Reversible compressor/expander work-doing system

文档序号：804755 发布日期：2021-03-26 浏览：20次中文

阅读说明：本技术 可逆压缩/膨胀机做功系统 (Reversible compressor/expander work-doing system ) 是由贾鹏于 2019-09-10 设计创作，主要内容包括：本发明涉及一种可逆压缩/膨胀机做功系统,包括高压换热罐、1号正反向可逆压缩/膨胀机、2号正反向可逆压缩/膨胀机、1号变温器、2号变温器和低压换热罐。高压换热罐顺次连接1号变温器、1号正反向可逆压缩/膨胀机、2号变温器和2号正反向可逆压缩/膨胀机,形成正向流动循环。低压换热罐顺次连接2号变温器、2号正反向可逆压缩/膨胀机、1号变温器和1号正反向可逆压缩/膨胀机,形成反向流动循环。本发明通过可逆压缩/膨胀机做功,驱动做功设备工作或带动发电设备发电。(The invention relates to a work doing system of a reversible compression/expansion machine, which comprises a high-pressure heat exchange tank, a No. 1 forward and reverse reversible compression/expansion machine, a No. 2 forward and reverse reversible compression/expansion machine, a No. 1 temperature changer, a No. 2 temperature changer and a low-pressure heat exchange tank. The high-pressure heat exchange tank is sequentially connected with the No. 1 temperature changer, the No. 1 forward and reverse reversible compression/expansion machine, the No. 2 temperature changer and the No. 2 forward and reverse reversible compression/expansion machine to form forward flow circulation. The low-pressure heat exchange tank is sequentially connected with the No. 2 temperature changer, the No. 2 forward and reverse reversible compression/expansion machine, the No. 1 temperature changer and the No. 1 forward and reverse reversible compression/expansion machine to form reverse flow circulation. The reversible compression/expansion machine is used for applying work to drive working equipment to work or drive power generation equipment to generate power.)

1. A work-doing system of a reversible compression/expansion machine is characterized in that: the work doing system comprises a high-pressure heat exchange tank (1), a No. 1 forward and reverse reversible compression/expansion machine (2), a No. 2 forward and reverse reversible compression/expansion machine (3), a No. 1 temperature changer (9), a No. 2 temperature changer (10) and a low-pressure heat exchange tank (7); the No. 1 forward and reverse reversible compression/expansion machine (2) is provided with a No. 1 expansion inlet (13), a No. 1 expansion outlet (14), a No. 1 compression inlet (15) and a No. 1 compression outlet (16); the No. 2 reversible compression/expansion machine (3) is provided with a No. 2 expansion inlet (13 '), a No. 2 expansion outlet (14'), a No. 2 compression inlet (15 ') and a No. 2 compression outlet (16');

an outlet of the high-pressure heat exchange tank (1) is connected to a hydrogen absorption inlet of a No. 1 temperature changer (9) through a valve (8), a hydrogen absorption outlet of the No. 1 temperature changer (9) is connected to a No. 1 expansion inlet (13) of a No. 1 forward and reverse reversible compression/expansion machine (2), a No. 1 expansion outlet (14) of the No. 1 forward and reverse reversible compression/expansion machine (2) is connected to a hydrogen discharge inlet of a No. 2 temperature changer (10) through a valve, a hydrogen discharge outlet of the No. 2 temperature changer (10) is connected to a No. 2 compression inlet (15 ') of a No. 2 forward and reverse reversible compression/expansion machine (3), and a No. 2 compression outlet (16') of the No. 2 forward and reverse reversible compression/expansion machine (3) is connected to an inlet of the high-pressure heat exchange tank (1) through a valve;

an outlet of the low-pressure heat exchange tank (7) is connected to a hydrogen absorption inlet of a No. 2 temperature changer (10) through a valve, a hydrogen absorption outlet of the No. 2 temperature changer (10) is connected to a No. 2 expansion inlet (13 ') of a No. 2 reversible compression/expansion machine (3), a No. 2 expansion outlet (14') of the No. 2 reversible compression/expansion machine (3) is connected to a hydrogen discharge inlet of a No. 1 temperature changer (9) through a valve, a hydrogen discharge outlet of the No. 1 temperature changer (9) is connected to a No. 1 compression inlet (15) of the No. 1 reversible compression/expansion machine (2), and a No. 1 compression outlet (16) of the No. 1 reversible compression/expansion machine (2) is connected to an inlet of the low-pressure heat exchange tank (7) through a valve;

a metal hydrogen storage material reaction bed layer (5) B is arranged in the temperature changer (9) No. 1, and a metal hydrogen storage material reaction bed layer (6) A is arranged in the temperature changer (10) No. 2;

the No. 1 forward and reverse reversible compression/expansion machine (2) and the No. 2 forward and reverse reversible compression/expansion machine (3) are coaxially connected with the power output shaft.

2. The reversible compression/expansion machine work system of claim 1, wherein: the metal B hydrogen storage material of the metal B hydrogen storage material reaction bed layer (5) comprises but is not limited to titanium metal hydrogen storage material; the A metal hydrogen storage material of the A metal hydrogen storage material reaction bed layer (6) comprises but is not limited to rare earth metal hydrogen storage material.

3. The reversible compression/expansion machine work system of claim 1, wherein: the work-doing system further comprises a generator (4); the No. 1 forward and reverse reversible compression/expansion machine (2) and the No. 2 forward and reverse reversible compression/expansion machine (3) are coaxially connected with a generator (4), and a circuit of the generator (4) is connected to an external power grid and/or a storage battery.

4. The reversible compression/expansion machine work system of claim 1, wherein: the work system further includes a cooler (29); the cooler (29) is arranged outside the low-pressure heat exchange tank (7).

5. The reversible compression/expansion machine work system of claim 1, wherein: the No. 1 forward and reverse reversible compression/expansion machine (2) and the No. 2 forward and reverse reversible compression/expansion machine (3) alternately perform expansion and compression processes;

the No. 1 positive and negative reversible compression/expansion machine (2) performs gas expansion work when the intake airflow flows in the positive direction and performs gas compression when the intake airflow flows in the negative direction; the No. 2 positive and negative reversible compression/expansion machine (3) performs gas compression when the intake airflow flows in the positive direction and performs gas expansion work when the intake airflow flows in the negative direction.

6. The reversible compression/expansion machine work system of any one of claims 1 to 5, wherein: the work doing system is further provided with a protective cover (28), and the protective cover (28) is provided with a combustible gas alarm (25) and a hydrogen adding port (24); the protective cover (28) is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation, and the pipeline in the protective cover (28) is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation; the protective cover (28) is also provided with a temperature regulator (26); the temperature regulator (26) emits high-temperature cold energy, and the low-temperature heat exchange tank (7) emits low-temperature cold energy; the protective cover (28) is filled with system heat supplementing hydrogen, and heat entering from the external environment through the temperature regulator (26) and heat generated by mechanical equipment are supplemented into the high-temperature heat exchange tank (1) so that the system can continuously work and operate; the system for supplementing hot hydrogen comprises, but is not limited to, hydrogen and other gases or liquids or solids besides hydrogen, or mixtures of two or more of the above, or mixtures of three.

7. The reversible compression/expansion machine work system of claim 6, wherein: the reversible compression/expansion machine work-doing system does work outwards through a Kohler pump cycle; the Kohlenbu cycle is defined as that at least two metal hydrides exist in the system, at least four state points exist, and the hydrogen absorption heat release and the hydrogen desorption heat absorption of the at least four state points are kept or basically kept in heat balance in the system through a circulating heat exchange medium, namely the heat of the hydrogen absorption heat release of one state point is transferred to the hydrogen desorption heat absorption process in the other three state points by the circulating heat exchange medium;

the hydrogen desorption endothermic state in at least four existing state points does not or basically does not absorb heat into the environment, but transfers the heat of the hydrogen absorption exothermic heat in at least four state points to the hydrogen desorption endothermic process in at least four state points;

the hydrogen absorption and heat release state in at least four existing state points does not or basically does not dissipate heat to the environment, but transfers heat to the hydrogen desorption and heat absorption process in at least four existing state points, and the hydrogen desorption and heat absorption process in at least four existing state points can completely or almost completely receive the transferred heat;

the hydrogen absorption and heat release state points in the at least four state points can transfer heat to the hydrogen release and heat absorption state points, the heat is basically internal balance, and all or most of the heat absorption and heat release balance is completed in the system, so that heat dissipation to the environment or heat absorption from the environment is hardly needed;

the system can do work through the working cycle formed by at least four state points, the working mode is that hydrogen is used as a medium to do work, the temperature-pressure of the hydrogen can be circularly changed by the at least four state points, so that the working cycle is formed, and the working equipment can be an impeller type swing mechanism or a piston type or other modes; at least four state points can be restored to the original state points through the power cycle, and the hydrogen absorption and heat release state points and the hydrogen desorption and heat absorption state points; allowing the system to release low-temperature cold energy into the environment and absorb heat from the environment;

besides using gaseous hydrogen as a circulating heat exchange medium of a work-doing system, other gases can be used as the circulating heat exchange medium; in addition, other substances including but not limited to stable solids, liquids or liquid organic hydrides can be used instead of hydrogen as the circulating heat exchange medium of the work-doing system; the heat exchange mode can be direct heat exchange or partition wall heat exchange, and the heat exchange medium for partition wall heat exchange can be gas, liquid, solid or a mixture of the above or a mixture of every two;

the state point connections of the pressure-temperature diagram of the at least two metal hydrides may or may not intersect;

the process of doing work by the system hydrogen comprises the work of circularly exchanging heat with the hydrogen and the work of doing work with the hydrogen.

8. The reversible compression/expansion machine work system of claim 7, wherein: the Kohlenberg cycle is represented by two metal hydrides with different properties, each metal hydride has two working state points, the lowest hydrogen release temperature and the highest hydrogen absorption temperature of the metal hydride a define a working range, the two temperatures can be adjusted, so that the working range can be large or small, the highest hydrogen release temperature and the lowest hydrogen absorption temperature of the metal hydride b influence a power temperature difference, the hydrogen release endothermic state point temperature of the metal hydride b is lower than the hydrogen absorption exothermic state point temperature of the metal hydride a, the hydrogen release endothermic state point pressure of the metal hydride b is higher than the hydrogen absorption exothermic state point pressure of the metal hydride a, the hydrogen absorption exothermic state point temperature of the metal hydride b is higher than the hydrogen release endothermic state point temperature of the metal hydride a, the hydrogen absorption exothermic state point pressure of the metal hydride b is higher than the hydrogen release endothermic state point pressure of the metal hydride a, that is, the highest temperature of the metal hydride a is higher than that of the metal hydride b, while the highest pressure of the metal hydride a is lower than that of the metal hydride b, the lowest temperature of the metal hydride a is lower than that of the metal hydride b, the lowest pressure of the metal hydride a is lower than that of the metal hydride b, the temperature difference between the highest hydrogen absorption temperature of the metal hydride a and the highest hydrogen desorption temperature of the metal hydride b can be equal to or not equal to the temperature difference between the lowest hydrogen desorption temperature of the metal hydride a and the lowest hydrogen absorption temperature of the metal hydride b, and the system performs more work when the pressure ratio is constant; when the expansion work is done, the high-temperature high-enthalpy hydrogen is adopted to increase the work doing capacity, and when the compression work is consumed, the low-temperature low-enthalpy hydrogen is adopted to reduce the power consumption and maximize the net work of the system; under the condition of low temperature, the low-temperature low-enthalpy hydrogen is adopted during expansion work to increase the work doing capacity, and the lower-temperature lower-enthalpy hydrogen is adopted during compression work consumption to reduce the work consumption and maximize the net work of the system; the system is provided with two hydrogen absorption and heat release state points and two hydrogen release and heat absorption state points, the high-temperature hydrogen absorption and heat release of the metal hydride a are used for the high-temperature hydrogen release and heat absorption of the metal hydride b through the circulation of heat exchange hydrogen, the low-temperature hydrogen absorption and heat release of the metal hydride b are used for the low-temperature hydrogen release and heat absorption of the metal hydride a through the circulation of the heat exchange hydrogen, and the heat released and absorbed by the absorbed and released hydrogen keeps equal or almost equal pairwise; although the metal hydride a has only two state points and the metal hydride b has only two state points, the two state points are continuously switched from one state point to the other state point along with the continuous change of the hydrogen absorption and release state points, and the two state points are continuously switched, two metal hydrides are incorporated into a system, so that a cycle can be formed, each state point can be automatically recovered and can work outside the system, four state points are continuously circulated in the system, and heat is continuously exchanged in the system, so that a work cycle is realized, the hydrogen absorption and heat release in the high-temperature state of the metal hydride a and the hydrogen desorption and heat absorption in the high-temperature state of the metal hydride b are a group, heat exchange is carried out between the metal hydride a and the hydrogen desorption and the heat absorption in the low-temperature state of the metal hydride b are a group, exchange heat with each other at low temperature.

9. A liquid heat exchange medium work application system is characterized in that: comprises a high-pressure expander (11), a low-pressure expander (12), a No. 1 liquid heat exchange medium circulating pump (17), a No. 2 liquid heat exchange medium circulating pump (18), a metal hydrogen storage material reaction bed A, a metal hydrogen storage material reaction bed B and a cooler (29); the metallic hydrogen storage material reaction bed A comprises a hydrogen reaction bed A1 (19) and a hydrogen reaction bed A2 (20), and the metallic hydrogen storage material reaction bed B comprises a hydrogen reaction bed B1 (21) and a hydrogen reaction bed B2 (22);

the hydrogen discharge outlet of the hydrogen reaction bed A1 (19) is connected to the inlet of the high-pressure expander (11), and the outlet of the high-pressure expander (11) is connected to the hydrogen absorption inlet of the hydrogen reaction bed B1 (21); the hydrogen discharge outlet of the hydrogen reaction bed B1 (21) is connected to the inlet of the low-pressure expansion machine (12), the outlet of the low-pressure expansion machine (12) is connected to the tube-side inlet of the cooler (29), and the tube-side outlet of the cooler (29) is connected to the hydrogen absorption inlet of the hydrogen reaction bed A1 (19);

the hydrogen discharge outlet of the hydrogen reaction bed A2 (20) is connected to the inlet of the high-pressure expander (11), and the outlet of the high-pressure expander (11) is connected to the hydrogen absorption inlet of the hydrogen reaction bed B2 (22); the hydrogen discharge outlet of the hydrogen reaction bed B2 (22) is connected to the inlet of the low-pressure expansion machine (12), the outlet of the low-pressure expansion machine (12) is connected to the tube-side inlet of the cooler (29), and the tube-side outlet of the cooler (29) is connected to the hydrogen absorption inlet of the hydrogen reaction bed A1 (19);

air enters from a shell side inlet of the cooler (29), cooled liquid nitrogen and liquid oxygen exit from a shell side liquid air outlet of the cooler (29) and enter a liquid oxygen and liquid nitrogen separation preparation system (36), and the separated liquid nitrogen and liquid oxygen enter a liquid nitrogen tank (37) and a liquid oxygen tank (38) respectively;

the hydrogen reaction bed A1 (19), the hydrogen reaction bed A2 (20), the hydrogen reaction bed B1 (21) and the hydrogen reaction bed B2 (22) are respectively connected with the No. 1 liquid heat exchange medium circulating pump (17) and the No. 2 liquid heat exchange medium circulating pump (18) in a circulating mode through liquid heat exchange medium pipelines; the No. 1 liquid heat exchange medium circulating pump (17) and the No. 2 liquid heat exchange medium circulating pump (18) are used for exchanging heat of circulating media in the hydrogen reaction bed A1 (19), the hydrogen reaction bed A2 (20) and the hydrogen reaction bed B1 (21) and the hydrogen reaction bed B2 (22) after the hydrogen reaction bed A1 (19), the hydrogen reaction bed A2 (20), the hydrogen reaction bed B1 (21) and the hydrogen reaction bed B2 (22) absorb/release hydrogen;

the liquid heat exchange medium work doing system is also provided with a protective cover (28), and the protective cover (28) is provided with a combustible gas alarm (25) and a hydrogen adding port (24); the protective cover (28) is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation, and the pipeline in the protective cover (28) is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation; the protective cover (28) is also provided with a temperature regulator (26);

the protective cover (28) is filled with system heat supplementing hydrogen, and heat entering from the external environment through the temperature regulator (26) and heat generated by mechanical equipment are supplemented to the No. 1 liquid heat exchange medium circulating pump (17) and the No. 2 liquid heat exchange medium circulating pump (18) so that the system can continuously work; the cold energy generated by the system work is transmitted to the outside through a cooler (29); the system for supplementing hot hydrogen comprises, but is not limited to, hydrogen and other gases or liquids or solids besides hydrogen, or mixtures of two or more of the above, or mixtures of three.

10. The liquid heat exchange medium work system of claim 9, wherein: and a shell-side inlet of a cooler (29) in the liquid heat exchange medium work-doing system is also used for receiving external hydrogen, and liquid hydrogen cooled by the cooler (29) is discharged from a shell-side liquid hydrogen outlet of the cooler (29) and enters a liquid hydrogen storage tank (30).

Technical Field

The invention belongs to the technical field of comprehensive utilization of energy, and relates to a work-doing system of a reversible compression/expansion machine.

Background

The nature is full of unlimited normal temperature energy sources, air, seawater and other unlimited normal temperature energy sources, and the energy source has development potential. Most of the energy on the earth comes from the sun, and nowadays, the energy is increasingly scarce, and new renewable green clean power generation technology is increasingly paid attention. In the existing new energy, the application of the water energy and wind energy power generation technology is common, and the technology is mature. The hydropower development potential is not large, the wind power is too dispersed, the hydropower development potential can be applied only in some specific areas, and the hydropower and wind power generation device has large investment and wide floor area. Air energy gradually enters the visual field of people, and the air energy water heater is also commonly applied at present, and the principle is that heat energy in the air is utilized to heat water through a heat pump. However, the technology of generating electricity by utilizing air energy is very few, the technology is not mature enough, and the popularization and the application are difficult.

The Chinese patent application with publication number CN 107939525A discloses a working system and method of a gas expander in a compressed air energy storage system, the working system of the gas expander in the compressed air energy storage system comprises a high-pressure gas source, a steam source, a mixer, a gas ejector and a gas expander, the gas ejector is provided with an inner cavity, a first inlet, a second inlet and an outlet which are communicated with the inner cavity, the high-pressure gas source and the steam source are communicated with the first inlet through the mixer, a waste gas outlet of the gas expander is communicated with the second inlet, and a gas inlet of the gas expander is communicated with the outlet. In this patent application, the high-pressure gas medium of high-pressure gas source output mixes the back with the high-temperature steam of steam source output, in as high-pressure working gas stream input gas sprayer, has improved the entrainment ability to low pressure exhaust gas, and then has improved the efficiency of doing work. However, the patent application of the invention can not realize the work-doing power generation of the compression/expansion machine through the heat generated by the hydrogen absorption and desorption of the metal hydrogen storage material.

Disclosure of Invention

The invention aims to provide a reversible compression/expansion machine work system, which takes hydrogen as a circulating working medium, utilizes the hydrogen absorption/release characteristics of a metal hydrogen storage material, drives work equipment to work or drives power generation equipment to generate power by the work of the reversible compression/expansion machine, fully utilizes natural energy and industrial waste heat, and is beneficial to energy conservation and emission reduction and creation of economic benefits.

The embodiment of the application provides a work doing system of a reversible compression/expansion machine, which comprises a high-pressure heat exchange tank, a No. 1 forward and reverse reversible compression/expansion machine, a No. 2 forward and reverse reversible compression/expansion machine, a No. 1 temperature changer, a No. 2 temperature changer and a low-pressure heat exchange tank; the No. 1 positive and negative reversible compression/expansion machine is provided with a No. 1 expansion inlet, a No. 1 expansion outlet, a No. 1 compression inlet and a No. 1 compression outlet; the No. 2 reversible compression/expansion machine is provided with a No. 2 expansion inlet, a No. 2 expansion outlet, a No. 2 compression inlet and a No. 2 compression outlet.

An outlet of the high-pressure heat exchange tank is connected to a hydrogen absorption inlet of a temperature changer No. 1 through a valve, a hydrogen absorption outlet of the temperature changer No. 1 is connected to an expansion inlet No. 1 of a reversible compression/expansion machine No. 1, an expansion outlet No. 1 of the reversible compression/expansion machine No. 1 is connected to a hydrogen discharge inlet of a temperature changer No. 2 through a valve, a hydrogen discharge outlet of the temperature changer No. 2 is connected to a compression inlet No. 2 of the reversible compression/expansion machine No. 2, and a compression outlet No. 2 of the reversible compression/expansion machine No. 2 is connected to an inlet of the high-pressure heat exchange tank through a valve.

An outlet of the low-pressure heat exchange tank is connected to a hydrogen absorption inlet of a No. 2 temperature changer through a valve, a hydrogen absorption outlet of the No. 2 temperature changer is connected to a No. 2 expansion inlet of a No. 2 reversible compression/expansion machine, a No. 2 expansion outlet of the No. 2 reversible compression/expansion machine is connected to a hydrogen discharge inlet of the No. 1 temperature changer through a valve, a hydrogen discharge outlet of the No. 1 temperature changer is connected to a No. 1 compression inlet of the No. 1 reversible compression/expansion machine, and a No. 1 compression outlet of the No. 1 reversible compression/expansion machine is connected to an inlet of the low-pressure heat exchange tank through a valve.

A metal hydrogen storage material reaction bed layer B is arranged in the temperature changer No. 1, and a metal hydrogen storage material reaction bed layer A is arranged in the temperature changer No. 2.

The No. 1 forward and reverse reversible compression/expansion machine and the No. 2 forward and reverse reversible compression/expansion machine are coaxially connected with the power output shaft.

Further, the metal B hydrogen storage material of the metal B hydrogen storage material reaction bed layer includes but is not limited to titanium metal hydrogen storage material; the A metal hydrogen storage material of the A metal hydrogen storage material reaction bed layer comprises but is not limited to rare earth metal hydrogen storage material.

Further, the power system also comprises a generator; the No. 1 forward and reverse reversible compression/expansion machine and the No. 2 forward and reverse reversible compression/expansion machine are coaxially connected with a generator, and a generator circuit is connected to an external power grid and/or a storage battery.

In addition, the work system also comprises a cooler; the cooler is disposed outside the low pressure heat exchange tank.

Further, the No. 1 forward and reverse reversible compression/expansion machine and the No. 2 forward and reverse reversible compression/expansion machine alternately perform expansion and compression processes; the No. 1 positive and negative reversible compression/expansion machine performs gas expansion work when the intake airflow flows in the positive direction, and performs gas compression when the intake airflow flows in the negative direction; the No. 2 reversible compression/expansion machine performs gas compression when the intake airflow flows forward and performs gas expansion work when the intake airflow flows backward.

Furthermore, the acting system is also provided with a protective cover, and the protective cover is provided with a combustible gas alarm and a hydrogen adding port; the protective cover is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation, and the pipeline in the protective cover is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation; the protective cover is also provided with a temperature regulator; the temperature regulator emits high-temperature cold energy, and the low-temperature heat exchange tank emits low-temperature cold energy; the protective cover is filled with system heat supplementing hydrogen, and heat entering from the external environment through the temperature regulator and heat generated by mechanical equipment are supplemented into the high-temperature heat exchange tank, so that the system can continuously work; the system for supplementing hot hydrogen comprises, but is not limited to, hydrogen and other gases or liquids or solids besides hydrogen, or mixtures of two or more of the above, or mixtures of three.

Further, the work-doing system of the reversible compression/expansion machine does work outwards through a Kohler pump cycle; the Kohlenbu cycle is defined as at least two metal hydrides in the system, at least four state points exist, and the hydrogen absorption heat release and the hydrogen desorption heat absorption of the at least four state points are kept or basically kept in heat balance in the system through a circulating heat exchange medium, namely the heat of the hydrogen absorption heat release of one state point is transferred to the hydrogen desorption heat absorption process in the other three state points by the circulating heat exchange medium.

The hydrogen evolving endothermic state of the at least four state points that is present does not or substantially does not endotherm to the environment, but rather transfers heat from the hydrogen evolution exothermic heat of the at least four state points to the hydrogen evolving endothermic process of the at least four state points.

The hydrogen-absorbing and heat-releasing states of the at least four existing state points do not or substantially do not dissipate heat to the environment, but rather transfer heat to the hydrogen-releasing and heat-absorbing processes of the at least four existing state points, and the hydrogen-releasing and heat-absorbing processes of the at least four existing state points are fully or almost fully capable of receiving the transferred heat.

The hydrogen absorption and heat release state points of the at least four state points can transfer heat to the hydrogen release and heat absorption state points, the heat is basically internal balance, and all or most of the heat absorption and heat release balance is completed inside the system, so that heat dissipation to the environment or heat absorption from the environment is hardly needed.

The system can do work through the working cycle formed by at least four state points, the working mode is that hydrogen is used as a medium to do work, the temperature-pressure of the hydrogen can be circularly changed by the at least four state points, so that the working cycle is formed, and the working equipment can be an impeller type swing mechanism or a piston type or other modes; at least four state points can be restored to the original state points through the power cycle, and the hydrogen absorption and heat release state points and the hydrogen desorption and heat absorption state points; allowing the system to release cold into the environment and absorb heat from the environment.

Besides using gaseous hydrogen as a circulating heat exchange medium of a work-doing system, other gases can be used as the circulating heat exchange medium; in addition, other substances including but not limited to stable solids, liquids or liquid organic hydrides can be used instead of hydrogen as the circulating heat exchange medium of the work-doing system; the heat exchange mode can be direct heat exchange or partition wall heat exchange, and the heat exchange medium for partition wall heat exchange can be gas, liquid, solid or mixture of the above or mixture of every two.

The state point connections of the pressure-temperature diagram of the at least two metal hydrides may or may not intersect; the process of doing work by the system hydrogen comprises the work of circularly exchanging heat with the hydrogen and the work of doing work with the hydrogen.

Further, the Kilo-Gem cycle is represented by two metal hydrides with different properties, each metal hydride has two working state points, the lowest hydrogen release temperature and the highest hydrogen absorption temperature of the metal hydride a define a working range, the two temperatures can be adjusted, so that the working range can be large or small, the highest hydrogen release temperature and the lowest hydrogen absorption temperature of the metal hydride b influence a working temperature difference, the hydrogen release endothermic state point temperature of the metal hydride b is lower than the hydrogen absorption exothermic state point temperature of the metal hydride a, the hydrogen release endothermic state point pressure of the metal hydride b is higher than the hydrogen absorption exothermic state point pressure of the metal hydride a, the hydrogen absorption exothermic state point temperature of the metal hydride b is higher than the hydrogen release endothermic state point temperature of the metal hydride a, the hydrogen absorption exothermic state point pressure of the metal hydride b is higher than the hydrogen release endothermic state point pressure of the metal hydride a, that is, the highest temperature of the metal hydride a is higher than that of the metal hydride b, while the highest pressure of the metal hydride a is lower than that of the metal hydride b, the lowest temperature of the metal hydride a is lower than that of the metal hydride b, the lowest pressure of the metal hydride a is lower than that of the metal hydride b, the temperature difference between the highest hydrogen absorption temperature of the metal hydride a and the highest hydrogen desorption temperature of the metal hydride b can be equal to or not equal to the temperature difference between the lowest hydrogen desorption temperature of the metal hydride a and the lowest hydrogen absorption temperature of the metal hydride b, and the system performs more work when the pressure ratio is constant; when the expansion work is done, the high-temperature high-enthalpy hydrogen is adopted to increase the work doing capacity, and when the compression work is consumed, the low-temperature low-enthalpy hydrogen is adopted to reduce the power consumption and maximize the net work of the system; under the condition of low temperature, the low-temperature low-enthalpy hydrogen is adopted during expansion work to increase the work doing capacity, and the lower-temperature lower-enthalpy hydrogen is adopted during compression work consumption to reduce the work consumption and maximize the net work of the system; the system is provided with two hydrogen absorption and heat release state points and two hydrogen release and heat absorption state points, the high-temperature hydrogen absorption and heat release of the metal hydride a are used for the high-temperature hydrogen release and heat absorption of the metal hydride b through the circulation of heat exchange hydrogen, the low-temperature hydrogen absorption and heat release of the metal hydride b are used for the low-temperature hydrogen release and heat absorption of the metal hydride a through the circulation of the heat exchange hydrogen, and the heat released and absorbed by the absorbed and released hydrogen keeps equal or almost equal pairwise; although the metal hydride a has only two state points and the metal hydride b has only two state points, the two state points are continuously switched from one state point to the other state point along with the continuous change of the hydrogen absorption and release state points, and the two state points are continuously switched, two metal hydrides are incorporated into a system, so that a cycle can be formed, each state point can be automatically recovered and can work outside the system, four state points are continuously circulated in the system, and heat is continuously exchanged in the system, so that a work cycle is realized, the hydrogen absorption and heat release in the high-temperature state of the metal hydride a and the hydrogen desorption and heat absorption in the high-temperature state of the metal hydride b are a group, heat exchange is carried out between the metal hydride a and the hydrogen desorption and the heat absorption in the low-temperature state of the metal hydride b are a group, exchange heat with each other at low temperature.

The embodiment of the application also provides a liquid heat exchange medium work-doing system, which comprises a high-pressure expander, a low-pressure expander, a No. 1 liquid heat exchange medium circulating pump, a No. 2 liquid heat exchange medium circulating pump, a metal hydrogen storage material reaction bed A, a metal hydrogen storage material reaction bed B and a cooler; the metallic hydrogen storage material reaction bed A comprises a hydrogen reaction bed A1 and a hydrogen reaction bed A2, and the metallic hydrogen storage material reaction bed B comprises a hydrogen reaction bed B1 and a hydrogen reaction bed B2.

The hydrogen discharge outlet of the hydrogen reaction bed A1 is connected to the inlet of the high-pressure expander, and the outlet of the high-pressure expander is connected to the hydrogen absorption inlet of the hydrogen reaction bed B1; the hydrogen discharge outlet of hydrogen reaction bed B1 was connected to the inlet of a low pressure expander, the outlet of the low pressure expander was connected to the tube-side inlet of a cooler, and the tube-side outlet of the cooler was connected to the hydrogen absorption inlet of hydrogen reaction bed a 1.

The hydrogen discharge outlet of the hydrogen reaction bed A2 is connected to the inlet of the high-pressure expander, and the outlet of the high-pressure expander is connected to the hydrogen absorption inlet of the hydrogen reaction bed B2; the hydrogen discharge outlet of hydrogen reaction bed B2 was connected to the inlet of a low pressure expander, the outlet of the low pressure expander was connected to the tube-side inlet of a cooler, and the tube-side outlet of the cooler was connected to the hydrogen absorption inlet of hydrogen reaction bed a 1.

Air enters from a shell pass inlet of the cooler, cooled liquid nitrogen and liquid oxygen exit from a shell pass liquid air outlet of the cooler and enter a liquid oxygen and liquid nitrogen separation preparation system, and the separated liquid nitrogen and liquid oxygen enter a liquid nitrogen tank and a liquid oxygen tank respectively.

The hydrogen reaction bed A1, the hydrogen reaction bed A2, the hydrogen reaction bed B1 and the hydrogen reaction bed B2 are respectively connected with the No. 1 liquid heat exchange medium circulating pump and the No. 2 liquid heat exchange medium circulating pump in a circulating manner through liquid heat exchange medium pipelines; and the No. 1 liquid heat exchange medium circulating pump and the No. 2 liquid heat exchange medium circulating pump are used for exchanging heat of circulating media in the hydrogen reaction bed A1, the hydrogen reaction bed A2, the hydrogen reaction bed B1 and the hydrogen reaction bed B2 after the hydrogen reaction bed A1, the hydrogen reaction bed A2, the hydrogen reaction bed B1 and the hydrogen reaction bed B2 absorb/discharge hydrogen.

The liquid heat exchange medium work doing system is also provided with a protective cover, and the protective cover is provided with a combustible gas alarm and a hydrogen adding port; the protective cover is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation, and the pipeline in the protective cover is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation; the safety cover is also provided with a temperature regulator.

The protective cover is filled with system heat supplementing hydrogen, and heat entering from the external environment through the temperature regulator and heat generated by mechanical equipment are supplemented to the No. 1 liquid heat exchange medium circulating pump and the No. 2 liquid heat exchange medium circulating pump, so that the system can continuously work; the cold energy generated by the system acting is transmitted to the outside through the cooler; the system for supplementing hot hydrogen comprises, but is not limited to, hydrogen and other gases or liquids or solids besides hydrogen, or mixtures of two or more of the above, or mixtures of three.

Furthermore, a shell pass inlet of a cooler in the liquid heat exchange medium work-doing system is also used for accessing external hydrogen, and liquid hydrogen cooled by the cooler is discharged from a shell pass liquid hydrogen outlet of the cooler and enters a liquid hydrogen storage tank.

The reversible compression/expansion machine work-doing system disclosed by the invention takes hydrogen as a circulating working medium, changes the temperature of a hydrogen circulating medium in the work-doing system by arranging a metal hydrogen storage material reaction bed layer in a temperature changer and utilizing the characteristics of hydrogen absorption, heat release and hydrogen desorption of the metal hydrogen storage material, and then drives work-doing equipment to work or drives power generation equipment to generate power by the reversible compression/expansion machine work-doing, so that the natural energy and industrial waste heat are fully utilized, and the energy-saving emission-reducing and economic benefit creation are facilitated. The work system disclosed by the invention is arranged on vehicles such as ships and other equipment, can utilize energy carried by other natural substances, and can convert earth hydrogen energy into mechanical energy to drive the vehicles to run by driving the expander to do work through working medium circulation, thereby realizing green traffic. The cold released by the system is used for liquefying various gases and providing cold for places needing cold.

Drawings

FIG. 1 is a schematic diagram of the reversible compressor/expander work system provided by the present invention;

FIG. 2 is a view showing an operating state of a metal hydride according to example 1 of the present invention;

FIG. 3 is a schematic diagram of another reversible compression/expansion machine work system according to the present invention;

FIG. 4 is a view showing an operating state of a metal hydride according to example 2 of the present invention;

FIG. 5 is a phase diagram of hydrogen;

FIG. 6 is an enlarged view of a portion of FIG. 5;

FIG. 7 is a schematic structural diagram of a liquid heat exchange medium work-doing system provided by the present invention;

FIG. 8 is a view showing an operating state of a metal hydride according to example 3 of the present invention;

FIG. 9 is a schematic structural diagram of another liquid heat exchange medium work-doing system provided by the present invention;

fig. 10 is a view showing an operation state of a metal hydride according to example 4 of the present invention.

Wherein: 1-high pressure heat exchange tank, 2-1 number positive and negative reversible compression/expansion machine, 3-2 number positive and negative reversible compression/expansion machine, 4-generator, 5-B metal hydrogen storage material reaction bed layer, 6-A metal hydrogen storage material reaction bed layer, 7-low pressure heat exchange tank, 8-valve, 9-1 number temperature changer, 10-2 number temperature changer, 11-high pressure expansion machine, 12-low pressure expansion machine, 13-1 number expansion inlet, 14-1 number expansion outlet, 15-1 number compression inlet, 16-1 number compression outlet, 13 '-2 number expansion inlet, 14' -2 number expansion outlet, 15 '-2 number compression inlet, 16' -2 number compression outlet, 17-1 number liquid heat exchange medium circulating pump, 18-2 number liquid hydrogen storage medium circulating pump, 19-A1 metal hydrogen storage material reaction bed layer, 20-A2 metal material reaction bed layer, 21-B1 metal material reaction bed layer, 22-B2 metal hydrogen storage material reaction bed layer, 23-hydrogen filtering membrane, 24-hydrogen adding port, 25-combustible gas alarm, 26-temperature regulator, 27-gas-liquid separator, 28-protective cover, 29-cooler, 30-liquid hydrogen tank, 31-hydrogen inlet, 32-liquid hydrogen outlet, 33-air inlet, 34-liquid oxygen outlet, 35-liquid nitrogen outlet, 36-liquid nitrogen, liquid oxygen separation preparation system, 37-liquid nitrogen tank, 38-liquid oxygen tank.

Detailed Description

The present invention will be described in detail with reference to the following examples and drawings. The scope of protection of the invention is not limited to the embodiments, and any modification made by those skilled in the art within the scope defined by the claims also falls within the scope of protection of the invention.

Example 1:

the invention provides a work system of a forward and reverse reversible compression/expansion machine, which comprises a high-pressure heat exchange tank 1, a No. 1 forward and reverse reversible compression/expansion machine 2, a No. 2 forward and reverse reversible compression/expansion machine 3, a No. 1 temperature changer 9, a No. 2 temperature changer 10, a low-pressure heat exchange tank 7 and a generator 4, as shown in figure 1.

Specifically, the No. 1 reversible compression/expansion machine 2 is provided with a No. 1 expansion inlet 13, a No. 1 expansion outlet 14, a No. 1 compression inlet 15, and a No. 1 compression outlet 16. The No. 2 reversible compression/expansion machine 3 is provided with a No. 2 expansion inlet 13 ', a No. 2 expansion outlet 14', a No. 2 compression inlet 15 ', and a No. 2 compression outlet 16'. The temperature changer 9 and 10 are respectively provided with a hydrogen absorption inlet, a hydrogen absorption outlet, a hydrogen discharge inlet and a hydrogen discharge outlet.

An outlet of the high-pressure heat exchange tank 1 is connected to a hydrogen absorption inlet of a No. 1 temperature changer 9 through a valve 8, a hydrogen absorption outlet of the No. 1 temperature changer 9 is connected to a No. 1 expansion inlet 13 of the No. 1 reversible compression/expansion machine 2, a No. 1 expansion outlet 14 of the No. 1 reversible compression/expansion machine 2 is connected to a hydrogen discharge inlet of the No. 2 temperature changer 10 through a valve, a hydrogen discharge outlet of the No. 2 temperature changer 10 is connected to a No. 2 compression inlet 15 'of the No. 2 reversible compression/expansion machine 3, and a No. 2 compression outlet 16' of the No. 2 reversible compression/expansion machine 3 is connected to an inlet of the high-pressure heat exchange tank 1 through a valve 8.

An outlet of the low-pressure heat exchange tank 7 is connected to a hydrogen absorption inlet of the No. 2 temperature changer 10 through a valve, a hydrogen absorption outlet of the No. 2 temperature changer 10 is connected to a No. 2 expansion inlet 13 'of the No. 2 reversible compression/expansion machine 3, a No. 2 expansion outlet 14' of the No. 2 reversible compression/expansion machine 3 is connected to a hydrogen discharge inlet of the No. 1 temperature changer 9 through a valve 8, a hydrogen discharge outlet of the No. 1 temperature changer 9 is connected to a No. 1 compression inlet 15 of the No. 1 reversible compression/expansion machine 2, and a No. 1 compression outlet 16 of the No. 1 reversible compression/expansion machine 2 is connected to an inlet of the low-pressure heat exchange tank 7 through a valve.

The No. 1 forward and reverse reversible compression/expansion machine 2 and the No. 2 forward and reverse reversible compression/expansion machine 3 are coaxially connected with the generator 4 through output shafts. In one embodiment, the generator 4 is electrically connected to an external power grid or battery, thereby enabling the generator 4 to generate electricity from the kinetic energy of work output from the reversible compression/expansion machine # 1 or the reversible compression/expansion machine # 2. In practical application, in addition to the external connection of the generator on the power output shaft of the No. 1 reversible compression/expansion machine 2 and the No. 2 reversible compression/expansion machine 3, other devices, such as a fan or a waterwheel, can be connected to the power output shaft externally. The No. 1 forward and reverse reversible compression/expansion machine 2 and the No. 2 forward and reverse reversible compression/expansion machine 3 may be piston machines or wheel machines, and energy output by the No. 1 forward and reverse reversible compression/expansion machine 2 and the No. 2 forward and reverse reversible compression/expansion machine 3 to do work may be converted into energy of other forms by the piston machines or the wheel machines.

When gaseous hydrogen is used as the circulating heat exchange medium in the work-doing system shown in fig. 1, a reaction bed layer 5 of a metal hydrogen storage material B can be arranged in a temperature changer 9 No. 1, wherein the metal hydrogen storage material B is a titanium metal hydrogen storage material, such as Ti₂Mn₅. A reaction bed layer 6 of metal hydrogen storage material A is arranged in a No. 2 temperature changer 10, wherein the metal hydrogen storage material A is rare earth metal hydrogen storage material, such as LaAl₂And N is added. The metal hydrogen storage material B consisting of titanium metal hydrogen storage material absorbs hydrogen and releases heat at below 120 ℃ and above 1MPa, and releases hydrogen and absorbs heat at above-60 ℃ and below 0.15MPa (the metal can absorb hydrogen and release heat at-100 ℃ and below 0.15 MPa). The metal hydrogen storage material A consisting of the rare earth metal hydrogen storage material releases and absorbs hydrogen at the temperature of more than 40 ℃ and more than 2MPa, absorbs hydrogen at the temperature of less than 20 ℃ and more than 0.3MPa and releases heat, and four state points are shown in figure 2.

The No. 1 positive and negative reversible compression/expansion machine 2 can complete the gas expansion work-doing process when the intake airflow flows in the positive direction; when the intake airflow reversely flows, the gas compression process can be completed. On the contrary, the No. 2 reversible compression/expansion machine 3 can complete the gas compression process when the intake airflow flows in the forward direction; when the intake airflow reversely flows, the process of gas expansion and work application can be finished. The No. 1 forward and reverse reversible compression/expansion machine 2 and the No. 2 forward and reverse reversible compression/expansion machine 3 alternately perform expansion and compression processes.

For the work-doing system shown in fig. 1, the work-doing system is divided into a forward flow cycle and a reverse flow cycle in time sequence. During forward flow circulation, through switching of a valve group consisting of valves 8, high-pressure hydrogen firstly enters a No. 1 temperature changer 9 from a high-pressure heat exchange tank 1, and a metal hydrogen storage material B in the No. 1 temperature changer 9 absorbs hydrogen to release a large amount of heat so as to raise the unabsorbed hydrogen to a certain temperature and then sends the unabsorbed hydrogen to a No. 1 forward and reverse reversible compressor/expander 2 to perform expansion work; the hydrogen after expansion work enters a No. 2 temperature changer 10, and the A metal hydrogen storage material in the No. 2 temperature changer 10 releases hydrogen to absorb a large amount of heat so that the hydrogen is reduced to a certain temperature and then is sent into a No. 2 reversible compression/expansion machine 3 for compression. The compressed hydrogen is sent back to the high pressure heat exchange tank 1.

During reverse flow circulation, low-pressure hydrogen firstly enters the No. 2 temperature changer 10 from the low-pressure heat exchange tank 7 through switching of a valve group consisting of valves 8, and the A metal hydrogen storage material in the No. 2 temperature changer 10 absorbs hydrogen to release a large amount of heat so as to raise the unabsorbed hydrogen to a certain temperature and then sends the unabsorbed hydrogen into the No. 2 forward and reverse reversible compressor/expander 3 to perform expansion work; the hydrogen after expansion work enters a No. 1 temperature changer 9, and the A metal hydrogen storage material in the No. 1 temperature changer 9 releases hydrogen to absorb a large amount of heat so that the hydrogen is reduced to a certain temperature and then is sent to a No. 1 reversible compression/expansion machine 2 for compression. The compressed hydrogen is sent back to the low pressure heat exchange tank 7.

In this embodiment, the specific process of the forward flow cycle when the working system works is as follows: through the switching of a valve group consisting of a valve 8, high-pressure hydrogen at 2MPa and 39.35 ℃ at the outlet of a high-pressure heat exchange tank 1 firstly enters a No. 1 temperature changer 9, a metal hydrogen storage material B in the No. 1 temperature changer 9 absorbs partial hydrogen to release a large amount of heat so as to raise the temperature of the hydrogen which is not absorbed to 120 ℃, and then the hydrogen is sent into a No. 1 forward and reverse reversible compression/expansion machine 2 to do work through expansion, wherein the hydrogen pressure at the outlet of the No. 1 forward and reverse reversible compression/expansion machine 2 is 1MPa, and the hydrogen temperature is 48.9 ℃. Then hydrogen with the temperature of 48.9 ℃ and the pressure of 1MPa enters a No. 2 temperature changer 10, the A metal hydrogen storage material in the No. 2 temperature changer 10 is subjected to hydrogen discharge to absorb a large amount of heat, so that the temperature of the hydrogen is reduced to-33 ℃, and then the hydrogen is sent into a No. 2 forward and reverse reversible compression/expansion machine 3 to be compressed, wherein the pressure of the hydrogen at the outlet of the No. 2 forward and reverse reversible compression/expansion machine 3 is 2MPa, and the temperature is 20 ℃. The hydrogen with the temperature of 20 ℃ and the pressure of 2MPa returns to the inlet of the high-pressure heat exchange tank 1 to form closed circulation. When the work-doing system is operated, the forward flow circulation path of the hydrogen medium is shown as the path shown by the solid line in fig. 1. The hydrogen gas returned to the high-pressure heat exchange tank 1 can be heated to 39.35 ℃ by heat exchange to the outside.

Metal a hydrogen storage material still has the ability to absorb and desorb hydrogen after exceeding the temperature and pressure ranges defined in fig. 2. Therefore, the A metal hydrogen storage material can release hydrogen and absorb heat under the temperature state of 48.9 ℃.

In this embodiment, the specific process of the reverse flow circulation when the working system works is as follows: through the switching of a valve group consisting of a valve 8, low-pressure hydrogen at the outlet of a low-pressure heat exchange tank 7 is at 0.3MPa and at-97.25 ℃ and enters a No. 2 temperature changer 10, a metal hydrogen storage material A in the No. 2 temperature changer 10 absorbs partial hydrogen to release a large amount of heat to raise the temperature of the unabsorbed hydrogen to 20 ℃, and then the unabsorbed hydrogen is sent into a No. 2 forward and reverse reversible compression/expansion machine 3 to be expanded to do work, wherein the pressure of the hydrogen at the outlet of the No. 2 forward and reverse reversible compression/expansion machine 3 is at 0.15MPa, and the temperature is at-65.8 ℃. Then hydrogen with the temperature of 65.8 ℃ below zero and the pressure of 0.15MPa enters a temperature changer 9 No. 1, the metal hydrogen storage material B in the temperature changer 9 No. 1 is subjected to hydrogen release to absorb a large amount of heat so that the temperature of the hydrogen is reduced to 147.7 ℃ below zero, and then the hydrogen is sent to a reversible compression/expansion machine 2 No. 1 for compression, wherein the pressure of the hydrogen at the outlet of the reversible compression/expansion machine 2 No. 1 is 0.3MPa, and the temperature is 120 ℃ below zero. The hydrogen with the temperature of minus 120 ℃ and the pressure of 0.3MPa returns to the inlet of the low-pressure heat exchange tank 7 to form a closed cycle. When the work-doing system is in operation, the circulation path for the hydrogen medium flowing in the reverse direction is shown by the dotted line in fig. 1. The hydrogen returning to the low-pressure heat exchange tank 7 can be heated to-97.25 ℃ by exchanging heat to the outside.

B metal hydrogen storage materials still have the ability to absorb and desorb hydrogen beyond the temperature and pressure ranges defined in fig. 2. Therefore, the B metal hydrogen storage material can release hydrogen and absorb heat under the temperature state of-147.7 ℃.

In this embodiment, the flow rate of hydrogen absorbed/released by the metal hydrogen storage material in the two temperature changers is 0.064kg/s, the flow rate of circulating heat exchange hydrogen is 0.78kg/s, and the average output power of the system is 104.8kw (including the sum of the work outputs of the heat exchange hydrogen and the work hydrogen). The work-done system provided in this example performs forward and reverse flow switching approximately every 200ms, with a frequency of 300 times per minute, and a redundancy equivalent of 25 times (1 redundancy equivalent refers to the minimum amount of metallic hydrogen storage material required for a single hydrogen absorption saturation of the metallic hydrogen storage material over a complete process cycle). The amount of the metal hydrogen storage material in each temperature changer was 11.9L, and the average particle size of the metal hydride was 500 nm. And a grating device is arranged at the inlet and the outlet of each temperature changer, and the grating device only allows hydrogen to pass through and does not allow metal hydride particles to leak from the grating. The inlet and outlet of the pipeline are strictly sealed, only hydrogen with certain pressure and certain temperature is allowed to pass through, and the metal hydride is not allowed to scatter outside the grating. The metal hydride is only in the grid, which allows only hydrogen in the conduit to pass through.

In addition, a protective hood 28 can be provided for the work-producing system, in particular, the protective hood 28 is provided with a combustible gas alarm 25 and a hydrogen gas inlet 24. Once hydrogen leaks from the system, the system can be monitored by a combustible gas alarm 25, so that the system can be stopped for maintenance, and the safety is ensured. The protective cover 28 is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation, the equipment is additionally provided with external heat preservation, and the pipeline is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation. The hydrogen addition port 24 may be used to supplement the system with hot hydrogen to the work system.

The protective cover 28 is provided with a temperature regulator 26 so that the entire system allows heat to be extracted from the environment and also allows heat to be dissipated to the environment to match the heat during heat exchange.

The protective cover 28 is filled with system heat supplementing hydrogen, the temperature is 42 ℃, because the generator 4 does work externally, the temperature of the system is reduced continuously, heat is required to be taken from the environment through the temperature regulator 26, the high-temperature high-pressure heat exchange circulation temperature is kept constant, and the system heat supplementing hydrogen transfers heat into the system through the high-pressure heat exchange tank 1. The system directly absorbs heat from the environment through the low-pressure heat exchange tank 7 and transmits cold to equipment needing cold in the environment. In this embodiment, the cycle working process of the working system emits cold, the low-temperature heat exchange tank 7 emits low-temperature cold, and the temperature regulator 26 emits high-temperature cold.

It should be noted that besides using gaseous hydrogen as the circulating heat exchange medium of the work-producing system, other gases, such as carbon dioxide, may also be used as the circulating heat exchange medium. In addition, other substances including but not limited to stable solids, liquids or liquid organic hydrides can be used instead of hydrogen as the circulating heat exchange medium of the work-producing system, and even liquid hydrogen itself can be used as the heat exchange medium. The heat exchange mode can be direct heat exchange or wall heat exchange, and the heat exchange medium for wall heat exchange can be gas, liquid or solid.

The embodiment of the application realizes cyclic work through the Ke Lai Pu cycle. The Kohlenberg cycle is represented by two metal hydrides with different properties, each metal hydride has two working state points, the lowest hydrogen release temperature and the highest hydrogen absorption temperature of the metal hydride a define a working range, the two temperatures can be adjusted, so that the working range can be large or small, the highest hydrogen release temperature and the lowest hydrogen absorption temperature of the metal hydride b influence a power temperature difference, the hydrogen release endothermic state point temperature of the metal hydride b is lower than the hydrogen absorption exothermic state point temperature of the metal hydride a, the hydrogen release endothermic state point pressure of the metal hydride b is higher than the hydrogen absorption exothermic state point pressure of the metal hydride a, the hydrogen absorption exothermic state point temperature of the metal hydride b is higher than the hydrogen release endothermic state point temperature of the metal hydride a, the hydrogen absorption exothermic state point pressure of the metal hydride b is higher than the hydrogen release endothermic state point pressure of the metal hydride a, that is, the maximum temperature of the metal hydride a is higher than that of the metal hydride b, while the maximum pressure of the metal hydride a is lower than that of the metal hydride b, the minimum temperature of the metal hydride a is lower than that of the metal hydride b, the minimum pressure of the metal hydride a is lower than that of the metal hydride b, the temperature difference between the maximum hydrogen absorption temperature of the metal hydride a and the maximum hydrogen desorption temperature of the metal hydride b may or may not be equal to the temperature difference between the minimum hydrogen desorption temperature of the metal hydride a and the minimum hydrogen absorption temperature of the metal hydride b, which is the same in this embodiment, 80 ℃, and the larger the value is, the larger the work of the system is, the larger the pressure ratio is. When the expansion work is done, the high-temperature high-enthalpy hydrogen is adopted to increase the work doing capacity, and when the compression work is consumed, the low-temperature low-enthalpy hydrogen is adopted to reduce the power consumption and maximize the net work of the system. Under the condition of low temperature, the low-temperature low-enthalpy hydrogen is adopted during expansion work to increase the work doing capacity, and the lower-temperature lower-enthalpy hydrogen is adopted during compression work consumption to reduce the work consumption and maximize the net work of the system. The system is provided with two hydrogen absorption and heat release state points and two hydrogen release and heat absorption state points, the high-temperature hydrogen absorption and heat release of the metal hydride a are used for the high-temperature hydrogen release and heat absorption of the metal hydride b through the circulation of the heat exchange hydrogen, the low-temperature hydrogen absorption and heat release of the metal hydride b are used for the low-temperature hydrogen release and heat absorption of the metal hydride a through the circulation of the heat exchange hydrogen, and the heat released and absorbed by the absorbed and released hydrogen keeps equal or almost equal pairwise. Although the metal hydride a has only two state points and the metal hydride b has only two state points, the two state points are continuously switched from one state point to the other state point along with the continuous change of the hydrogen absorption and release state points, and the two state points are continuously switched, two metal hydrides are incorporated into a system, so that a cycle can be formed, each state point can be automatically recovered and can work outside the system, four state points are continuously circulated in the system, and heat is continuously exchanged in the system, so that a work cycle is realized, the hydrogen absorption and heat release in the high-temperature state of the metal hydride a and the hydrogen desorption and heat absorption in the high-temperature state of the metal hydride b are a group, heat exchange is carried out between the metal hydride a and the hydrogen desorption and the heat absorption in the low-temperature state of the metal hydride b are a group, the system cycle for realizing external work is defined as one of the Kohleper cycle by exchanging heat with each other at low temperature. If the environment is lower than 42 ℃, the temperature of the system heat supplementing hydrogen is raised to 42 ℃ or above by utilizing the electricity generated by the system through a heat pump.

The Kohlenbu cycle is defined as at least two metal hydrides, at least four state points exist, and the hydrogen absorption heat release and the hydrogen desorption heat absorption of the at least four state points are kept or basically kept in heat balance in the system through a circulating heat exchange medium, namely the heat of the hydrogen absorption heat release of one state point is transferred to the hydrogen desorption heat absorption process in the other three state points by the circulating heat exchange medium.

The hydrogen desorption endothermic state in at least four existing state points does not or basically does not absorb heat into the environment, but transfers the heat of the hydrogen absorption exothermic heat in at least four state points to the hydrogen desorption endothermic process in at least four state points;

the hydrogen-absorbing and heat-releasing states of the at least four existing state points do not or substantially do not dissipate heat to the environment, but rather transfer heat to the hydrogen-releasing and heat-absorbing processes of the at least four existing state points, and the hydrogen-releasing and heat-absorbing processes of the at least four existing state points are fully or almost fully capable of receiving the transferred heat.

The system can do work through the working cycle formed by at least four state points, the working mode is that hydrogen is used as a medium to do work, the temperature-pressure of the hydrogen can be circularly changed by the at least four state points, and therefore the working cycle is formed, and the working equipment can be an impeller type slewing mechanism, a piston type slewing mechanism or other modes. At least four state points can be restored to the original state points through the work cycle, and the hydrogen absorption and heat release state points and the hydrogen desorption and heat absorption state points. Allowing the system to release cold into the environment and absorb heat from the environment.

Besides using gaseous hydrogen as the circulating heat exchange medium of the work-doing system, other gases can be used as the circulating heat exchange medium. In addition, other substances including but not limited to stable solids, liquids or liquid organic hydrides can be used instead of hydrogen as the circulating heat exchange medium of the work-producing system, and even liquid hydrogen itself can be used as the heat exchange medium. The heat exchange mode can be direct heat exchange or partition wall heat exchange, and the heat exchange medium for partition wall heat exchange can be gas, liquid, solid or mixture of the above or mixture of every two.

The statepoint connections of the P-T diagram (pressure-temperature diagram) of at least two metal hydrides may or may not intersect. As a typical example, the P-T diagram of two metal hydrides according to the present embodiment is shown in FIG. 2. And allowing the upper high-temperature high-pressure cycle to pause for a period of time, such as 2-10 milliseconds, after the upper high-temperature high-pressure cycle is completed, and then starting the lower low-temperature low-pressure cycle, and similarly allowing the lower low-temperature low-pressure cycle to pause for a period of time, such as 2-10 milliseconds, after the lower low-temperature low-pressure cycle is completed, and then starting the upper high-temperature high. The metal hydride B is allowed to be loaded on the impeller, the impeller gap, and the shaft inside the No. 1 reversible compression/expansion machine 2, and the metal hydride B is also allowed to be loaded on the right side of the No. 1 reversible compression/expansion machine 2. In the same way, the metal hydride a is allowed to be loaded on the impeller, the impeller gap, and the shaft inside the No. 2 reversible compression/expansion machine 3, and the metal hydride a is also allowed to be loaded on the right side of the No. 2 reversible compression/expansion machine 3. The metal hydride can be arranged in a groove or a volute connected with the impeller of the reversible compressor/expander or in the reversible compressor/expander, or is coaxially arranged with the impeller but not contacted with the impeller, can rotate together with the impeller at the same rotating speed, can be fixed on the impeller or not contacted with the impeller, can also be arranged in a grid net, the grid only allows hydrogen to pass through but not solid particles to leak, the metal hydride can also be a coating coated on the blade, and the metal hydride in the temperature changer can be arranged in the reversible compressor/expander together with the metal hydride in the reversible compressor/expander.

Example 2:

the working system provided by this embodiment is as shown in fig. 3, and is similar to embodiment 1, except that the low-pressure heat exchange tank 7 exchanges heat with external hydrogen gas, and the external hydrogen gas is cooled to prepare liquid hydrogen, which is sent to the liquid hydrogen tank 30 as a product.

The embodiment includes a high-pressure heat exchange tank 1, a No. 1 reversible compression/expansion machine 2, a No. 2 reversible compression/expansion machine 3, a No. 1 temperature changer 9, a No. 2 temperature changer 10, a low-pressure heat exchange tank 7, a generator 4, a cooler 29, and a liquid hydrogen tank 30.

The No. 1 forward and reverse reversible compression/expansion machine 2 and the No. 2 forward and reverse reversible compression/expansion machine 3 are coaxially connected with the generator 4 through a power output shaft. In a specific embodiment, the kinetic energy output by the No. 1 forward and reverse reversible compression/expansion machine 2 or the No. 2 forward and reverse reversible compression/expansion machine 3 is used for driving the generator 4 to generate electricity, and the generator 4 is electrically connected to an external power grid or a storage battery to supply electricity to the outside.

When gaseous hydrogen is used as the circulating heat exchange medium in the work-doing system shown in fig. 3, a reaction bed layer 5 of a metal hydrogen storage material B can be arranged in the temperature changer No. 19, wherein the metal hydrogen storage material B is a titanium metal hydrogen storage material, such as ticlmn₅Predominantly metal hydrides. A reaction bed layer 6 of metal hydrogen storage material A is arranged in a No. 2 temperature changer 10, wherein the metal hydrogen storage material A is rare earth metal hydrogen storage material, such as La₂Al₂A metal hydride with V as the main component. The metal hydrogen storage material B consisting of the titanium metal hydrogen storage material absorbs hydrogen and releases heat at 120 ℃ and 1MPa, and releases hydrogen and absorbs heat at-260 ℃ and 0.004MPa (the metal can also release hydrogen and absorb heat at-262 ℃ and 0.004 MPa). The metal hydrogen storage material A consisting of the rare earth metal hydrogen storage material absorbs hydrogen and heat at 20 ℃ and 2.0MPa, absorbs hydrogen and releases heat at-160 ℃ and 0.002MPa, and the four state points are shown in figure 4.

For the work-doing system shown in fig. 3, the work-doing system is divided into a forward flow cycle and a reverse flow cycle in time sequence. During forward flow circulation, through switching of a valve group consisting of valves 8, high-pressure hydrogen firstly enters a No. 1 temperature changer 9 from a high-pressure heat exchange tank 1, and a metal hydrogen storage material B in the No. 1 temperature changer 9 absorbs hydrogen to release a large amount of heat so as to raise the unabsorbed hydrogen to a certain temperature and then sends the unabsorbed hydrogen to a No. 1 forward and reverse reversible compressor/expander 2 to perform expansion work; the hydrogen after expansion work enters a No. 2 temperature changer 10, the A metal hydrogen storage material in the No. 2 temperature changer 10 releases hydrogen to absorb a large amount of heat so that the hydrogen is reduced to a certain temperature, and then the hydrogen is sent into a No. 2 reversible compression/expansion machine 3 for compression, and the compressed hydrogen is sent back to the high-pressure heat exchange tank 1.

During reverse flow circulation, low-pressure hydrogen firstly enters the No. 2 temperature changer 10 from the low-pressure heat exchange tank 7 through switching of a valve group consisting of valves 8, and the A metal hydrogen storage material in the No. 2 temperature changer 10 absorbs hydrogen to release a large amount of heat so as to raise the unabsorbed hydrogen to a certain temperature and then sends the unabsorbed hydrogen into the No. 2 forward and reverse reversible compressor/expander 3 to perform expansion work; the hydrogen after expansion work enters a temperature changer 9 No. 1, the metal hydrogen storage material A in the temperature changer 9 No. 1 releases hydrogen to absorb a large amount of heat so that the hydrogen is reduced to a certain temperature, and then the hydrogen is sent into a reversible compressor/expander 2 No. 1 for compression, and the compressed hydrogen is sent back to the low-pressure heat exchange tank 7.

In this embodiment, the specific process of the forward flow cycle when the working system works is as follows: through the switching of a valve group consisting of a valve 8, high-pressure hydrogen at 2.0MPa at the outlet of a high-pressure heat exchange tank 1 enters a No. 1 temperature changer 9, a metal hydrogen storage material B in the No. 1 temperature changer 9 absorbs partial hydrogen to release a large amount of heat so as to raise the temperature of the hydrogen which is not absorbed to 120 ℃, and then the hydrogen is sent into a No. 1 forward and reverse reversible compression/expansion machine 2 to do work through expansion, wherein the hydrogen pressure at the outlet of the No. 1 forward and reverse reversible compression/expansion machine 2 is 1MPa, and the hydrogen temperature is 48.9 ℃. Then hydrogen with the temperature of 48.9 ℃ and the pressure of 1MPa enters a No. 2 temperature changer 10, the A metal hydrogen storage material in the No. 2 temperature changer 10 is subjected to hydrogen discharge and absorption to absorb a large amount of heat so that the temperature of the hydrogen is reduced to-33.0 ℃, and then the hydrogen is sent into a No. 2 forward and reverse reversible compression/expansion machine 3 for compression, wherein the pressure of the hydrogen at the outlet of the No. 2 forward and reverse reversible compression/expansion machine 3 is 2.0MPa, and the temperature is 20 ℃. The hydrogen with the temperature of 20 ℃ and the pressure of 2.0MPa returns to the inlet of the high-pressure heat exchange tank 1 to form closed circulation. The hydrogen gas returned to the high-pressure heat exchange tank 1 can be heated to 39.35 ℃ by heat exchange to the outside.

Metal a hydrogen storage material still has the ability to absorb and desorb hydrogen after exceeding the temperature and pressure ranges defined in fig. 4. Therefore, the A metal hydrogen storage material can release hydrogen and absorb heat under the temperature state of 48.9 ℃.

In this embodiment, the specific process of the reverse flow circulation when the working system works is as follows: through the switching of a valve group consisting of a valve 8, low-pressure hydrogen at the outlet of a low-pressure heat exchange tank 7 at 0.004MPa and 240 ℃ below zero firstly enters a No. 2 temperature changer 10, a metal hydrogen storage material A in the No. 2 temperature changer 10 absorbs partial hydrogen to release a large amount of heat so as to raise the temperature of the hydrogen which is not absorbed to-160 ℃, and then the hydrogen is sent into a No. 2 forward and reverse reversible compression/expansion machine 3 to be expanded to do work, wherein the pressure of the hydrogen at the outlet of the No. 2 forward and reverse reversible compression/expansion machine 3 is 0.002MPa, and the temperature is-180.5 ℃. Then hydrogen with the temperature of minus 180.5 ℃ and the pressure of 0.002MPa enters a No. 1 temperature changer 9, a metal hydrogen storage material B in the No. 1 temperature changer 9 is subjected to hydrogen release to absorb a large amount of heat so that the temperature of the hydrogen is reduced to minus 262.4 ℃, and then the hydrogen is sent to a No. 1 forward and reverse reversible compression/expansion machine 2 for compression, wherein the pressure of the hydrogen at the outlet of the No. 1 forward and reverse reversible compression/expansion machine 2 is 0.004MPa, and the temperature is minus 260 ℃. The hydrogen with the temperature of minus 260 ℃ and the pressure of 0.004MPa returns to the inlet of the low-pressure heat exchange tank 7 to form a closed cycle. The hydrogen gas at-260 ℃ and 0.004MPa returned to the low-pressure heat exchange tank 7 can exchange heat with external hydrogen gas in a cooler 29, the external 0.1MPa hydrogen gas is cooled to liquid hydrogen, and the liquid hydrogen is sent to a liquid hydrogen tank 30 to be used as a product. The hydrogen gas at-260 ℃ in the low-pressure heat exchange tank 7 is subjected to low-temperature heat exchange, and the temperature is increased to-240 ℃.

B metal hydrogen storage materials still have the ability to absorb and desorb hydrogen beyond the temperature and pressure ranges defined in fig. 4. Therefore, the metal B hydrogen storage material can release hydrogen and absorb heat under the temperature state of-180.5 ℃.

It should be noted that the heat exchange medium in this embodiment is always gaseous hydrogen, and even hydrogen at-260 ℃ and 0.004MPa in the low-pressure heat exchange tank 7 is still gaseous. Fig. 5 and 6 show gas-liquid phase diagrams of hydrogen gas at a critical temperature of-239.97 ℃ (33.19K) or less. When the hydrogen temperature is-260 c as shown in fig. 5, the gas-liquid state of hydrogen can be controlled by adjusting the pressure of hydrogen. As can be seen from a comparison of FIG. 6, hydrogen was gaseous at-260 ℃ under a temperature-pressure condition of 0.004 MPa.

In addition, the embodiment of the application also provides a concept of the dynamic performance of hydrogen absorption and desorption of the metal hydride. Specifically, the kinetics of metal hydrides is a function of the maximum temperature, minimum temperature, operating frequency and temperature differential, and is also related to the nature of the metal hydride itself.

In this embodiment, the flow rate of hydrogen absorbed/released by the metal hydrogen storage material in the two temperature changers is 0.064kg/s, the flow rate of circulating heat exchange hydrogen is 1.058kg/s, and the average output power of the system is 125kw (including the sum of the work output of the heat exchange hydrogen and the work output of the work hydrogen). The system of this embodiment performs forward and reverse flow switching about every 600ms, with a frequency of 100 times per minute, a redundancy equivalent of 25 times (1 redundancy equivalent refers to the minimum amount of metal hydrogen storage material required for a single hydrogen absorption saturation of the metal hydrogen storage material over a complete process cycle), and an amount of metal hydrogen storage material per temperature changer of 35.1L. The average grain size of the metal hydride is 500 nm. And a grating device is arranged at the inlet and the outlet of each temperature changer, and the grating device only allows hydrogen to pass through and does not allow metal hydride particles to leak from the grating.

The system is provided with a protective cover 28, and the protective cover 28 is provided with a combustible gas alarm 25 and a hydrogen gas adding port 24. Once hydrogen leaks from the system, the system can be monitored by a combustible gas alarm 25, so that the system can be stopped for maintenance, and the safety is ensured. The protective cover 28 is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation, the equipment is additionally provided with external heat preservation, and the pipeline is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation.

The protective cover 28 is filled with system heat-supplementing hydrogen, the temperature is 22 ℃, because the generator 4 does work to the outside, the temperature of the system heat-supplementing hydrogen is continuously reduced, heat is required to be taken from the ambient temperature through the temperature regulator 26, the high-temperature high-pressure heat exchange circulation temperature is kept constant, and the heat of the system heat-supplementing hydrogen is transferred into the system through the high-pressure heat exchange tank 1. The system transmits cold energy to the environment through the low-pressure heat exchange tank 7, and the cold energy is transmitted to equipment needing the cold energy in the environment. Specifically, the cooler 29 may be added to the low-pressure heat exchange tank 7, and the hydrogen inlet 31 and the liquid hydrogen outlet 32 may be provided in the protective cover 28, and the liquid hydrogen tank 30 may be added to the protective cover 28. The hydrogen inlet 31 provided on the protective cover 28 is connected to the inlet of the cooler 29 through a hydrogen line to deliver the external hydrogen into the cooler 29, thereby achieving low-temperature heat exchange between the external hydrogen and the low-pressure heat exchange tank 7, and thus liquefying the external hydrogen into liquid hydrogen at a low temperature of-260 ℃. The cooler 29 is connected via a liquid hydrogen line to a liquid hydrogen outlet 32 provided on the protective hood 28 for discharging liquid hydrogen product out of the protective hood 28.

The inlet and outlet of the pipeline are strictly sealed, only hydrogen with certain pressure and certain temperature is allowed to pass through, and the metal hydride is not allowed to scatter outside the grating. The metal hydride is only in the grid, which allows only hydrogen in the conduit to pass through.

By the method of the embodiment, nitrogen, oxygen, argon, helium and carbon dioxide in the air can be separated and liquefied.

Example 3:

the structure of the liquid heat exchange medium work-doing system provided by the invention is shown in fig. 7, and comprises two groups of metal hydrogen storage material reaction beds A and B, at least two groups of hydrogen reaction beds are arranged in the system, the hydrogen reaction beds A1, A2, B1 and B2 are the same as A1 and A2 metal hydrides, and the B1 and B2 metal hydrides are the same, so that hydrogen absorption/desorption operation is alternately carried out. The difference of the change characteristics of the self hydrogen absorption/desorption pressure of different metal hydrogen storage materials under the influence of temperature is utilized, so that the pressure difference exists between one group of hydrogen desorption pressure and the other group of hydrogen absorption pressure of two groups of different metal hydrogen storage materials under the condition that the temperature is close to each other, and the pressure difference can be utilized to do work through a hydrogen expander to generate electric power.

The metal hydride loaded in the metal hydrogen storage material reaction bed A discharges hydrogen at 10 ℃ and 0.5MPa, and absorbs hydrogen at-259 ℃ and 0.005 MPa; the metal hydride loaded in the metal hydrogen storage material reaction bed B absorbs hydrogen at 19 ℃ and 0.2MPa and releases hydrogen at-250 ℃ and 0.002 MPa. Fig. 8 shows temperature-pressure state points of the metal hydride charged on the metallic hydrogen storage material reaction bed a and the metallic hydrogen storage material reaction bed B.

The hydrogen reaction bed A and the hydrogen reaction bed B are both provided with a hydrogen discharge outlet and a hydrogen absorption inlet. The hydrogen discharge outlet of the hydrogen reaction bed a1 is connected to the inlet of the high-pressure expander 11, and the outlet of the high-pressure expander 11 is connected to the hydrogen absorption inlet of the hydrogen reaction bed B1. The hydrogen discharge outlet of the hydrogen reaction bed B1 is connected to the inlet of the low pressure expander 12, the outlet of the low pressure expander 12 is connected to the tube-side inlet of the cooler 29, and the tube-side outlet of the cooler 29 is connected to the hydrogen absorption inlet of the hydrogen reaction bed a 1. In order to ensure continuous operation of high-pressure expander 11 and low-pressure expander 12, hydrogen reaction bed a2 and hydrogen reaction bed B2 are provided, and likewise, the hydrogen discharge outlet of hydrogen reaction bed a2 is connected to the inlet of high-pressure expander 11, and the outlet of high-pressure expander 11 is connected to the hydrogen suction inlet of hydrogen reaction bed B2. The hydrogen discharge outlet of the hydrogen reaction bed B2 is connected to the inlet of the low pressure expander 12, the outlet of the low pressure expander 12 is connected to the tube-side inlet of the cooler 29, and the tube-side outlet of the cooler 29 is connected to the hydrogen absorption inlet of the hydrogen reaction bed a 1. Air and external hydrogen at normal pressure respectively enter from a shell-side inlet of the cooler 29, cooled liquid hydrogen exits from a shell-side liquid hydrogen outlet of the cooler 29 and enters the liquid hydrogen storage tank 30 as a product, cooled liquid nitrogen and liquid oxygen exit from a shell-side liquefied air outlet of the cooler 29 and enter the liquid oxygen and liquid nitrogen separation preparation system 36, and the separated liquid nitrogen and liquid oxygen respectively enter the liquid nitrogen tank 37 and the liquid oxygen tank 38 as products.

In this embodiment, the flow rate of hydrogen absorbed/released by the metal hydrogen storage material is 0.064kg/s, the circulating heat exchange medium is liquid hydrogen, the average output power of the system is 27.5kw, the forward flow is 50ms, the reverse flow is performed, the 50ms switching is performed once, the operation frequency is 600 times per minute, the redundancy equivalent is 25 times (1 time redundancy equivalent refers to the minimum amount of the metal hydrogen storage material required when the metal hydrogen storage material is saturated by absorbing hydrogen once in the whole complete process cycle), and the amount of the metal hydrogen storage material in each hydrogen reaction bed is 5.85L. The average grain size of the metal hydride is 500 nm. And a grating device is arranged at the inlet and the outlet of each temperature changer, and the grating device only allows hydrogen to pass through and does not allow metal hydride particles to leak from the grating.

Furthermore, a protective cover 28 can be provided for the system, the protective cover 28 being provided with a combustible gas alarm 25 and a hydrogen gas inlet 24. Once hydrogen leaks from the system, the system can be monitored by a combustible gas alarm 25, so that the system can be stopped for maintenance, and the safety is ensured. The protective cover 28 is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation, the equipment is additionally provided with external heat preservation, and the pipeline is additionally provided with internal heat preservation or external heat preservation or internal and external heat preservation.

In order to enable the work-doing system to realize the production of liquid hydrogen, liquid nitrogen and liquid oxygen, a hydrogen inlet 31 and an air inlet 33 may be further disposed on the protective cover 28, so as to input external hydrogen and air to the cooler 29 as raw materials for producing liquid hydrogen, liquid nitrogen and liquid oxygen.

In addition, in order to enable the protective cover 28 for outputting the liquid hydrogen, the liquid nitrogen and the liquid oxygen produced by the work system, a liquid hydrogen outlet 32, a liquid oxygen outlet 34 and a liquid nitrogen outlet 35 can be further arranged on the protective cover 28, and the liquid hydrogen outlet 32, the liquid oxygen outlet 34 and the liquid nitrogen outlet 35 are respectively communicated with a liquid hydrogen tank 30, a liquid oxygen tank 38 and a liquid nitrogen tank 37.

The specific working process is as follows:

as shown in fig. 7, when the hydrogen reaction bed a1 and the hydrogen reaction bed B1 communicate with the high pressure expander 11 to perform a high pressure expansion cycle, the hydrogen reaction bed a2 and the hydrogen reaction bed B2 communicate with the low pressure expander 12 to perform a low pressure expansion cycle; next, when the hydrogen reaction bed a1 and the hydrogen reaction bed B1 are switched to communicate with the low-pressure expander 12 for the low-pressure expansion cycle, the hydrogen reaction bed a2 and the hydrogen reaction bed B2 are correspondingly switched to communicate with the high-pressure expander 11 for the high-pressure expansion cycle; two groups are alternately circulated.

When the hydrogen reaction bed A1 and the hydrogen reaction bed B1 are subjected to a high pressure expansion cycle, see the state diagram of FIG. 8, the specific process is as follows: the hydrogen reaction bed A1 releases hydrogen at 10 ℃ and 0.5MPa, the released hydrogen enters a high-pressure expansion machine 11 to do work through expansion, the hydrogen at the outlet of the high-pressure expansion machine 11 enters an air heat exchanger at-55.7 ℃ and 0.2MPa to exchange heat with the environment, the temperature is raised to 19 ℃, the hydrogen enters a hydrogen reaction bed B1 to absorb the hydrogen at 0.2MPa and 19 ℃, and simultaneously the heat released when the hydrogen is absorbed by the hydrogen reaction bed B1 is transferred to the hydrogen reaction bed A1 through a No. 1 liquid heat exchange medium circulating pump 17 to be used for absorbing the hydrogen. At this time, the hydrogen reaction bed A2 and the hydrogen reaction bed B2 are correspondingly subjected to low-pressure expansion cycles, and the specific processes are as follows: hydrogen is discharged from the hydrogen reaction bed B2 at 0.005MPa and-259 ℃, the discharged hydrogen enters the low-pressure expansion machine 12 to do expansion work and generate power, the hydrogen at-262.3 ℃ at the outlet of the low-pressure expansion machine 12 and the hydrogen at 0.002MPa enter the tube side inlet of the cooler 29 to exchange heat with air and external hydrogen, the temperature is raised to-250 ℃, then the hydrogen enters the hydrogen reaction bed A2 from the tube side outlet of the cooler 29 to absorb hydrogen, the hydrogen is absorbed by the hydrogen reaction bed A2 at-250 ℃ and 0.002MPa, and simultaneously the heat discharged when the hydrogen is absorbed by the hydrogen reaction bed A2 is transferred to the hydrogen reaction bed B2 to be used for discharging the hydrogen through the No. 2 liquid heat exchange medium circulating pump 18.

When the hydrogen reaction bed A1 and the hydrogen reaction bed B1 are subjected to a low-pressure expansion cycle, the specific process is as follows: hydrogen is discharged from the hydrogen reaction bed B1 at 0.005MPa and-259 ℃, the discharged hydrogen enters the low-pressure expansion machine 12 to do expansion work and generate power, the hydrogen at-262.3 ℃ at the outlet of the low-pressure expansion machine 12 and the hydrogen at 0.002MPa enter the tube side inlet of the cooler 29 to exchange heat with air and external hydrogen, the temperature is raised to-250 ℃, then the hydrogen enters the hydrogen reaction bed A2 from the tube side outlet of the cooler 29 to absorb hydrogen, the hydrogen is absorbed by the hydrogen reaction bed A1 at-250 ℃ and 0.002MPa, and simultaneously the heat discharged when the hydrogen is absorbed by the hydrogen reaction bed A1 is transferred to the hydrogen reaction bed B1 to be used for discharging the hydrogen through the No. 2 liquid heat exchange medium circulating pump 18. At this time, the hydrogen reaction bed A2 and the hydrogen reaction bed B2 are respectively subjected to high-pressure expansion cycles, and the specific processes are as follows: the hydrogen reaction bed A2 releases hydrogen at 10 ℃ and 0.5MPa, the released hydrogen enters a high-pressure expansion machine 11 to do work through expansion, the hydrogen at the outlet of the high-pressure expansion machine 11 enters an air heat exchanger at-55.7 ℃ and 0.2MPa to exchange heat with the environment, the temperature is raised to 19 ℃, the hydrogen enters a hydrogen reaction bed B2 to absorb the hydrogen at 0.2MPa and 19 ℃, and simultaneously the heat released when the hydrogen is absorbed by the hydrogen reaction bed B2 is transferred to the hydrogen reaction bed A2 through a No. 1 liquid heat exchange medium circulating pump 17 to be used for absorbing the hydrogen. Through the above cycle reciprocation, the high pressure expander 11 and the low pressure expander 12 continuously perform work. When hydrogen reaction bed a1 and hydrogen reaction bed B1 are undergoing a low pressure expansion cycle, hydrogen reaction bed a2 and hydrogen reaction bed B2 are undergoing a high pressure expansion cycle, and when hydrogen reaction bed a1 and hydrogen reaction bed B1 are undergoing a high pressure expansion cycle, hydrogen reaction bed a2 and hydrogen reaction bed B2 are undergoing a low pressure expansion cycle. The high-low pressure expansion cycle is alternatively carried out, and the high-low pressure expander continuously operates.

The hydrogen outlet of each hydrogen reaction bed is provided with a filtering membrane 23 which only allows the hydrogen to pass through but not allows the liquid hydrogen to pass through. A gas-liquid separator 27 is provided at each of the liquid hydrogen outlets of the hydrogen reaction beds to allow only liquid hydrogen to pass therethrough and not allow hydrogen gas to pass therethrough.

The high-temperature heat exchange medium and the low-temperature heat exchange medium adopted in the embodiment are all liquid hydrogen, the high-temperature heat exchange medium works at a temperature of 10-19 ℃, and the low-temperature heat exchange medium works at a temperature of-250 to-259 ℃. Because the circulation process of the heat exchange medium has very high frequency and the heat exchange medium needs to be switched for more than 600 times per minute, the retention time of the heat exchange medium in a high-temperature working interval of 10-19 ℃ is very short, so that the heat exchange medium enters a low-temperature working interval of-250 to-259 ℃ without being vaporized. By means of the high-frequency rapid switching of the heat exchange medium, this embodiment can be made to remain liquid without vaporization or with little vaporization all the time, in the case of using liquid hydrogen as the heat exchange medium. The liquid hydrogen stored in the liquid hydrogen tank 30 can provide liquid hydrogen consumption supplement for the heat exchange medium.

The embodiment of the application also provides a concept of the temperature of the center of gravity. Specifically, the temperature of the center of gravity may be used to identify the gas-liquid state of the heat exchange material during the temperature cycling conversion process. The temperature of the center of gravity is a parameter used in the whole temperature cycle conversion interval, is a function of the temperature difference, and is also related to the temperature conversion frequency of the heat exchange substance and the property of the heat exchange substance. The temperature of the center of gravity is a point in a temperature cycle change interval, and the temperature of the center of gravity can often determine the gas-liquid state of the heat exchange medium in the temperature cycle conversion process. The temperature of the center of gravity is related to the residence time of the heat exchange substance at each temperature point in the temperature cycle change interval. And in the determined temperature cycle change interval, the retention time of the heat exchange substance at the temperature of the gravity center of the heat exchange substance is longest.

In the embodiment, the temperature cycle change interval of the liquid hydrogen as the heat exchange substance is 19 to-259 ℃, when the temperature conversion frequency is 600 times per minute, the temperature of the gravity center of the liquid hydrogen as the heat exchange substance is about-253 ℃, and the temperature of the gravity center determines that the liquid hydrogen can be always in a liquid state and not vaporized or vaporized in a small amount in the temperature cycle process of 19 to-259 ℃ and 600 times per minute.

In addition, in practical application, the protective cover 28 is filled with system hot hydrogen at 22 ℃. Because the generator 4 does work externally, the temperature of the system heat supplementing hydrogen is continuously reduced, heat is required to be taken from the ambient temperature through the temperature regulator 26, the high-temperature high-pressure heat exchange circulating temperature is kept constant, and the system heat supplementing hydrogen is transmitted into the system through the built-in heat exchanger. The system directly absorbs heat from the environment through the external heat exchanger and transmits cold to equipment needing cold in the environment. The system can supplement hot hydrogen gas, including but not limited to other gases or liquids or solids besides hydrogen gas, or mixtures of two or three of the above.

Example 4:

the structure of the liquid heat exchange medium work-doing system provided by this embodiment is shown in fig. 9, and is similar to embodiment 3, except that: firstly, liquid heat exchange medium is changed from liquid hydrogen to butane. Secondly, discharging hydrogen at 10 ℃ and 0.5MPa and absorbing hydrogen at-209 ℃ and 0.03MPa by using metal hydride loaded by the metal hydrogen storage material reaction bed A as a state point diagram 10; the metal hydride loaded in the metal hydrogen storage material reaction bed B absorbs hydrogen at 19 ℃ and 0.2MPa and releases hydrogen at-200 ℃ and 0.012MPa, and the specific temperature-pressure state points are shown in figure 10. And thirdly, only air enters from a shell side inlet of the cooler 29, the air is condensed and then enters the liquid nitrogen and liquid oxygen separation preparation system 36 from a shell side liquid air outlet of the cooler 29, the separated liquid nitrogen enters a liquid nitrogen tank 37 as a product, and the liquid oxygen enters a liquid oxygen tank 38 as a product.

The specific working process is as follows:

as shown in FIG. 9, when hydrogen reaction bed A1 and hydrogen reaction bed B1 are in communication with high pressure expander 11 for a high pressure expansion cycle, hydrogen reaction bed A2 and hydrogen reaction bed B2 are in communication with low pressure expander 12 for a low pressure expansion cycle, next sequence, when hydrogen reaction bed A1 and hydrogen reaction bed B1 are in communication with low pressure expander 12 for a low pressure expansion cycle, hydrogen reaction bed A2 and hydrogen reaction bed B2 are correspondingly in communication with high pressure expander 11 for a high pressure expansion cycle; two groups are alternately circulated.

When the hydrogen reaction bed A1 and the hydrogen reaction bed B1 are subjected to a high-pressure expansion cycle, the specific process is as follows: the hydrogen reaction bed A1 releases hydrogen at 10 ℃ and 0.5MPa, the released hydrogen enters a high-pressure expansion machine 11 to do work through expansion, the hydrogen at the outlet of the high-pressure expansion machine 11 is at-55.7 ℃ and 0.2MPa, enters a built-in heat exchanger to exchange heat with the environment, the temperature is raised to 19 ℃, the hydrogen enters a hydrogen reaction bed B1 to absorb hydrogen at 0.2MPa and 19 ℃, and simultaneously the heat released when the hydrogen is absorbed by the hydrogen reaction bed B1 is transferred to the hydrogen reaction bed A1 through a No. 1 liquid heat exchange medium circulating pump 17 to be used for absorbing hydrogen. At this time, the hydrogen reaction bed A2 and the hydrogen reaction bed B2 are correspondingly subjected to low-pressure expansion cycles, and the specific processes are as follows: hydrogen is discharged from a hydrogen reaction bed B2 at 0.03MPa and-209 ℃, the discharged hydrogen enters a low-pressure expansion machine 12 to do expansion work and generate power, the hydrogen at the outlet of the low-pressure expansion machine 12 is at-223.9 ℃ and 0.012MPa, enters the tube pass inlet of a cooler 29 to exchange heat with air, the temperature is raised to-200 ℃, then the hydrogen enters a hydrogen reaction bed A2 from the tube pass outlet of the cooler 29 to absorb hydrogen, the hydrogen is absorbed by the hydrogen reaction bed A2 at-200 ℃ and 0.012MPa, and simultaneously the heat discharged when the hydrogen is absorbed by the hydrogen reaction bed A2 is transferred to the hydrogen reaction bed B2 through a No. 2 liquid heat exchange medium circulating pump 18 to be used for discharging hydrogen.

When the hydrogen reaction bed A1 and the hydrogen reaction bed B1 are subjected to a low-pressure expansion cycle, the specific process is as follows: hydrogen is discharged from a hydrogen reaction bed B1 at 0.03MPa and-209 ℃, the discharged hydrogen enters a low-pressure expansion machine 12 to do expansion work and generate power, the hydrogen at the outlet of the low-pressure expansion machine 12 is at-223.9 ℃ and 0.012MPa, enters the tube pass inlet of a cooler 29 to exchange heat with air, the temperature is raised to-200 ℃, then the hydrogen enters a hydrogen reaction bed A1 from the tube pass outlet of the cooler 29 to absorb hydrogen, the hydrogen is absorbed by the hydrogen reaction bed A1 at-200 ℃ and 0.012MPa, and simultaneously the heat discharged when the hydrogen is absorbed by the hydrogen reaction bed A1 is transferred to the hydrogen reaction bed B1 through a No. 2 liquid heat exchange medium circulating pump 18 to be used for discharging hydrogen. At this time, the hydrogen reaction bed A2 and the hydrogen reaction bed B2 are respectively subjected to high-pressure expansion cycles, and the specific processes are as follows: the hydrogen reaction bed A2 releases hydrogen at 10 ℃ and 0.5MPa, the released hydrogen enters a high-pressure expansion machine 11 to do work through expansion, the hydrogen at the outlet of the high-pressure expansion machine 11 enters an internal heat exchanger at-55.7 ℃ and 0.2MPa to exchange heat with the environment, the temperature is raised to 19 ℃, the hydrogen enters a hydrogen reaction bed B2 to absorb the hydrogen at 0.2MPa and 19 ℃, and simultaneously the heat released when the hydrogen is absorbed by the hydrogen reaction bed B2 is transferred to the hydrogen reaction bed A2 through a No. 1 liquid heat exchange medium circulating pump 17 to be used for absorbing the hydrogen. Through the above cycle reciprocation, the high pressure expander 11 and the low pressure expander 12 continuously perform work.

When hydrogen reaction bed a1 and hydrogen reaction bed B1 are undergoing a low pressure expansion cycle, hydrogen reaction bed a2 and hydrogen reaction bed B2 are undergoing a high pressure expansion cycle, and when hydrogen reaction bed a1 and hydrogen reaction bed B1 are undergoing a high pressure expansion cycle, hydrogen reaction bed a2 and hydrogen reaction bed B2 are undergoing a low pressure expansion cycle. The high-low pressure expansion cycle is alternatively carried out, and the high-low pressure expander continuously operates.

In the embodiment, the high-temperature heat exchange medium and the low-temperature heat exchange medium are both liquid n-butane, the high-temperature heat exchange medium works at a temperature of 10-19 ℃, and the low-temperature heat exchange medium works at a temperature of-200 to-209 ℃. Because the circulation process of the heat exchange medium has very high frequency and needs to be switched for more than 200 times per minute, the retention time of the heat exchange medium in a high-temperature working interval of 10-19 ℃ is very short, so that the heat exchange medium enters a low-temperature working interval of-200 to-209 ℃ without being vaporized. Through the high-frequency quick switching of the heat exchange medium, the liquid n-butane used in the embodiment can be always kept to be not gasified and not to be solid under the condition that the used liquid n-butane is used as the heat exchange medium. The temperature of the center of gravity is-50 ℃.

The hydrogen outlet of each hydrogen reaction bed is provided with a filtering membrane 23 which only allows hydrogen to pass through and not allows normal butane to pass through. A gas-liquid separator 27 is provided at each liquid outlet of the hydrogen reaction bed to allow only n-butane to pass therethrough and not hydrogen gas to pass therethrough.

In this embodiment, the flow rate of hydrogen absorbed/released by the metal hydrogen storage material is 0.064kg/s, the circulating heat exchange is liquid n-butane, the average output power of the system is 62kw, the forward flow is switched once for 300ms in the reverse flow for 300ms, the operation frequency is 200 times per minute, the redundancy equivalent is 25 times (1 time redundancy equivalent refers to the minimum amount of metal hydrogen storage material required when the metal hydrogen storage material is saturated by hydrogen absorption once in the whole complete process cycle), and the amount of metal hydrogen storage material in each hydrogen reaction bed is 17.6L. The average grain size of the metal hydride is 500 nm. And a grating device is arranged at the inlet and the outlet of each temperature changer, and the grating device only allows hydrogen to pass through and does not allow metal hydride particles to leak from the grating.

The above-mentioned embodiments are only used for illustrating the technical solutions of the present application, and not for limiting the same; although the present application has been described in detail with reference to the foregoing embodiments, it should be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; such modifications and substitutions do not substantially depart from the spirit and scope of the embodiments of the present application and are intended to be included within the scope of the present application.

30页详细技术资料下载

上一篇：一种医用注射器针头装配设备

下一篇：一种提高汽轮机效率的改进朗肯循环动力系统

Reversible compressor/expander work-doing system

相关技术

网友询问留言