according to claim 11, characterized in that: The raw hydrogen gas stream comes from one or more hydrogen production systems, including one or more of an ALK hydrogen production system, a PEM hydrogen production system, an AEM hydrogen production system and a SOEC hydrogen production system.

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