CN115928103B - PEM hydrogen production and hydrogenation integrated system and hydrogen production control method - Google Patents
PEM hydrogen production and hydrogenation integrated system and hydrogen production control method Download PDFInfo
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
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- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
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Abstract
The invention relates to a PEM hydrogen production and hydrogenation integrated system and a hydrogen production control method, and belongs to the technical field of new energy. The PEM hydrogen production and hydrogenation integrated system comprises a hydrogen production system, a transportation system and a hydrogenation system; the hydrogen production system comprises hydrogen production equipment, low-pressure hydrogen buffer equipment, first hydrogen compression equipment and a hydrogen tube bundle container which are connected in sequence; the hydrogenation system comprises a second hydrogen compression device, a high-pressure hydrogen storage device and a hydrogenation device which are connected in sequence; the transportation system is used for conveying the hydrogen in the hydrogen tube bundle container to the second hydrogen compression device. The PEM hydrogen production and hydrogenation integrated system can realize the self-use of hydrogen, improve the production efficiency, ensure the electrolysis performance of the PEM electrolytic tank and prolong the service life of the PEM electrolytic tank.
Description
Technical Field
The invention relates to the technical field of new energy, in particular to a PEM hydrogen production and hydrogenation integrated system and a hydrogen production control method.
Background
In the context of the "two carbon target", the development of energy structures has been a trend toward green, low carbon, clean directions. Hydrogen is a new energy source which is widely paid attention to because of good combustion performance and no pollution of combustion products to the environment. For example, hydrogen is widely used in the field of new energy automobiles. In a new energy vehicle, hydrogen gas is used as a fuel for a hydrogen fuel cell to generate electric energy through chemical reaction.
The water electrolysis hydrogen production process refers to that water is dissociated under electrolysis to generate oxygen and hydrogen, and the oxygen and the hydrogen are separated out from an anode and a cathode of an electrolytic tank respectively. The current mature water electrolysis hydrogen production process comprises an alkaline water hydrogen production technology and a PEM (Chinese name: proton exchange membrane) hydrogen production technology. The alkaline water hydrogen production technology has low investment and running cost, but has the problems of alkali liquor loss, corrosion, high energy consumption and the like. PEM hydrogen production technology is a hotspot in hydrogen production research and is rapidly developed. Compared with the traditional hydrogen production technology, the PEM hydrogen production is used for carrying out electrolytic hydrogen production on water, is clean and safe, and can stably run for a long time; the proton exchange membrane adopted by the PEM system can effectively isolate hydrogen and oxygen generated at two sides of the anode and cathode, has better safety, and the generated hydrogen has high purity.
Disclosure of Invention
The invention aims at providing a PEM hydrogen production and hydrogenation integrated system.
The second object of the invention is to provide a hydrogen production control method based on a PEM hydrogen production and hydrogenation integrated system.
To achieve the above object:
the present invention provides in a first aspect a PEM hydrogen production and hydrogenation integrated system comprising a hydrogen production system, a transport system, and a hydrogenation system;
the hydrogen production system comprises hydrogen production equipment, low-pressure hydrogen buffer equipment, first hydrogen compression equipment and a hydrogen tube bundle container which are connected in sequence;
The hydrogen production equipment comprises a PEM electrolytic tank, a water supply device, a hydrogen treatment device and an oxygen treatment device; the water supply device is used for providing ultrapure water required by electrolysis for the PEM electrolytic tank; the hydrogen treatment device is used for treating a hydrogen product generated at the cathode end of the PEM electrolytic tank and conveying the treated hydrogen to the low-pressure hydrogen buffer device; the oxygen treatment device is used for treating an oxygen product generated at the anode end of the PEM electrolytic cell; the hydrogen production equipment also comprises a temperature detector and a controller; the temperature detector is used for detecting the water temperature of the PEM electrolytic tank; the control machine is used for adjusting the electrolysis current of the PEM electrolytic tank and the air outlet pressure of the cathode end according to the water temperature;
the hydrogenation system comprises a second hydrogen compression device, a high-pressure hydrogen storage device and a hydrogenation device which are connected in sequence;
the transportation system is used for conveying the hydrogen in the hydrogen tube bundle container to the second hydrogen compression device.
In some embodiments, the hydrogen treatment device comprises a hydrogen-water separator, a first shell-and-tube heat exchanger, a catalytic deoxidizing column and an adsorption drying column which are connected in sequence;
the air inlet end of the hydrogen-water separator is connected with the cathode end of the PEM electrolytic cell, and the air outlet end of the hydrogen-water separator is connected to the hydrogen inlet of the first shell-and-tube heat exchanger;
The hydrogen outlet of the first shell-and-tube heat exchanger is connected to the air inlet end of the catalytic deoxidization tower, the air outlet end of the catalytic deoxidization tower is connected to the air inlet end of the adsorption drying tower, and the air outlet end of the adsorption drying tower is connected to the air inlet end of the low-pressure hydrogen buffer device.
In some embodiments, the oxygen treatment device comprises an oxygen water separator and a second shell-and-tube heat exchanger; the air inlet end of the oxygen-water separator is connected with the anode end of the PEM electrolytic cell and is used for separating oxygen from water of the oxygen product;
the second shell-and-tube heat exchanger is used for cooling the oxygen separated by the oxygen-water separator, the oxygen inlet is connected with the air outlet end of the oxygen-water separator, and the oxygen outlet is used for discharging the cooled oxygen.
In some embodiments, the water supply device comprises an ultrapure water machine and a water storage tank; the ultra-pure water machine is used for preparing ultra-pure water required by the electrolysis of the PEM electrolytic tank; the water storage tank is respectively connected with the ultrapure water machine and the PEM electrolytic tank and is used for storing ultrapure water and delivering the ultrapure water to the PEM electrolytic tank.
In some embodiments, the body structural style of the first shell-and-tube heat exchanger is a seat style, the seat being a saddle seat;
The specification of the heat exchange tube of the first shell-and-tube heat exchanger is phi (15-20) x 2mm, the effective tube length is 1-2m, the number of heat exchange tube bundles is 70-80, and the heat exchange area is 6-8m2;
the nominal diameter of the hydrogen inlet of the first shell-and-tube heat exchanger is 30-40mm, and the nominal pressure is 3-5MPa; the nominal diameter of the hydrogen outlet of the first shell-and-tube heat exchanger is 30-40mm, and the nominal pressure is 3-5MPa.
In some embodiments, the body structural style of the second shell-and-tube heat exchanger is a seat style, the seat being a saddle seat;
the specification of the heat exchange tube of the second shell-and-tube heat exchanger is phi (15-20) x 2mm, the effective tube length is 1-2m, the number of heat exchange tube bundles is 110-120, and the heat exchange area is 9-10m 2 ；
The nominal diameter of the oxygen inlet of the second shell-and-tube heat exchanger is 40-50mm, and the nominal pressure is 4-6MPa; the nominal diameter of the oxygen outlet of the second shell-and-tube heat exchanger is 40-45mm, and the nominal pressure is 4-5MPa.
In some embodiments, the water storage tank is provided with a water level detector for detecting the water level of ultrapure water in the water storage tank.
In some embodiments, the hydrogenation apparatus comprises a hydrogenation machine having a maximum operating pressure of 45MPa or less.
In some embodiments, the transport system is a hydrogen transport pipe network or a hydrogen bundle vehicle.
The present invention provides in a second aspect a hydrogen production control method based on the PEM hydrogen production hydrogenation integrated system provided in the first aspect,
when the water temperature is less than 30 ℃, the control machine adjusts the PEM electrolytic tank to increase the electrolytic current according to a first speed, and finally stabilizes the electrolytic current at 1000-1500A, and meanwhile, the air outlet pressure of the cathode end is gradually increased, and finally stabilizes the electrolytic current at 1-1.5MPa;
when the water temperature is 30-60 ℃, the control machine adjusts the PEM electrolytic tank to increase the electrolytic current according to a second speed, and finally stabilizes at 2000-2500A, and meanwhile, the air outlet pressure of the cathode end is gradually increased, and finally stabilizes at 1-1.5MPa;
when the water temperature is higher than 60 ℃, the controller adjusts the PEM electrolytic cell to increase the electrolytic current according to a third speed, finally stabilizes at 3000-3750A, and simultaneously sets the air outlet pressure of the cathode end to 1-1.5MPa.
In some embodiments, the first speed is 100-200A/min;
the second speed is 200-300A/min;
the third speed is 500-600A/min.
In some embodiments, when the water temperature is less than 30 ℃, the controller sequentially increases the outlet pressure of the cathode end to a first pressure, a second pressure and a third pressure, and finally stabilizes at 1-1.5MPa; wherein the first pressure is 0.2-0.3MPa, the second pressure is 0.4-0.5MPa, and the third pressure is 0.6-0.7MPa;
When the water temperature is 30-60 ℃, the control machine sequentially increases the air outlet pressure of the cathode end to fourth pressure, fifth pressure and sixth pressure, and finally, the air outlet pressure is stabilized at 1-1.5MPa; wherein the fourth pressure is 0.4-0.5MPa, the fifth pressure is 0.6-0.7MPa, and the sixth pressure is 0.8-0.9MPa.
In some embodiments, after electrolysis is complete, the controller reduces the electrolysis current of the PEM electrolyzer to 0 at a fourth rate; the fourth speed is 10-20A/s.
Advantageous effects
The technical scheme of the invention has the following advantages:
the PEM hydrogen production and hydrogenation integrated system provided by the invention can realize spontaneous hydrogen self-use, and has strong replicable popularization value.
The PEM hydrogen production and hydrogenation integrated system provided by the invention comprises various hydrogen storage devices, and the different hydrogen storage devices ensure the safe storage requirements and the safe and convenient transportation requirements of hydrogen at different stages, and also expand the maximum hydrogen storage amount of the system.
The hydrogen production control method provided by the invention has the following advantages that the current and the operation pressure of the hydrogen outlet end are adaptively adjusted based on the water temperature: the electrolysis is carried out by adopting different electrolysis currents according to the water temperature, so that the electric energy is not wasted, the electric energy is fully utilized at the corresponding electrolysis temperature, the hydrogen production is increased step by step, the production efficiency is improved, and the electricity utilization safety is ensured; adjusting the air outlet pressure according to the water temperature, ensuring that the operation pressure of the hydrogen air outlet end is adapted to the hydrogen production efficiency, and ensuring the production safety; different electrolysis currents are adopted for electrolysis according to the water temperature, and meanwhile, the current is increased according to the corresponding speed, so that the electrolysis performance of the PEM electrolytic tank is ensured, the PEM electrolytic tank can be protected, and the service life of the PEM electrolytic tank is prolonged.
The control machine is adopted to reduce the current to 0 according to a certain speed after the electrolysis is completed, so that the electrolysis performance of the PEM electrolytic cell is ensured, and the service life of the PEM electrolytic cell can be prolonged.
The water outlet ends of the hydrogen-water separator and the oxygen-water separator in the PEM hydrogen production and hydrogenation integrated system provided by the invention can be connected to the water storage tank in the water supply device, so that the recycling of ultrapure water is realized.
Drawings
FIG. 1 is a schematic diagram of a hydrogen production system in a PEM hydrogen production and hydrogenation integrated system provided by the invention;
fig. 2 is a schematic structural diagram of a hydrogenation system in a PEM hydrogen production and hydrogenation integrated system provided by the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the technical solutions of the present invention will be clearly and completely described below in connection with the embodiments of the present invention. It will be apparent that the described embodiments are some, but not all, embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
The invention provides a PEM hydrogen production and hydrogenation integrated system, referring to fig. 1 and 2, comprising a hydrogen production system, a transportation system and a hydrogenation system;
The hydrogen production system comprises hydrogen production equipment, low-pressure hydrogen buffer equipment 105, first hydrogen compression equipment 106 and a hydrogen tube bundle container 107 which are connected in sequence (such as through pipelines); the hydrogen production equipment comprises a PEM electrolytic tank 101, a water supply device 102, a hydrogen treatment device 103 and an oxygen treatment device 104; the water supply device 102 is used for providing ultrapure water required for electrolysis for the PEM electrolytic tank 101; the hydrogen treatment device 103 is used for treating a hydrogen product generated at the cathode end of the PEM electrolyzer 101 and delivering the treated hydrogen to the low-pressure hydrogen buffer device 105; the oxygen treatment device 104 is used for treating oxygen products generated at the anode end of the PEM electrolyzer 101;
the hydrogenation system comprises a second hydrogen compression device 201, a high-pressure hydrogen storage device 202 and a hydrogenation device 203 which are connected in sequence (such as through a pipeline connection);
the transport system is used to transport hydrogen within the hydrogen tube bundle container 107 to the second hydrogen compression device 201.
The water supply device 102 in the PEM hydrogen production and hydrogenation integrated system provided by the invention prepares a water source (such as tap water) into ultrapure water for the PEM electrolytic tank 101 to prepare hydrogen. The hydrogen product produced in PEM electrolyzer 101 is processed by hydrogen treatment device 103 to produce usable hydrogen which is transported to low pressure hydrogen buffer device 105 for storage, then compressed by first hydrogen compression device 106, and the compressed hydrogen is transported to hydrogen bundle container 107 for storage. The hydrogen is then transported to the hydrogenation system for use by means of a transport system. The second hydrogen compression device 201 of the hydrogenation system compresses the hydrogen transported by the transportation system again, then the hydrogen is transported to the high-pressure hydrogen storage device 202 for storage, and the hydrogen stored by the high-pressure hydrogen storage device 202 is transported to the hydrogenation device 203 for use.
The PEM hydrogen production and hydrogenation integrated system provided by the invention can realize spontaneous hydrogen self-use, and has strong replicable popularization value.
The PEM hydrogen production and hydrogenation integrated system provided by the invention comprises various hydrogen storage devices, and the different hydrogen storage devices ensure the safe storage requirements and the safe and convenient transportation requirements of hydrogen at different stages, and also expand the maximum hydrogen storage amount of the system.
It should be noted that:
the term "low pressure" in the low pressure hydrogen buffer device 105 means that the operating pressure is 3MPa or less. The low pressure hydrogen buffering device 105 may be an existing device meeting the low pressure requirements described above, for example, may be a low pressure hydrogen buffer tank operating at 3MPa.
The term "high pressure" in the high-pressure hydrogen storage device 202 means that the operating pressure is 45MPa or less. The high-pressure hydrogen storage device 202 may be an existing device meeting the high-pressure requirements described above, and may be, for example, a high-pressure hydrogen cylinder or a high-pressure hydrogen cylinder group having an operating pressure of 45MPa.
The hydrogen bundle container 107 is a well-defined term in the industry, and is a prior art device and is not described in detail herein.
Ultrapure water is a term of art-understood meaning and is not described in detail herein.
In some preferred embodiments, the transportation system is a hydrogen transportation pipe network or a hydrogen pipe bundle vehicle, and the transportation system realizes pipeline transportation or mobile transportation of hydrogen.
In some preferred embodiments, the hydrogen plant further comprises a temperature detector and a controller; the temperature detector is used for detecting the water temperature of the PEM electrolytic cell 101; the control unit is used for adjusting the electrolysis current of the PEM electrolytic cell 101 and the cathode-side air outlet pressure according to the water temperature as follows:
when the water temperature is less than 30 ℃, the control machine adjusts the PEM electrolytic tank to increase the electrolytic current according to a first speed, and finally stabilizes the electrolytic current at 1000-1500A, and meanwhile, the air outlet pressure of the cathode end is gradually increased, and finally stabilizes the electrolytic current at 1-1.5MPa;
when the water temperature is 30-60 ℃, the control machine adjusts the PEM electrolytic tank 101 to increase the electrolytic current according to a second speed, and finally stabilizes at 2000-2500A, and meanwhile, the air outlet pressure of the cathode end is gradually increased, and finally stabilizes at 1-1.5MPa;
when the water temperature is higher than 60 ℃, the controller adjusts the PEM electrolytic cell 101 to increase the electrolytic current according to the third speed, finally stabilizing at 3000-3750A, and setting the air outlet pressure of the cathode end to 1-1.5MPa.
In PEM electrolytic hydrogen production, especially in the case of industrial mass production, how to increase production efficiency and to compromise production safety is a production difficulty that needs to be overcome. The hydrogen production equipment provided by the invention is used for adaptively adjusting the current and the operating pressure of the hydrogen outlet end based on the water temperature. For electrolysis current, a three-stage adjustment is made based on water temperature. When the water temperature is less than 30 ℃, the current is not too high, and the current is not increased too fast, preferably the current is increased according to a slower speed, and finally the current is stabilized at 1000-1500A (for example, 1000A, 1100A, 1200A, 1300A, 1400A and 1500A). Increasing the current at a suitable rate for this temperature phase and eventually stabilizing at 2000-2500A (e.g., 2000A, 2100A, 2200A, 2300A, 2400A, 2500A) when the water temperature is 30-60 ℃; when the water temperature is > 60 ℃, the current is increased at a faster rate and eventually stabilizes at 3000-3750A (e.g., 3000A, 3100A, 3200A, 3300A, 3400A, 3500A, 3600A, 3700A, 3750A may be possible). For the gas outlet pressure at the cathode end of the PEM electrolyzer 101, it is preferable to step up at a specific rate when the water temperature is < 30 c and eventually stabilize it at 1-1.5MPa (which may be, for example, 1MPa, 1.1MPa, 1.2MPa, 1.3MPa, 1.4MPa, 1.5 MPa); when the water temperature is 30-60 ℃, gradually increasing according to a specific speed, and finally stabilizing at 1-1.5MPa; when the water temperature is more than 60 ℃, the air outlet pressure is directly set to be 1-1.5MPa (for example, 1MPa, 1.1MPa, 1.2MPa, 1.3MPa, 1.4MPa and 1.5MPa can be adopted).
The technical scheme has the following advantages:
(1) the three-section electrolysis current is adopted for electrolysis according to the water temperature, so that electric energy is not wasted, the electric energy is fully utilized at the corresponding electrolysis temperature, the hydrogen production amount is increased step by step, the production efficiency is improved, and meanwhile, the electricity utilization safety is ensured.
(2) And the air outlet pressure is regulated according to the water temperature, so that the operation pressure of the hydrogen air outlet end is matched with the hydrogen production efficiency, and the production safety is ensured.
(3) Different electrolysis currents are adopted for electrolysis according to the water temperature, and meanwhile, the current is increased according to the corresponding speed, so that the electrolysis performance of the PEM electrolysis cell 101 is ensured, the PEM electrolysis cell 101 can be protected, and the service life of the PEM electrolysis cell 101 is prolonged.
In some preferred embodiments, the first speed is 100-200A/min (A is the current unit, an, the same applies below), for example, 100A/min, 110A/min, 120A/min, 130A/min, 140A/min, 150A/min, 160A/min, 170A/min, 180A/min, 190A/min, 200A/min.
The second speed is 200-300A/min, for example, 200A/min, 210A/min, 220A/min, 230A/min, 240A/min, 250A/min, 260A/min, 270A/min, 280A/min, 290A/min, 300A/min, and most preferably 250A/min.
In some preferred embodiments, the third speed is 500-600A/min, e.g., 500A/min, 510A/min, 520A/min, 530A/min, 540A/min, 550A/min, 560A/min, 570A/min, 580A/min, 590A/min, 600A/min.
In some preferred embodiments, when the water temperature is less than 30 ℃, the controller increases the outlet pressure of the cathode end to a first pressure, a second pressure and a third pressure in sequence, and finally stabilizes at 1-1.5MPa; wherein the first pressure is 0.2-0.3MPa, the second pressure is 0.4-0.5MPa, and the third pressure is 0.6-0.7MPa.
In some preferred embodiments, when the water temperature is 30-60 ℃, the controller increases the outlet pressure of the cathode end to fourth pressure, fifth pressure and sixth pressure in sequence, and finally stabilizes at 1-1.5MPa; wherein the fourth pressure is 0.4-0.5MPa, the fifth pressure is 0.6-0.7MPa, and the sixth pressure is 0.8-0.9MPa.
In some preferred embodiments, the controller is further configured to: after the electrolysis is completed, the electrolysis current of the PEM electrolysis cell 101 is reduced to 0 according to a fourth speed; the fourth speed is 10-20A/s, and may be, for example, 10A/s, 11A/s, 12A/s, 13A/s, 14A/s, 15A/s, 16A/s, 17A/s, 18A/s, 19A/s, 20A/s. The controller is used to reduce the current to 0 at a certain speed after the electrolysis is completed, so as to ensure the electrolysis performance of the PEM electrolytic cell 101 and prolong the service life of the PEM electrolytic cell 101.
In some preferred embodiments, the hydrogen treatment apparatus 103 comprises a hydrogen-water separator, a first shell-and-tube heat exchanger, a catalytic deoxygenation column, and an adsorption drying column connected in sequence (e.g., via tubing);
wherein the gas inlet end of the hydrogen-water separator is connected with the cathode end of the PEM electrolytic cell 101, and the gas outlet end is connected to the hydrogen inlet of the first shell-and-tube heat exchanger;
the hydrogen outlet of the first shell-and-tube heat exchanger is connected to the air inlet end of the catalytic deoxidizing tower, the air outlet end of the catalytic deoxidizing tower is connected to the air inlet end of the adsorption drying tower, and the air outlet end of the adsorption drying tower is connected to the air inlet end of the low-pressure hydrogen buffer device 105.
The hydrogen product generated by electrolysis firstly enters a hydrogen-water separator, the hydrogen-water separator is used for processing the hydrogen product, hydrogen and ultrapure water in the hydrogen product are subjected to gas-liquid separation in the hydrogen-water separator, then enter a first shell-and-tube heat exchanger for condensation, saturated steam contained in the hydrogen is condensed, then enter a catalytic deoxidizing tower for deoxidizing treatment, trace oxygen contained in the hydrogen is removed, the purity of the hydrogen and the oxygen index in the hydrogen are ensured, and finally enter an adsorption drying tower for drying treatment, so that the hydrogen with high purity is obtained.
The water separated by the hydrogen-water separator contains hydrogen, and thus in some preferred embodiments, the hydrogen treatment apparatus 103 provided by the present invention further includes a second hydrogen-water separator for performing gas-liquid separation of the water of the above hydrogen-water separator (which may be named as a first hydrogen-water separator) to remove a trace amount of hydrogen dissolved in the water.
In some preferred embodiments, the water outlet ends of the first and second hydrogen-water separators are connected to the water supply 102 to achieve recycling of ultrapure water.
The first hydrogen-water separator, the second hydrogen-water separator, the catalytic deoxidizing column, and the adsorption drying column are all existing devices, and the present invention is not described in detail herein.
In some preferred embodiments, the body structural form of the first shell-and-tube heat exchanger is a saddle form, the saddle being a saddle; the specification of the heat exchange tube of the first shell-and-tube heat exchanger is phi (15-20) x 2mm, the effective tube length is 1-2m, the number of heat exchange tube bundles is 70-80, and the heat exchange area is 6-8m 2 The method comprises the steps of carrying out a first treatment on the surface of the The nominal diameter of the hydrogen inlet of the first shell-and-tube heat exchanger is 30-40mm, and the nominal pressure is 3-5MPa; the nominal diameter of the hydrogen outlet of the first shell-and-tube heat exchanger is 30-40mm, and the nominal pressure is 3-5MPa.
The first shell-and-tube heat exchanger is a dividing wall type heat exchanger taking the wall surface of a tube bundle enclosed in a shell as a heat transfer surface, has a simple structure and a wider flow section, can be used at high temperature and high pressure, and is used for cooling hydrogen generated by electrolysis in a megawatt water electrolysis hydrogen production system, so that the hydrogen can be sufficiently cooled before purification.
The first shell-and-tube heat exchanger meets the design standards of GB/T150-2011, GB/T151-2014 and TSG21-2016 pressure vessels.
The main body structure of the first shell-and-tube heat exchanger is in a support type, the support is a saddle support, the main body material can be 316L stainless steel, and the saddle support material can be carbon steel; during installation, horizontal installation can be adopted, and installation feet can be made.
The shell side medium of the first shell-and-tube heat exchanger can be ethylene glycol solution, the tube side medium can be hydrogen, and the parameters are preferably as follows: the specification of the heat exchange tube is phi (15-20) x 2mm, the effective tube length is 1-2m, the number of heat exchange tube bundles is 70-80, and the heat exchange area is 6-8m 2 . In some preferred embodiments, the oxygen treatment device 104 comprises an oxygen water separator and a second shell-and-tube heat exchanger; the inlet end of the oxygen-water separator is connected to the anode end of the PEM electrolyzer 101 for oxygen production of the oxygen gas Separating water; the second shell-and-tube heat exchanger is used for cooling the oxygen separated by the oxygen-water separator, the oxygen inlet is connected with the air outlet end of the oxygen-water separator, and the oxygen outlet is used for discharging the cooled oxygen.
In some preferred embodiments, the outlet end of the oxygen-water separator is connected to the water supply 102 to enable the recycling of ultrapure water.
In some preferred embodiments, the body structural form of the second shell-and-tube heat exchanger is a saddle form, the saddle being a saddle; the specification of the heat exchange tube of the second shell-and-tube heat exchanger is phi (15-20) x 2mm, the effective tube length is 1-2m, the number of heat exchange tube bundles is 110-120, and the heat exchange area is 9-10m 2 The method comprises the steps of carrying out a first treatment on the surface of the The nominal diameter of the oxygen inlet of the second shell-and-tube heat exchanger is 40-50mm, and the nominal pressure is 4-6MPa; the nominal diameter of the oxygen outlet of the second shell-and-tube heat exchanger is 40-45mm, and the nominal pressure is 4-5MPa.
The second shell-and-tube heat exchanger is a dividing wall type heat exchanger taking the wall surface of a tube bundle enclosed in a shell as a heat transfer surface, is suitable for high-temperature and high-pressure environments, and can be used for cooling oxygen generated by electrolysis in a megawatt water electrolysis hydrogen production system, so that the oxygen can be sufficiently cooled before entering an oxygen-water separator.
The second shell-and-tube heat exchanger meets the design standards of GB/T150-2011, GB/T151-2014 and TSG21-2016 pressure vessels.
The main body structure of the second shell-and-tube heat exchanger is in a support type, the support is a saddle support, the main body material can be 316L stainless steel, and the saddle support material can be carbon steel; during installation, horizontal installation can be adopted, and installation feet can be made.
The shell side medium of the first shell-and-tube heat exchanger can be ethylene glycol solution, the tube side medium can be oxygen, and the parameters are preferably as follows: the specification of the heat exchange tube is phi (15-20) x 2mm, the effective tube length is 1-2m, the number of the heat exchange tube bundles is 110-120, and the heat exchange area is 9-10m 2 。
In some preferred embodiments, the water supply 102 comprises an ultrapure water machine and a water storage tank; the ultrapure water machine is used for preparing ultrapure water required by electrolysis of the PEM electrolytic tank 101, the water inlet end is connected with a water source (such as a municipal water supply pipeline), and the water outlet end is connected with the water inlet end of the water storage tank; the water storage tank is respectively connected with the ultrapure water machine and the PEM electrolytic tank 101, and is used for storing ultrapure water and delivering the ultrapure water to the PEM electrolytic tank 101, and it can be confirmed that the water inlet end of the water storage tank is connected with the water outlet end of the ultrapure water machine, and the water outlet end of the water storage tank is connected with the water inlet end of the PEM electrolytic tank 101.
In some preferred embodiments, the water outlet ends of the first hydrogen-water separator, the second hydrogen-water separator and the oxygen-water separator are all connected to the water storage tank, so that the recovery and utilization of the ultrapure water are realized. It can be determined that the water outlet ends of the first hydrogen-water separator, the second hydrogen-water separator and the oxygen-water separator are all connected to the water inlet end of the water storage tank.
In some preferred embodiments, the water storage tank is provided with a water level detector for detecting the water level of ultrapure water in the water storage tank.
In some preferred embodiments, the hydrogenation apparatus 203 comprises a hydrogenation machine having a maximum operating pressure of 45MPa or less.
Example 1
A PEM hydrogen production and hydrogenation integrated system comprises a hydrogen production system, a transportation system and a hydrogenation system;
the hydrogen production system comprises hydrogen production equipment and low-pressure hydrogen buffer equipment (10 m is adopted 3 The low-pressure hydrogen buffer tank of (1) is operated under 3MPa, and the maximum hydrogen storage amount is 25 kg), a first hydrogen compression device (adopting an air compressor) and a hydrogen tube bundle container (adopting a hydrogen tube bundle container with the operating pressure of 20MPa and the maximum hydrogen storage amount of 133 kg);
The hydrogen production equipment comprises a PEM electrolytic tank, a water supply device, a hydrogen treatment device and an oxygen treatment device; the water supply device is used for providing ultrapure water required by electrolysis for the PEM electrolytic tank; the hydrogen treatment device is used for treating a hydrogen product generated at the cathode end of the PEM electrolytic tank and conveying the treated hydrogen to the low-pressure hydrogen buffer device; the oxygen treatment device is used for treating an oxygen product generated at the anode end of the PEM electrolytic cell;
the hydrogenation system comprises a second hydrogen compression device (adopting an air compressor), a high-pressure hydrogen storage device (adopting a high-pressure hydrogen cylinder group with the operating pressure of 45MPa and the maximum hydrogen storage amount of 173 kg) and a hydrogenation device which are connected in sequence; the total stored hydrogen amount of the PEM hydrogen production and hydrogenation integrated system can reach 331kg at maximum;
the transportation system is a hydrogen tube bundle vehicle and is used for conveying hydrogen in the hydrogen tube bundle container to the second hydrogen compression equipment.
The hydrogen production equipment also comprises a temperature detector and a controller; the temperature detector is used for detecting the water temperature of the PEM electrolytic tank; the control machine is used for adjusting the electrolysis current of the PEM electrolytic tank and the air outlet pressure of the cathode end according to the water temperature as follows:
When the water temperature is less than 30 ℃, the controller adjusts the PEM electrolytic tank to increase the electrolytic current according to a first speed, so that the electrolytic current is finally stabilized at 1000A, and meanwhile, the air outlet pressure at the cathode end is gradually increased, so that the electrolytic current is finally stabilized at 1MPa;
when the water temperature is 30-60 ℃, the control machine adjusts the PEM electrolytic tank to increase the electrolytic current according to a second speed, so that the electrolytic current is finally stabilized at 2000A, and meanwhile, the air outlet pressure of the cathode end is gradually increased, so that the electrolytic current is finally stabilized at 1MPa;
when the water temperature is higher than 60 ℃, the controller adjusts the PEM electrolytic cell to increase the electrolytic current according to a third speed, and finally stabilizes at 3750A, and simultaneously sets the air outlet pressure of the cathode end to be 1MPa.
The first speed is 150A/min; the second speed is 250A/min; the third speed is 550A/min.
When the water temperature is less than 30 ℃, the controller sequentially increases the air outlet pressure of the cathode end to a first pressure, a second pressure and a third pressure, and finally stabilizes at 1MPa; wherein the first pressure is 0.3MPa, the second pressure is 0.5MPa, and the third pressure is 0.7MPa;
when the water temperature is 30-60 ℃, the controller sequentially increases the air outlet pressure of the cathode end to fourth pressure, fifth pressure and sixth pressure, and finally stabilizes the air outlet pressure at 1MPa; wherein the fourth pressure is 0.5MPa, the fifth pressure is 0.7MPa, and the sixth pressure is 0.9MPa.
The controller is further configured to: after the electrolysis is completed, reducing the electrolysis current of the PEM electrolyzer to 0 according to a fourth speed; the fourth speed is 12.5A/s.
The hydrogen treatment device comprises a hydrogen-water separator, a first shell-and-tube heat exchanger, a catalytic deoxidizing tower and an adsorption drying tower which are connected in sequence;
the air inlet end of the hydrogen-water separator is connected with the cathode end of the PEM electrolytic cell, and the air outlet end of the hydrogen-water separator is connected to the hydrogen inlet of the first shell-and-tube heat exchanger;
the hydrogen outlet of the first shell-and-tube heat exchanger is connected to the air inlet end of the catalytic deoxidization tower, the air outlet end of the catalytic deoxidization tower is connected to the air inlet end of the adsorption drying tower, and the air outlet end of the adsorption drying tower is connected to the air inlet end of the low-pressure hydrogen buffer device.
The first shell-and-tube heat exchanger adopts glycol solution as a shell side medium and adopts hydrogen as a tube side medium, and the design content is specifically as follows:
(a) Structural design
The main body structure is in a support type, and the support is a saddle type support.
Further, the individual nozzle designs are shown in table 1.
TABLE 1
| Nozzle type | Nominal diameter/mm | Nominal pressure/MPa | Flange type | Connection surface pattern | Connection standard and form |
| Hydrogen inlet | 32 | 4.0 | PL | RF | HG/T20592-2009 |
| Glycol solution outlet | 20 | 1.0 | PL | RF | HG/T20592-2009 |
| Hydrogen outlet | 32 | 4.0 | PL | RF | HG/T20592-2009 |
| Glycol solution inlet | 20 | 1.0 | PL | RF | HG/T20592-2009 |
| Venting out&Drain outlet | 15 | 4.0 | WN | RF | HG/T20592-2009 |
(b) Installation instruction
And (5) adopting horizontal installation and taking the horizontal installation as an installation anchor.
(c) Design parameters
The main body is made of 316L stainless steel, the saddle support is made of carbon steel, the heat exchange tube is phi 19 x 2mm in specification, the effective tube length is 1.5m, the number of heat exchange tube bundles is 76, and the heat exchange area is 6.4m 2 。
Design pressure: 0.8MPa of shell side and 3.5MPa of tube side; design temperature: shell side 60 ℃, tube side 110 ℃.
Working pressure: 0.7MPa of shell side and 3.7MPa of tube side; operating temperature: shell side 50 ℃ and tube side 100 ℃.
(d) Notice matters
When cleaning the tubes, steam must not be blown directly into the individual tubes, avoiding causing tube deformation or tube-to-tube sheet connection looseness.
The cleaning agent is selected to be suitable for the material of the equipment.
Based on the materials selected by the equipment, the chloride ion content in the water should be strictly controlled to be less than 25PPM in the using process.
(e) Device maintenance
Periodic checks were performed in accordance with TSG 21-2016.
Periodic sewage discharge and thickness measurement are carried out, and periodic inspection is actually carried out.
The equipment should often detect the medium temperature, pressure drop, water drain and vibration conditions of tube bundles of the tube and shell side during operation, if abnormality is found, the cause should be analyzed in time, overhauls and maintenance should be carried out if necessary, and overhauls and maintenance must be carried out during shutdown.
When the equipment stops running, the interior of the equipment is cleaned and dried in time, and all valves are closed in time, so that the humidity in the equipment is kept to be not more than 20%.
When the equipment is stopped for a long time, antiseptic measures are adopted, and a nitrogen charging method can be adopted. And opening a release valve and a water drain valve to clean and blow-dry water and hydrogen in the equipment, sealing all the valves, and filling and maintaining nitrogen with purity not less than 99% and pressure of 0.05 MPa.
The equipment is checked regularly according to the rules of the fixed pressure vessel safety technology supervision regulations.
The oxygen treatment device comprises an oxygen-water separator and a second shell-and-tube heat exchanger; the air inlet end of the oxygen-water separator is connected with the anode end of the PEM electrolytic cell and is used for separating oxygen from water of the oxygen product; the second shell-and-tube heat exchanger is used for cooling the oxygen separated by the oxygen-water separator, the oxygen inlet is connected with the air outlet end of the oxygen-water separator, and the oxygen outlet is used for discharging the cooled oxygen.
The second shell-and-tube heat exchanger adopts glycol solution as a shell side medium and oxygen as a tube side medium, and specifically meets the following design contents:
(a) Structural design
The main body structure is in a support type, and the support is a saddle type support.
In addition, the individual nozzle designs are shown in table 2.
TABLE 2
| Nozzle type | Nominal diameter/mm | Nominal pressure/MPa | Flange type | Connection surface pattern | Connection standard and form |
| Oxygen inlet | 40 | 4.0 | PL | RF | HG/T20592-2009 |
| Glycol solution outlet | 20 | 1.0 | PL | RF | HG/T20592-2009 |
| Oxygen outlet | 40 | 4.0 | PL | RF | HG/T20592-2009 |
| Glycol solution inlet | 20 | 1.0 | PL | RF | HG/T20592-2009 |
| Venting out&Drain outlet | 15 | 4.0 | WN | RF | HG/T20592-2009 |
(b) Installation instruction
And (5) adopting horizontal installation and taking the horizontal installation as an installation anchor.
(c) Design parameters
The main body is made of 316L stainless steel, the saddle support is made of carbon steel, the heat exchange tube is phi 19 x 2mm in specification, the effective tube length is 1.5m, the number of heat exchange tube bundles is 120, and the heat exchange area is 10m 2 。
Design pressure: 0.8MPa of shell side and 3.5MPa of tube side; design temperature: shell side 60 ℃, tube side 110 ℃.
Working pressure: 0.7MPa of shell side and 3.7MPa of tube side; operating temperature: shell side 50 ℃ and tube side 100 ℃.
(d) Notice matters
When cleaning the tubes, steam must not be blown directly into the individual tubes, avoiding causing tube deformation or tube-to-tube sheet connection looseness.
The cleaning agent is selected to be suitable for the material of the equipment.
Based on the materials selected by the equipment, the chloride ion content in the water should be strictly controlled to be less than 25PPM in the using process.
(e) Device maintenance
Periodic checks were performed in accordance with TSG 21-2016.
Periodic sewage discharge and thickness measurement are carried out, and periodic inspection is actually carried out.
The equipment should often detect the medium temperature, pressure drop, water drain and vibration conditions of tube bundles of the tube and shell side during operation, if abnormality is found, the cause should be analyzed in time, overhauls and maintenance should be carried out if necessary, and overhauls and maintenance must be carried out during shutdown.
When the equipment stops running, the interior of the equipment is cleaned and dried in time, and all valves are closed in time, so that the humidity in the equipment is kept to be not more than 20%.
When the equipment is stopped for a long time, antiseptic measures are adopted, and a nitrogen charging method can be adopted. And opening a release valve and a water drain valve to clean and blow-dry water and hydrogen in the equipment, sealing all the valves, and filling and maintaining nitrogen with purity not less than 99% and pressure of 0.05 MPa.
The equipment is checked regularly according to the rules of the fixed pressure vessel safety technology supervision regulations.
The water supply device comprises an ultrapure water machine and a water storage tank; the ultra-pure water machine is used for preparing ultra-pure water required by the electrolysis of the PEM electrolytic tank; the water storage tank is respectively connected with the ultrapure water machine and the PEM electrolytic tank and is used for storing ultrapure water and delivering the ultrapure water to the PEM electrolytic tank.
Example 2
A PEM hydrogen production and hydrogenation integrated system comprises a hydrogen production system, a transportation system and a hydrogenation system;
The hydrogen production system comprises hydrogen production equipment and low-pressure hydrogen buffer equipment (10 m is adopted 3 The low-pressure hydrogen buffer tank of (1) is operated under 3MPa, and the maximum hydrogen storage amount is 25 kg), a first hydrogen compression device (adopting an air compressor) and a hydrogen tube bundle container (adopting a hydrogen tube bundle container with the operating pressure of 20MPa and the maximum hydrogen storage amount of 133 kg);
the hydrogen production equipment comprises a PEM electrolytic tank, a water supply device, a hydrogen treatment device and an oxygen treatment device; the water supply device is used for providing ultrapure water required by electrolysis for the PEM electrolytic tank; the hydrogen treatment device is used for treating a hydrogen product generated at the cathode end of the PEM electrolytic tank and conveying the treated hydrogen to the low-pressure hydrogen buffer device; the oxygen treatment device is used for treating an oxygen product generated at the anode end of the PEM electrolytic cell;
the hydrogenation system comprises a second hydrogen compression device (adopting an air compressor), a high-pressure hydrogen storage device (adopting a high-pressure hydrogen cylinder group with the operating pressure of 45MPa and the maximum hydrogen storage amount of 173 kg) and a hydrogenation device which are connected in sequence; the total stored hydrogen amount of the PEM hydrogen production and hydrogenation integrated system can reach 331kg at maximum;
The transportation system is a hydrogen tube bundle vehicle and is used for conveying hydrogen in the hydrogen tube bundle container to the second hydrogen compression equipment.
The hydrogen production equipment also comprises a temperature detector and a controller; the temperature detector is used for detecting the water temperature of the PEM electrolytic tank; the control machine is used for adjusting the electrolysis current of the PEM electrolytic tank and the air outlet pressure of the cathode end according to the water temperature as follows:
when the water temperature is less than 30 ℃, the controller adjusts the PEM electrolytic tank to increase the electrolytic current according to a first speed, so that the electrolytic current is finally stabilized at 1500A, and meanwhile, the air outlet pressure at the cathode end is gradually increased, so that the electrolytic current is finally stabilized at 1.5MPa;
when the water temperature is 30-60 ℃, the control machine adjusts the PEM electrolytic tank to increase the electrolytic current according to a second speed, so that the electrolytic current is finally stabilized at 2500A, and meanwhile, the air outlet pressure of the cathode end is gradually increased, so that the electrolytic current is finally stabilized at 1.5MPa;
when the water temperature is higher than 60 ℃, the controller adjusts the PEM electrolytic cell to increase the electrolytic current according to a third speed, finally stabilizing at 3000A, and setting the air outlet pressure of the cathode end to be 1.5MPa.
The first speed is 200A/min; the second speed is 300A/min; the third speed is 600A/min.
When the water temperature is less than 30 ℃, the controller sequentially increases the air outlet pressure of the cathode end to a first pressure, a second pressure and a third pressure, and finally stabilizes at 1-1.5MPa; wherein the first pressure is 0.3MPa, the second pressure is 0.5MPa, and the third pressure is 0.7MPa;
when the water temperature is 30-60 ℃, the controller sequentially increases the air outlet pressure of the cathode end to fourth pressure, fifth pressure and sixth pressure, and finally stabilizes the air outlet pressure at 1.5MPa; wherein the fourth pressure is 0.5MPa, the fifth pressure is 0.7MPa, and the sixth pressure is 0.9MPa.
The controller is further configured to: after the electrolysis is completed, reducing the electrolysis current of the PEM electrolyzer to 0 according to a fourth speed; the fourth speed is 20A/s.
The hydrogen treatment device comprises a first hydrogen-water separator, a first shell-and-tube heat exchanger, a catalytic deoxidizing tower and an adsorption drying tower which are connected in sequence;
the air inlet end of the first hydrogen-water separator is connected with the cathode end of the PEM electrolytic tank, and the air outlet end of the first hydrogen-water separator is connected to the hydrogen inlet of the first shell-and-tube heat exchanger;
the hydrogen outlet of the first shell-and-tube heat exchanger is connected to the air inlet end of the catalytic deoxidizing tower, the air outlet end of the catalytic deoxidizing tower is connected to the air inlet end of the adsorption drying tower,
And the air outlet end of the adsorption drying tower is connected to the air inlet end of the low-pressure hydrogen buffer device.
The first shell-and-tube heat exchanger adopts glycol solution as shell side medium and hydrogen as tube side medium, and the specific design content is shown in the embodiment 1.
The hydrogen treatment device also comprises a second hydrogen-water separator for separating gas from liquid of the water separated by the first hydrogen-water separator.
The oxygen treatment device comprises an oxygen-water separator and a second shell-and-tube heat exchanger; the air inlet end of the oxygen-water separator is connected with the anode end of the PEM electrolytic cell and is used for separating oxygen from water of the oxygen product; the second shell-and-tube heat exchanger is used for cooling the oxygen separated by the oxygen-water separator, the oxygen inlet is connected with the air outlet end of the oxygen-water separator, and the oxygen outlet is used for discharging the cooled oxygen.
The second shell-and-tube heat exchanger adopts glycol solution as shell side medium and oxygen as tube side medium, and the specific design content is shown in the embodiment 1.
The water supply device comprises an ultrapure water machine and a water storage tank; the ultra-pure water machine is used for preparing ultra-pure water required by the electrolysis of the PEM electrolytic tank; the water storage tank is respectively connected with the ultrapure water machine and the PEM electrolytic tank and is used for storing ultrapure water and delivering the ultrapure water to the PEM electrolytic tank.
The water outlet ends of the first hydrogen-water separator, the second hydrogen-water separator and the oxygen-gas separator are all connected to the water storage tank, so that the recovery and utilization of the ultrapure water are realized.
The water storage tank is provided with a water level detector for detecting the water level of ultrapure water in the water storage tank.
The hydrogenation equipment comprises a hydrogenation machine, and the maximum working pressure of the hydrogenation machine is less than or equal to 45MPa.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and are not limiting; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit and scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. A PEM hydrogen production and hydrogenation integrated system is characterized by comprising a hydrogen production system, a transportation system and a hydrogenation system;
the hydrogen production system comprises hydrogen production equipment, low-pressure hydrogen buffer equipment, first hydrogen compression equipment and a hydrogen tube bundle container which are connected in sequence;
The hydrogen production equipment comprises a PEM electrolytic tank, a water supply device, a hydrogen treatment device and an oxygen treatment device; the water supply device is used for providing ultrapure water required by electrolysis for the PEM electrolytic tank; the hydrogen treatment device is used for treating a hydrogen product generated at the cathode end of the PEM electrolytic tank and conveying the treated hydrogen to the low-pressure hydrogen buffer device; the oxygen treatment device is used for treating an oxygen product generated at the anode end of the PEM electrolytic cell; the hydrogen production equipment also comprises a temperature detector and a controller; the temperature detector is used for detecting the water temperature of the PEM electrolytic tank; the control machine is used for adjusting the electrolysis current of the PEM electrolytic tank and the air outlet pressure of the cathode end according to the water temperature;
the hydrogenation system comprises a second hydrogen compression device, a high-pressure hydrogen storage device and a hydrogenation device which are connected in sequence;
the transportation system is used for conveying the hydrogen in the hydrogen tube bundle container to the second hydrogen compression equipment;
the operating pressure of the low-pressure hydrogen buffer device is less than or equal to 3MPa;
the operating pressure of the high-pressure hydrogen storage device is less than or equal to 45MPa.
2. The integrated PEM hydrogen production and hydrogenation system of claim 1 wherein,
The hydrogen treatment device comprises a hydrogen-water separator, a first shell-and-tube heat exchanger, a catalytic deoxidizing tower and an adsorption drying tower which are connected in sequence;
the air inlet end of the hydrogen-water separator is connected with the cathode end of the PEM electrolytic cell, and the air outlet end of the hydrogen-water separator is connected to the hydrogen inlet of the first shell-and-tube heat exchanger;
the hydrogen outlet of the first shell-and-tube heat exchanger is connected to the air inlet end of the catalytic deoxidization tower, the air outlet end of the catalytic deoxidization tower is connected to the air inlet end of the adsorption drying tower, and the air outlet end of the adsorption drying tower is connected to the air inlet end of the low-pressure hydrogen buffer device.
3. The integrated PEM hydrogen production and hydrogenation system of claim 1 wherein,
the oxygen treatment device comprises an oxygen-water separator and a second shell-and-tube heat exchanger; the air inlet end of the oxygen-water separator is connected with the anode end of the PEM electrolytic cell and is used for separating oxygen from water of the oxygen product;
the second shell-and-tube heat exchanger is used for cooling the oxygen separated by the oxygen-water separator, the oxygen inlet is connected with the air outlet end of the oxygen-water separator, and the oxygen outlet is used for discharging the cooled oxygen.
4. The integrated PEM hydrogen production and hydrogenation system of claim 1 wherein,
The water supply device comprises an ultrapure water machine and a water storage tank; the ultra-pure water machine is used for preparing ultra-pure water required by the electrolysis of the PEM electrolytic tank; the water storage tank is respectively connected with the ultrapure water machine and the PEM electrolytic tank and is used for storing ultrapure water and delivering the ultrapure water to the PEM electrolytic tank.
5. The integrated PEM hydrogen production and hydrogenation system of claim 2 wherein,
the main body structure type of the first shell-and-tube heat exchanger is a support type, and the support is a saddle type support;
the specification of the heat exchange tube of the first shell-and-tube heat exchanger is phi (15-20) x 2mm, the effective tube length is 1-2m, the number of heat exchange tube bundles is 70-80, and the heat exchange area is 6-8m 2 ；
The nominal diameter of the hydrogen inlet of the first shell-and-tube heat exchanger is 30-40mm, and the nominal pressure is 3-5MPa; the nominal diameter of the hydrogen outlet of the first shell-and-tube heat exchanger is 30-40mm, and the nominal pressure is 3-5MPa.
6. A PEM hydrogen production and hydrogenation integrated system according to claim 3,
the main body structure type of the second shell-and-tube heat exchanger is a support type, and the support is a saddle type support;
the specification of the heat exchange tube of the second shell-and-tube heat exchanger is phi (15-20) x 2mm, the effective tube length is 1-2m, the number of heat exchange tube bundles is 110-120, and the heat exchange area is 9-10m 2 ；
The nominal diameter of the oxygen inlet of the second shell-and-tube heat exchanger is 40-50mm, and the nominal pressure is 4-6MPa; the nominal diameter of the oxygen outlet of the second shell-and-tube heat exchanger is 40-45mm, and the nominal pressure is 4-5MPa.
7. A hydrogen production control method based on the PEM hydrogen production hydrogenation integrated system according to claim 1 to 6, characterized in that,
when the water temperature is less than 30 ℃, the control machine adjusts the PEM electrolytic tank to increase the electrolytic current according to a first speed, and finally stabilizes the electrolytic current at 1000-1500A, and meanwhile, the air outlet pressure of the cathode end is gradually increased, and finally stabilizes the electrolytic current at 1-1.5MPa;
when the water temperature is 30-60 ℃, the control machine adjusts the PEM electrolytic tank to increase the electrolytic current according to a second speed, and finally stabilizes at 2000-2500A, and meanwhile, the air outlet pressure of the cathode end is gradually increased, and finally stabilizes at 1-1.5MPa;
when the water temperature is higher than 60 ℃, the controller adjusts the PEM electrolytic cell to increase the electrolytic current according to a third speed, finally stabilizes at 3000-3750A, and simultaneously sets the air outlet pressure of the cathode end to 1-1.5MPa.
8. The hydrogen production control method of the PEM hydrogen production hydrogenation integrated system according to claim 7,
The first speed is 100-200A/min;
the second speed is 200-300A/min;
the third speed is 500-600A/min.
9. The hydrogen production control method of the PEM hydrogen production hydrogenation integrated system according to claim 7,
when the water temperature is less than 30 ℃, the controller sequentially increases the air outlet pressure of the cathode end to a first pressure, a second pressure and a third pressure, and finally stabilizes at 1-1.5MPa; wherein the first pressure is 0.2-0.3MPa, the second pressure is 0.4-0.5MPa, and the third pressure is 0.6-0.7MPa;
when the water temperature is 30-60 ℃, the control machine sequentially increases the air outlet pressure of the cathode end to fourth pressure, fifth pressure and sixth pressure, and finally, the air outlet pressure is stabilized at 1-1.5MPa; wherein the fourth pressure is 0.4-0.5MPa, the fifth pressure is 0.6-0.7MPa, and the sixth pressure is 0.8-0.9MPa.
10. The hydrogen production control method of the PEM hydrogen production hydrogenation integrated system according to claim 7,
after electrolysis is completed, the control machine reduces the electrolysis current of the PEM electrolyzer to 0 according to a fourth speed; the fourth speed is 10-20A/s.
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