CN114807962B - Alkaline water electrolysis hydrogen production system based on absorption heat pump and adjusting method thereof - Google Patents
Alkaline water electrolysis hydrogen production system based on absorption heat pump and adjusting method thereof Download PDFInfo
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- CN114807962B CN114807962B CN202210393026.1A CN202210393026A CN114807962B CN 114807962 B CN114807962 B CN 114807962B CN 202210393026 A CN202210393026 A CN 202210393026A CN 114807962 B CN114807962 B CN 114807962B
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Abstract
The application belongs to the technical field of electrolytic hydrogen production, and discloses an alkaline electrolytic water hydrogen production system based on an absorption heat pump and an adjusting method thereof, wherein the system comprises the following components: the system comprises an alkaline water electrolysis hydrogen production subsystem and an absorption heat pump subsystem, wherein the absorption heat pump subsystem comprises a generator and an evaporator, and heat exchange tubes are arranged in the generator and the evaporator; the alkaline electrolyzed water hydrogen production subsystem comprises an electrolytic tank, a first regenerative heat exchanger, a second regenerative heat exchanger and a gas-liquid separation treatment device; the hydrogen pipeline and the oxygen pipeline at the outlet of the electrolytic tank partially pass through the first heat recovery heat exchanger and the second heat recovery heat exchanger for heat exchange before being input into the gas-liquid separation treatment device after heat exchange in the heat exchange pipe, and the liquid separated by the gas-liquid separation treatment device is input into the electrolytic tank after heat exchange by the first heat recovery heat exchanger and the second heat recovery heat exchanger. The application realizes the recovery of waste heat in the electrolysis process, can effectively maintain the working temperature of the electrolytic hydrogen production, and improves the comprehensive utilization rate of energy and the electrolytic hydrogen production efficiency.
Description
Technical Field
The application belongs to the technical field related to alkaline water electrolysis hydrogen production, and particularly relates to an alkaline water electrolysis hydrogen production system based on an absorption heat pump and an adjusting method thereof.
Background
Hydrogen has shown great development potential in the new energy market due to its advantages of high heat value, cleanliness, long-period storage and long-distance transportation. Currently, the alkaline water electrolysis hydrogen production technology is put into commercial production, and the advantages of simple structure, low cost, cleanness and environmental protection lead the alkaline water electrolysis hydrogen production technology to be most widely produced and most developed in the electrolytic hydrogen production market. However, the power consumption of the technology is as high as 4.5 to 5.5kWh/m 3 N (H2), and approximately 40% of the electric energy is converted into heat energy in the actual electrolysis process, so that the temperature of the electrolytic tank is obviously increased, and the heat energy is mostly along with the electrolyte and the productThe mixture of gases exiting the electrolyzer is dissipated in the environment. In recent years, a method for carrying out electrolytic hydrogen production by utilizing surplus electric energy of 'three-waste' (wind waste, light waste and water waste) by coupling electrolytic hydrogen production and renewable energy (wind energy, light energy and water energy) power generation technology becomes an important way for reducing the energy consumption of electrolytic hydrogen production and improving the comprehensive utilization rate of power generation. But is limited by the influence of natural conditions, renewable energy sources have intermittence and randomness, often resulting in the fluctuation of the generated power thereof. For an alkaline water electrolysis hydrogen production system, the working temperature of an electrolytic tank is generally set at 80 ℃, but in the period of lean power generation and low load operation, the electric power consumption is only 20% or less of that of normal operation, the heat dissipation capacity of the electrolytic tank to the outside is larger than that of electrolysis heat generation, the temperature of the electrolytic tank is obviously reduced, and the operation temperature of the electrolytic tank cannot reach the optimal working temperature area of electrolysis reaction, so that the rate of the electrolysis reaction is reduced, and the electrolysis efficiency is reduced.
The experimental research on the alkaline water electrolysis hydrogen production system at the present stage is concentrated on the development and optimization of hydrogen production materials, device structures and system control, and comprises the exploration and analysis of parameter adjustment methods such as temperature, flow and the like and energy management and utilization methods of the alkaline water electrolysis hydrogen production system, so that a certain research result is obtained from the aspects of energy utilization or operation efficiency. Chinese patent CN110670087a discloses a controllable rapid heating electrolytic water hydrogen production system, which discloses an electrically heatable auxiliary heat of gas-liquid mixture, which can effectively regulate and meet the heat requirement of the electrolytic water hydrogen production system in the starting and running processes thereof. Chinese patent CN111336571 discloses a system for recovering waste heat generated in the process of producing hydrogen by electrolyzing water and a working method thereof, which discloses a method for recovering waste heat generated in the process of producing hydrogen by electrolyzing water, wherein the waste heat is used as a heat source to supply water for a membrane distillation system to prepare a hydrogen production system, and the circulating water after heating the raw water by membrane distillation is reused for workshop heating, thereby improving energy utilization efficiency and reducing heat supply energy consumption of the distillation system. Chinese patents CN215062987 and CN113137783 disclose a system for recovering hydrogen production waste heat by using heat pump, but they have poor regulation capability and cannot be adaptively regulated according to load variation. Chinese patent CN213013112U discloses a comprehensive thermal management system of a large-scale alkaline water electrolysis hydrogen production device, which discloses a comprehensive thermal management system for recovering waste heat generated in the electrolysis process, wherein part of the waste heat is stored in a heat storage tank, part of the waste heat is supplied to heat user equipment, and part of the waste heat is used for heat exchange to raise the temperature of the returned alkaline solution at the inlet of the electrolytic tank. According to the search, the analysis design of waste heat recovery of an alkaline water electrolysis hydrogen production system is not lacking in the existing research, but the temperature obtained by recovery is 60-70 ℃, the grade of the energy obtained by recovery is generally lower than that of the waste heat, and in the related research, a design method for improving the working temperature of an electrolytic tank in a low-load operation period through auxiliary heat of an external heat source is also provided, and although the electrolytic tank can be effectively maintained in a set working temperature area, the adaptability of the system to load change is improved, and the energy consumption of the system is increased to a certain extent through the auxiliary heat of the external heat source.
Disclosure of Invention
Aiming at the defects or improvement demands of the prior art, the application provides an alkaline electrolyzed water hydrogen production system based on an absorption heat pump and an adjusting method thereof.
To achieve the above object, according to one aspect of the present application, there is provided an alkaline electrolyzed water hydrogen production system based on an absorption heat pump, the system comprising an alkaline electrolyzed water hydrogen production subsystem and an absorption heat pump subsystem, wherein: the absorption heat pump subsystem comprises a generator and an evaporator, wherein the hydrogen heat exchange tube and the oxygen heat exchange tube are arranged in the generator and the evaporator; the alkaline electrolyzed water hydrogen production subsystem comprises an electrolytic tank, a first regenerative heat exchanger, a second regenerative heat exchanger and a gas-liquid separation treatment device; the hydrogen pipeline at the outlet of the electrolytic tank is sequentially connected with the hydrogen heat exchange tube in the evaporator and the hydrogen heat exchange tube in the generator, and the oxygen pipeline at the outlet of the electrolytic tank is connected with the oxygen heat exchange tube in the evaporator and the oxygen heat exchange tube in the generator; the output pipeline of the hydrogen heat exchange tube in the generator is divided into two branches, one branch passes through the first regenerative heat exchanger to participate in heat exchange, and the other branch is output to the gas-liquid separation treatment device; the output pipeline of the oxygen heat exchange tube in the generator is divided into two branches, one branch penetrates through the second regenerative heat exchanger to participate in heat exchange, the other branch is output to the gas-liquid separation treatment device, liquid separated by the gas-liquid separation treatment device is divided into two branches, the two branches are respectively input into the electrolytic tank after heat exchange of the first regenerative heat exchanger and the second regenerative heat exchanger, and valves are respectively arranged on the two branches which are divided into the output pipeline of the hydrogen heat exchange tube and the oxygen heat exchange tube in the generator.
Preferably, the generator and the evaporator are sequentially arranged along the direction of the refrigerant, and if the hydrogen heat exchange tube in the generator is arranged at the downstream, the hydrogen heat exchange tube in the evaporator is arranged at the upstream; if the hydrogen heat exchange tube in the generator is arranged at the upstream, the hydrogen heat exchange tube in the evaporator is arranged at the downstream.
Preferably, the absorption heat pump subsystem further comprises a condenser, the condenser being provided between the generator and the evaporator.
Preferably, the system further comprises a hot water circulation subsystem, the hot water circulation subsystem comprises a desiccant regeneration device, the absorption heat pump subsystem further comprises an absorber, the absorber is arranged at the downstream of the evaporator, a fifth heat exchange tube is arranged in the absorber, and circulating water of the hot water circulation subsystem flows into the desiccant regeneration device after exchanging heat in the fifth heat exchange tube.
Preferably, the hot water circulation subsystem further comprises a circulating water preheater, the circulating water preheater is arranged between the first regenerative heat exchanger and the second regenerative heat exchanger and the gas-liquid separation treatment device, and two branches divided by an output pipeline of the hydrogen heat exchange tube in the generator are combined and flow into the circulating water preheater for heat exchange after passing through the first regenerative heat exchanger; the output pipeline of the oxygen heat exchange pipe in the generator is divided into two branches, and the two branches are combined and flow into the circulating water preheater for heat exchange after passing through the second regenerative heat exchanger.
Preferably, the absorption heat pump subsystem further comprises a solution heat exchanger, wherein the solution heat exchanger is arranged between the absorber and the generator, so that the dilute solution of the refrigerant output by the absorber exchanges heat with the concentrated solution of the refrigerant output by the generator before the dilute solution of the refrigerant output by the absorber is input into the generator, and the concentrated solution of the refrigerant after heat exchange is input into the absorber.
Preferably, a drying agent output pipeline of the drying agent regeneration device is connected with the gas-liquid separation treatment device and is used for drying the gas of the gas-liquid separation treatment device.
Preferably, the gas-liquid separation treatment device comprises an air cooler, a hydrogen separation treatment sub-device and an oxygen separation treatment sub-device, and the hydrogen separation treatment sub-device and the oxygen separation treatment sub-device are connected in parallel at the downstream of the air cooler.
Preferably, the operating pressure on the evaporator and absorber side is higher than the operating pressure on the condenser and generator side.
In another aspect, the application provides a method for adjusting an alkaline water electrolysis hydrogen production system based on an absorption heat pump, which comprises the following steps: when the electrolysis power of the electrolysis bath is sufficient, closing valves on the branches passing through the first regenerative heat exchanger and the second regenerative heat exchanger, and opening valves on the branches not passing through the first regenerative heat exchanger and the second regenerative heat exchanger; when the electrolysis power of the electrolysis bath is insufficient, valves on the branches of the first heat recovery heat exchanger and the second heat recovery heat exchanger are opened, and valves on the branches of the first heat recovery heat exchanger and the second heat recovery heat exchanger which are not passed through are opened or closed and the opening degree of the valves is controlled.
In general, compared with the prior art, the alkaline water electrolysis hydrogen production system based on the absorption heat pump and the adjusting method thereof have the following beneficial effects:
1. the low-grade waste heat in the alkaline water electrolysis hydrogen production process is utilized by the heat pump system, so that the energy waste is avoided, meanwhile, the low-grade waste heat in the hydrogen production process is also used for heating and refluxing alkali liquor, so that the temperature of the alkali liquor entering the electrolytic tank is improved, the stability of the electrolytic tank reaction, especially in low load, is facilitated to be maintained, the electrolytic hydrogen production working temperature is further effectively maintained, and the comprehensive energy utilization rate and the electrolytic hydrogen production efficiency are improved.
2. The heat recovery heat exchanger, the air cooler, the circulating water preheater and the like can further cool the gas-liquid mixture, so that the temperature of the gas-liquid mixture is obviously reduced, the atomization degree of liquid is low after the gas-liquid mixture enters the gas-liquid separation treatment device, the gas-liquid separation effect is more obvious, and the manufacturing cost of the cooling load of gas-liquid separation is reduced.
3. The absorber can emit a large amount of heat energy which is higher than the grade of the waste heat, and heat the circulating water of the hot water circulating system to obtain high-temperature circulating water for heating and regenerating the drying agent, so that the regeneration cost of the gas drying agent is obviously reduced, and the device can also be used for other high-temperature heat utilization equipment to realize grade improvement and reutilization of the waste heat.
4. The output pipelines of the hydrogen heat exchange pipe and the oxygen heat exchange pipe in the generator are divided into two branches which are respectively provided with a valve, the flow of the gas-liquid mixture in the corresponding regenerative heat exchanger can be controlled through the adjustment of the opening of the valves, and the heat exchange quantity of the gas-liquid mixture and the reflux alkali liquor is adjusted, so that the temperature of the reflux alkali liquor at the inlet of the electrolytic tank is changed, the electrolytic tank is maintained in a set working temperature zone, the temperature control capability of the alkaline electrolyzed water hydrogen production system is improved, the adaptability of the system under the variable load working condition is enhanced, and the comprehensive energy utilization efficiency of the system is improved.
Drawings
FIG. 1 is a schematic diagram of an alkaline point water splitting hydrogen production system based on an absorption heat pump according to an embodiment of the application;
FIG. 2 is a schematic diagram of a generator according to an embodiment of the present application;
FIG. 3 is a schematic view showing the structure of an evaporator according to an embodiment of the present application;
FIG. 4 is a schematic diagram of the absorber structure of an embodiment of the present application;
FIG. 5 is a schematic diagram of the alkaline point water splitting hydrogen production system of the present application during normal load operation based on an absorption heat pump;
FIG. 6 is a schematic diagram of the alkaline point hydrolysis hydrogen production system of the present application based on an absorption heat pump during low load operation.
The same reference numbers are used throughout the drawings to reference like elements or structures, wherein:
101-an electrolytic cell; 102-a first regenerative heat exchanger; 103-a second regenerative heat exchanger; 104-an air cooler; 105-hydrogen side gas-liquid separator; 106-an oxygen side gas-liquid separator; 107-hydrogen side gas treatment device; 108-an oxygen side gas treatment device; 109-a hydrogen storage tank; 110-an oxygen storage tank; 111-an alkali liquor circulating pump; 112-a first valve; 113-a second valve; 114-a third valve; 115-fourth valve; 201-a generator; 201-a-an inlet of a first heat exchange tube; 201-b-an outlet of the first heat exchange tube; 201-c-an inlet of a second heat exchange tube; 201-d-an outlet of the second heat exchange tube; 201-e-a first outlet; 201-g-second outlet; 201-h-a first heat exchange tube; 201-i-a second heat exchange tube; 201-f-generator inlet; 202-a condenser; 203-a solvent pump; 204-an evaporator; 204-a-an inlet of a fourth heat exchange tube; 204-b-an outlet of the fourth heat exchange tube; 204-c-an inlet of a third heat exchange tube; 204-d-an outlet of the third heat exchange tube; 204-e-evaporator inlet; 204-f-evaporator outlet; 204-g-a third heat exchange tube; 204-h-a fourth heat exchange tube; 205-absorber; 205-c-absorber second inlet; 205-d-absorber first inlet; 205-e-absorber outlet; 205-f-fifth heat exchange tube; 206-a solution heat exchanger; 207-solution pump; 208-throttle valve; 301 a desiccant regeneration device; 302-a circulating water preheater; 303-a circulating water pump.
Detailed Description
The present application will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present application more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the application. In addition, the technical features of the embodiments of the present application described below may be combined with each other as long as they do not collide with each other.
Referring to fig. 1, the application provides an alkaline point water-splitting hydrogen production system based on an absorption heat pump, which comprises an alkaline water-splitting hydrogen production subsystem and an absorption heat pump subsystem, and has the following specific structure.
The absorption heat pump subsystem comprises a generator 201 and an evaporator 204. The generator 201 includes a generator inlet 201-f for inputting a dilute solution of a refrigerant, a first outlet 201-e for outputting a concentrated solution of the refrigerant, and a second outlet 201-g for outputting a refrigerant gas, as shown in fig. 2. The generator 201 is further provided with two hydrogen heat exchange tubes and an oxygen heat exchange tube, as shown in fig. 2, which may be a first heat exchange tube 201-h and a second heat exchange tube 201-i. The evaporator 204 includes an evaporator inlet 204-e for inputting refrigerant and an evaporator outlet 204-f for outputting refrigerant vapor as shown in fig. 3. The evaporator 204 is also provided with a hydrogen heat exchange tube and an oxygen heat exchange tube, which are respectively a third heat exchange tube 204-g and a fourth heat exchange tube 204-h.
The generator and the evaporator are sequentially arranged along the direction of the refrigerant, and if the hydrogen heat exchange tube in the generator is arranged at the downstream, the hydrogen heat exchange tube in the evaporator is arranged at the upstream; if the hydrogen heat exchange tube in the generator is arranged at the upstream, the hydrogen heat exchange tube in the evaporator is arranged at the downstream.
A condenser 202 is disposed between the generator 201 and the evaporator 204, and the gas output from the generator 201 is condensed by the condenser 202 and then input into the evaporator 204. In order to ensure smooth circulation of the fluid, a solvent pump 203 is further disposed between the condenser 202 and the evaporator 204 to drive the fluid in the condenser 202 to be transferred into the evaporator 204.
The absorption heat pump subsystem further comprises an absorber 205, the absorber 205 being arranged downstream of the evaporator 204. As shown in fig. 4, a fifth heat exchange tube 205-f is disposed in the absorber 205, and the absorber 205 includes an absorber first inlet 205-d, an absorber second inlet 205-c, and an absorber outlet 205-e. The absorber first inlet 205-d is connected to the evaporator outlet 204-f, the absorber outlet 205-e is connected to the generator inlet 201-f, and the absorber second inlet 205-c is connected to the first outlet 201-e.
The absorption heat pump subsystem further comprises a solution heat exchanger 206, wherein the solution heat exchanger 206 is arranged between the absorber 205 and the generator 201, so that the dilute solution of the refrigerant output by the absorber 205 exchanges heat with the concentrated solution of the refrigerant output by the generator 201 before being input into the generator 201, and the concentrated solution of the refrigerant after heat exchange is input into the absorber 205. Further preferably, a solution pump 207 is further provided on the concentrated solution transporting pipe to ensure smooth transporting of the concentrated solution. Further preferably, a throttle valve 208 is also provided in the dilute solution delivery line.
The alkaline electrolyzed water hydrogen production subsystem comprises an electrolytic tank 101, a first regenerative heat exchanger 102, a second regenerative heat exchanger 103 and a gas-liquid separation treatment device. The cathode after electrolysis of the electrolytic tank generates hydrogen and the anode generates oxygen, so that two output branches of the electrolytic tank transport a hydrogen side gas-liquid mixture and an oxygen side gas-liquid mixture respectively, an outlet of the hydrogen side gas-liquid mixture is connected with an inlet 204-a of a fourth heat exchange tube, and then is input into an inlet 201-a of a first heat exchange tube, and then is output from an outlet 201-b of the first heat exchange tube and then is divided into two branches, one branch passes through the first regenerative heat exchanger 102 to participate in heat exchange, and the other branch is output to the gas-liquid separation treatment device. The outlet of the oxygen side gas-liquid mixture is connected with the inlet 204-c of the third heat exchange tube, the fluid output by the outlet 204-d of the third heat exchange tube is input into the inlet 201-c of the second heat exchange tube, then is output from the outlet 201-d of the second heat exchange tube and is divided into two branches, one branch passes through the second regenerative heat exchanger 103 to participate in heat exchange, and the other branch is output to the gas-liquid separation treatment device.
Valves are arranged on two branches of the output pipeline of the hydrogen heat exchange pipe and the oxygen heat exchange pipe in the generator, as shown in fig. 1, the valves are respectively a first valve 112, a second valve 113, a third valve 114 and a fourth valve 115, and the flow on the corresponding branch can be adjusted by adjusting the opening of the first valve 112, the opening of the second valve 113, the opening of the third valve 114 and the opening of the fourth valve 115, so that the heat exchange quantity can be adjusted, and the control of the temperature of the return alkali lye can be realized.
The liquid separated by the gas-liquid separation treatment device is respectively input into the electrolytic tank 101 through an alkali liquor circulating pump 111 after heat exchange of the first regenerative heat exchanger 102 and the second regenerative heat exchanger 103.
The gas-liquid separation treatment device comprises an air cooler 104, a hydrogen separation treatment sub-device and an oxygen separation treatment sub-device, wherein the hydrogen separation treatment sub-device and the oxygen separation treatment sub-device are connected in parallel and arranged at the downstream of the air cooler 104. The hydrogen separation processing sub-unit includes a hydrogen-side gas-liquid separator 105, a hydrogen-side gas processing unit 107, and a hydrogen tank 109. The oxygen separation treatment sub-unit includes an oxygen-side gas-liquid separator 106, an oxygen-side gas treatment device 108, and an oxygen storage tank 110.
The system further comprises a hot water circulation subsystem, wherein the hot water circulation subsystem comprises a desiccant regeneration device 301, and circulating water of the hot water circulation subsystem flows into the desiccant regeneration device 301 through a circulating water pump 303 after exchanging heat in the fifth heat exchange tube 205-f. The desiccant regeneration device 301 heats the saturated gas desiccant to regenerate the desiccant.
The hot water circulation subsystem further comprises a circulating water preheater 302, the circulating water preheater 302 is arranged between the first heat recovery heat exchanger 102 and the second heat recovery heat exchanger 103 and the gas-liquid separation treatment device, and two branches divided by an output pipeline of a hydrogen heat exchange tube in the generator 201 are merged and flow into the circulating water preheater 302 for heat exchange after passing through the first heat recovery heat exchanger 102; the two branches of the output pipeline of the oxygen heat exchange pipe in the generator 201 are combined and flow into the circulating water preheater 302 for heat exchange after passing through the second regenerative heat exchanger 103. The circulating water outputted from the desiccant regenerating device 301 is heated by the circulating water preheater 302 and then inputted into the fifth heat exchange tube 205-f.
In this embodiment, the electrolyte of the alkaline water electrolysis hydrogen production system is NaOH or KOH solution, and the gas treatment device includes equipment for cooling, drying, purifying, and the like, the gas.
The absorption heat pump subsystem is a second type of absorption heat pump, and the heat transfer medium is preferably lithium bromide solution. The evaporator 204 and absorber 205 side operating pressures are higher than the generator 201 and condenser 202 side operating pressures. The condenser 202 is provided with cooling water as a low temperature heat source to cool the refrigerant. The evaporator 204 and the generator 201 sequentially absorb the heat energy of the driving heat source, and the heat energy higher than the temperature of the driving heat source is discharged from the absorber 205 through solution circulation, wherein the evaporator 204 is an evaporator for multi-flow heat exchange by taking a mixture of gas and liquid on the hydrogen side and the oxygen side as the driving heat source, and the generator 201 is a generator for multi-flow heat exchange by taking the mixture of gas and liquid on the hydrogen side and the oxygen side as the driving heat source and participates in the absorption heat pump subsystem circulation.
The alkaline electrolyzed water hydrogen production subsystem, the absorption heat pump subsystem and the hot water circulation subsystem are all provided with necessary thermometers and regulating valves, and can be used for monitoring the temperature and regulating the flow.
The working process of the alkaline water electrolysis hydrogen production system based on the absorption heat pump in the embodiment is as follows.
When the electrolytic tank 101 is in a normal load working period, as shown in fig. 5, hydrogen and oxygen are generated by hydrolysis in the tank, the normal working temperature is set to be 85 ℃, part of electric energy is converted into heat energy in the electrolytic process, a large amount of heat is required to be dissipated outwards to maintain the stable tank temperature, the gas-liquid mixture at the hydrogen side and the gas-liquid mixture at the oxygen side at about 85 ℃ respectively flow out of the electrolytic tank 101 and are used as a driving heat source of the absorption heat pump subsystem to enter the evaporator 204, and heat exchange tubes corresponding to the generator 201 are used for heat exchange and cooling. The following describes the procedure for adjusting the hydrogen-side flow path: the hydrogen side gas-liquid mixture sequentially enters the fourth heat exchange tube 204-h and the first heat exchange tube 201-h for gradual cooling, after cooling, the temperature of the gas-liquid mixture at the outlet 201-b of the first heat exchange tube of the generator 201 is about 70 ℃ and is divided into two flow paths, at the moment, the opening of the first valve 112 and the opening of the second valve 113 are controlled, so that the first valve 112 is fully opened, the second valve 113 is closed, and at the moment, the hydrogen side gas-liquid mixture completely flows through the first valve 112 to bypass the first regenerative heat exchanger 102; then, the circulating water at the outlet of the drying agent regenerating device 301 is preheated by the hydrogen-side gas-liquid mixture in the circulating water preheater 302, the gas-liquid mixture is further cooled in the air cooler 104, the temperature is reduced to about 55 ℃, then the gas-liquid mixture enters the hydrogen-side gas-liquid separator 105, the hydrogen to be treated at the outlet of the hydrogen-side gas-liquid separator 105 enters the corresponding hydrogen-side gas treatment device 107 for purification treatment, and finally the hydrogen to be treated is stored in the hydrogen storage tank 109; the oxygen-side flow path is similar to the above, and the following description is given of the oxygen-side flow path: the gas-liquid mixture at the oxygen side flows out of the anode of the electrolytic tank 101, sequentially enters the third heat exchange tube 204-g and the second heat exchange tube 201-i for gradual cooling, the temperature of the gas-liquid mixture at the outlet 201-d of the second heat exchange tube is about 70 ℃ and is divided into two flow paths, and the opening of the third valve 114 and the fourth valve 115 is controlled to fully open the third valve 114 and close the fourth valve 115, and at the moment, the gas-liquid mixture at the oxygen side fully flows through the third valve 114 and bypasses the second regenerative heat exchanger 103; then, the circulating water at the outlet of the desiccant regeneration device 301 is preheated by the oxygen-side gas-liquid mixture in the circulating water preheater 302, the gas-liquid mixture is further cooled to about 55 ℃ in the air cooler 104, then the gas-liquid mixture enters the oxygen-side gas-liquid separator 106, the oxygen to be treated at the outlet of the oxygen-side gas-liquid separator 106 enters the corresponding oxygen-side gas treatment device 108 for purification treatment, and finally the purified oxygen is stored in the oxygen storage tank 110; the hydrogen side and the reflux lye at the outlet of the gas-liquid separator at the oxygen side are mixed and then divided into two paths, the two paths respectively flow through the first heat-return heat exchanger 102 and the second heat-return heat exchanger 103 but basically do not generate heat exchange, the temperature is maintained at about 55 ℃, and then the two paths are converged and pumped into the electrolytic tank 101 through the lye circulating pump 111 to participate in the electrolytic reaction.
When the electrolytic tank 101 is in a low-load working period, as shown in fig. 6, the normal working temperature of the electrolytic tank is still set to 85 ℃ because of the electrolysis of water in the tank to generate hydrogen and oxygen, the heat generated by the reaction in the electrolytic tank 101 is greatly reduced due to the obvious reduction of electric power, the heat dissipation of the tank to the external environment is basically unchanged, and the temperature of the reflux alkali liquid at the inlet of the electrolytic tank 101 needs to be properly increased in order to maintain the stable temperature of the tank; accordingly, the hydrogen-side gas-liquid mixture and the oxygen-side gas-liquid mixture respectively flow out of the electrolytic tank 101, enter the evaporator 204 and the generator 201, exchange heat in the corresponding heat pipes and are cooled, and the adjustment process of the hydrogen-side flow path is described as follows: the gas-liquid mixture at the hydrogen side sequentially enters the fourth heat exchange tube 204-h and the first heat exchange tube 201-h for gradual cooling, after cooling, the temperature of the gas-liquid mixture at the outlet 201-b of the first heat exchange tube of the generator 201 is about 70 ℃ and is divided into two flow paths, at the moment, the opening of the first valve 112 and the opening of the second valve 113 are controlled, so that the first valve 112 is closed, the second valve 113 is opened, and at the moment, the gas-liquid mixture at the hydrogen side completely flows through the second valve 113 and enters the first regenerative heat exchanger 102 for heat exchange and is cooled to about 62 ℃; then, the circulating water at the outlet of the drying agent regenerating device 301 is preheated by the hydrogen side gas-liquid mixture in the circulating water preheater 302, the temperature is reduced to about 55 ℃, the air cooler 104 is stopped, then the hydrogen enters the hydrogen side gas-liquid separator 105, the hydrogen to be treated at the outlet of the hydrogen side gas-liquid separator 105 enters the corresponding hydrogen side gas treatment device 107 for purification treatment, and finally the hydrogen enters the hydrogen storage tank 109; the oxygen-side flow path is similar to the above, and the following description is given of the oxygen-side flow path: the gas-liquid mixture at the oxygen side flows out of the anode of the electrolytic tank 101, sequentially enters the third heat exchange tube 204-g and the second heat exchange tube 201-i for gradual cooling, the temperature of the gas-liquid mixture at the outlet 201-d of the second heat exchange tube is about 70 ℃ and is divided into two flow paths, and the opening of the third valve 114 and the fourth valve 115 is controlled to close the third valve 114 and open the fourth valve 115, and at the moment, the gas-liquid mixture at the oxygen side completely flows through the fourth valve 115, exchanges heat in the second regenerative heat exchanger 103 and is cooled to about 62 ℃; then, the circulating water at the outlet of the desiccant regeneration device 301 is preheated by the oxygen-side gas-liquid mixture in the circulating water preheater 302, the temperature is reduced to about 55 ℃, the circulating water enters the oxygen-side gas-liquid separator 106, the oxygen to be treated at the outlet of the oxygen-side gas-liquid separator 106 enters the corresponding oxygen-side gas treatment device 108 for purification treatment, and finally the oxygen is stored in the oxygen storage tank 110; the hydrogen side is mixed with the reflux alkali liquor at the outlet of the gas-liquid separator at the oxygen side, the temperature is about 55 ℃, the mixture is divided into two paths, the two paths respectively flow through the first heat-regenerative heat exchanger 102 and the second heat-regenerative heat exchanger 103 to exchange heat with the corresponding gas-liquid mixture, the temperature is raised to about 65 ℃, and then the mixture is converged and pumped into the electrolytic tank 101 through the alkali liquor circulating pump 111 to participate in the electrolytic reaction.
In the above embodiment, the absorption heat pump subsystem keeps normal operation, the heat recovery is performed on the hydrogen production system, the refrigerant in the evaporator 204 absorbs the heat energy of the driving heat source from the outlet of the electrolytic tank 101, the evaporation temperature is about 75 ℃, the dilute solution in the generator 201 absorbs the heat energy of the driving heat source passing through the evaporator 204, part of the dilute solution is evaporated to form refrigerant vapor and concentrated solution, the concentrated solution temperature of the first outlet 201-e is about 68 ℃, the refrigerant vapor from the generator 201 is condensed in the water-cooled condenser 202, the temperature is reduced to about 25 ℃, the condensed refrigerant vapor is pumped into the evaporator 204, the absorption temperature can reach more than 110 ℃ in the absorber 205, the concentrated solution absorbs the refrigerant vapor from the evaporator, the concentration is reduced and a large amount of heat energy higher than the grade of the driving heat source is discharged, and the preheated circulating water is heated by the hot water circulating subsystem to obtain high-temperature circulating water.
The heat exchange medium in the hot water circulation subsystem is circulating water, wherein the temperature of the circulating water used by the gas desiccant regeneration device 301 is about 105 ℃, the pressure is higher than the atmospheric pressure, the circulating water in the circulating water preheater 302 is preheated and heated, and then the circulating water enters the absorber 205 for heating, and the high-grade heat energy is absorbed to form high-temperature circulating water at about 105 ℃.
In the process, the absorption heat pump subsystem recovers the waste heat in the hydrogen production process of alkaline electrolyzed water, obtains higher-grade heat energy and is used for dehydration and regeneration of the gas desiccant in the gas desiccant regeneration device 301; the flow of the gas-liquid mixture in the corresponding regenerative heat exchanger is controlled by the regulating valve, and the temperature of the returned alkali liquid at the inlet of the electrolytic tank 101 is controlled and regulated, so that the electrolytic tank 101 is maintained in a set working temperature zone, the recovery and grade improvement of waste heat are realized, the temperature control capability of the alkaline water electrolysis hydrogen production system is improved, the adaptability of the system under the variable load working condition is enhanced, and the comprehensive energy utilization efficiency of the system is improved.
It will be readily appreciated by those skilled in the art that the foregoing description is merely a preferred embodiment of the application and is not intended to limit the application, but any modifications, equivalents, improvements or alternatives falling within the spirit and principles of the application are intended to be included within the scope of the application.
Claims (10)
1. An alkaline water electrolysis hydrogen production system based on an absorption heat pump, which is characterized by comprising an alkaline water electrolysis hydrogen production subsystem and an absorption heat pump subsystem, wherein:
the absorption heat pump subsystem comprises a generator and an evaporator, and a hydrogen heat exchange tube and an oxygen heat exchange tube are arranged in the generator and the evaporator;
the alkaline electrolyzed water hydrogen production subsystem comprises an electrolytic tank, a first regenerative heat exchanger, a second regenerative heat exchanger and a gas-liquid separation treatment device; the hydrogen pipeline at the outlet of the electrolytic tank is sequentially connected with the hydrogen heat exchange tube in the evaporator and the hydrogen heat exchange tube in the generator, and the oxygen pipeline at the outlet of the electrolytic tank is connected with the oxygen heat exchange tube in the evaporator and the oxygen heat exchange tube in the generator; the output pipeline of the hydrogen heat exchange tube in the generator is divided into two branches, one branch of the output pipeline of the hydrogen heat exchange tube in the generator passes through the first regenerative heat exchanger to participate in heat exchange, and the other branch of the output pipeline of the hydrogen heat exchange tube in the generator is output to the gas-liquid separation treatment device; the output pipeline of the oxygen heat exchange tube in the generator is divided into two branches, one branch of the output pipeline of the oxygen heat exchange tube in the generator passes through the second regenerative heat exchanger to participate in heat exchange, the other branch of the output pipeline of the oxygen heat exchange tube in the generator is output to the gas-liquid separation treatment device, the liquid separated by the gas-liquid separation treatment device is divided into two branches, one branch of the liquid separated by the gas-liquid separation treatment device is input into the electrolytic tank after heat exchange by the first regenerative heat exchanger, the other branch of the liquid separated by the gas-liquid separation treatment device is input into the electrolytic tank after heat exchange by the second regenerative heat exchanger, and valves are arranged on the two branches respectively divided by the output pipeline of the hydrogen heat exchange tube and the oxygen heat exchange tube in the generator.
2. The system of claim 1, wherein the generator and the evaporator are arranged in sequence along a refrigerant flow direction, the hydrogen heat exchange tube in the evaporator being arranged upstream if the hydrogen heat exchange tube in the generator is arranged downstream; if the hydrogen heat exchange tube in the generator is arranged at the upstream, the hydrogen heat exchange tube in the evaporator is arranged at the downstream.
3. The system of claim 1 or 2, wherein the absorption heat pump subsystem further comprises a condenser, the condenser being disposed between the generator and the evaporator.
4. The system of claim 1, further comprising a hot water circulation subsystem, the hot water circulation subsystem comprising a desiccant regeneration device, the absorption heat pump subsystem further comprising an absorber, the absorber being disposed downstream of the evaporator, a fifth heat exchange tube being disposed within the absorber, the circulating water of the hot water circulation subsystem flowing into the desiccant regeneration device after heat exchange within the fifth heat exchange tube.
5. The system of claim 4, wherein the hot water circulation subsystem further comprises a circulating water preheater, the circulating water preheater is arranged between the first regenerative heat exchanger and the second regenerative heat exchanger and the gas-liquid separation treatment device, and the two branches of the output pipeline of the hydrogen heat exchange tube in the generator are divided into two branches which are combined after passing through the first regenerative heat exchanger and flow into the circulating water preheater for heat exchange; the output pipeline of the oxygen heat exchange pipe in the generator is divided into two branches, and the two branches are combined and flow into the circulating water preheater for heat exchange after passing through the second regenerative heat exchanger.
6. The system of claim 4, wherein the absorption heat pump subsystem further comprises a solution heat exchanger disposed between the absorber and the generator such that a dilute solution of the refrigerant output by the absorber exchanges heat with a concentrated solution of the refrigerant output by the generator prior to being input to the generator, the concentrated solution of the refrigerant after heat exchange being input to the absorber.
7. The system of any one of claims 4 to 6, wherein a desiccant output line of the desiccant regeneration device is connected to the gas-liquid separation treatment device for drying the gas of the gas-liquid separation treatment device.
8. The system of claim 1, wherein the gas-liquid separation treatment device comprises an air cooler, a hydrogen separation treatment sub-device, and an oxygen separation treatment sub-device, the hydrogen separation treatment sub-device and the oxygen separation treatment sub-device being disposed in parallel downstream of the air cooler.
9. A system according to claim 3, wherein the operating pressure on the evaporator and absorber side is higher than the operating pressure on the condenser and generator side.
10. A method of regulating an absorption heat pump-based alkaline water electrolysis hydrogen production system according to any one of claims 1 to 9, comprising:
when the electrolysis power of the electrolysis bath is sufficient, closing valves on the branches passing through the first regenerative heat exchanger and the second regenerative heat exchanger, and opening valves on the branches not passing through the first regenerative heat exchanger and the second regenerative heat exchanger;
when the electrolysis power of the electrolysis bath is insufficient, valves on the branches of the first heat recovery heat exchanger and the second heat recovery heat exchanger are opened, and valves on the branches of the first heat recovery heat exchanger and the second heat recovery heat exchanger which are not passed through are opened or closed and the opening degree of the valves is controlled.
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014076389A1 (en) * | 2012-11-16 | 2014-05-22 | Snecma | Electrical installation having a cooled fuel cell comprising an absorption heat engine |
| CN109913886A (en) * | 2019-02-01 | 2019-06-21 | 大连理工大学 | A kind of two-way joint hydrogen production process of low grade heat energy driving |
| CN111235590A (en) * | 2020-03-25 | 2020-06-05 | 深圳市凯豪达氢能源有限公司 | Alkaline water electrolysis hydrogen production waste heat utilization system and method |
| CN111336571A (en) * | 2020-04-07 | 2020-06-26 | 中国华能集团清洁能源技术研究院有限公司 | Water electrolysis hydrogen production waste heat utilization system and working method thereof |
| CN111748822A (en) * | 2020-06-04 | 2020-10-09 | 同济大学 | Comprehensive heat management system of large alkaline electrolyzed water hydrogen production device |
| CN212404297U (en) * | 2020-05-21 | 2021-01-26 | 考克利尔竞立(苏州)氢能科技有限公司 | Circulating water utilization device in electrolytic hydrogen production process |
| CN112899726A (en) * | 2021-01-18 | 2021-06-04 | 阳光电源股份有限公司 | Water electrolysis hydrogen production system and control method thereof |
| CN113137783A (en) * | 2021-05-17 | 2021-07-20 | 中国华能集团清洁能源技术研究院有限公司 | System and method for recycling hydrogen production waste heat of electrolyzed water by using heat pump |
| CN113322475A (en) * | 2021-05-24 | 2021-08-31 | 浙江工业大学 | High-temperature solid oxide water electrolysis hydrogen production system and process coupling solar energy amino-thermal chemical energy storage and kalina circulation |
| CN113694553A (en) * | 2021-08-18 | 2021-11-26 | 江苏科技大学 | Printing and dyeing weak alkali solution absorption type heat pump multi-effect distillation system and working method thereof |
-
2022
- 2022-04-14 CN CN202210393026.1A patent/CN114807962B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014076389A1 (en) * | 2012-11-16 | 2014-05-22 | Snecma | Electrical installation having a cooled fuel cell comprising an absorption heat engine |
| CN109913886A (en) * | 2019-02-01 | 2019-06-21 | 大连理工大学 | A kind of two-way joint hydrogen production process of low grade heat energy driving |
| CN111235590A (en) * | 2020-03-25 | 2020-06-05 | 深圳市凯豪达氢能源有限公司 | Alkaline water electrolysis hydrogen production waste heat utilization system and method |
| CN111336571A (en) * | 2020-04-07 | 2020-06-26 | 中国华能集团清洁能源技术研究院有限公司 | Water electrolysis hydrogen production waste heat utilization system and working method thereof |
| CN212404297U (en) * | 2020-05-21 | 2021-01-26 | 考克利尔竞立(苏州)氢能科技有限公司 | Circulating water utilization device in electrolytic hydrogen production process |
| CN111748822A (en) * | 2020-06-04 | 2020-10-09 | 同济大学 | Comprehensive heat management system of large alkaline electrolyzed water hydrogen production device |
| CN112899726A (en) * | 2021-01-18 | 2021-06-04 | 阳光电源股份有限公司 | Water electrolysis hydrogen production system and control method thereof |
| CN113137783A (en) * | 2021-05-17 | 2021-07-20 | 中国华能集团清洁能源技术研究院有限公司 | System and method for recycling hydrogen production waste heat of electrolyzed water by using heat pump |
| CN113322475A (en) * | 2021-05-24 | 2021-08-31 | 浙江工业大学 | High-temperature solid oxide water electrolysis hydrogen production system and process coupling solar energy amino-thermal chemical energy storage and kalina circulation |
| CN113694553A (en) * | 2021-08-18 | 2021-11-26 | 江苏科技大学 | Printing and dyeing weak alkali solution absorption type heat pump multi-effect distillation system and working method thereof |
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