Liquid hydrogen tank car evaporated gas cold energy recovery equipment and working method thereof

Abstract

The application discloses a liquid hydrogen tank car evaporated gas cold energy recovery equipment and a working method thereof. The liquid hydrogen tank car evaporated gas cold energy recovery equipment comprises a hydrogen liquefaction heat exchanger, a normal and secondary hydrogen conversion unit, a processing unit and a staged recovery unit. The hydrogen liquefaction heat exchanger is provided with a cooling pipe group and a heating pipe group. The heating pipe group comprises a first heating pipeline. The staged recovery unit comprises a staged recovery pipe group, a temperature sensor and a valve group. The staged recovery pipe group comprises a main pipeline, a cold pipe group and a hydrogen return pipe group. The valve group comprises at least one first valve and at least one second valve. A controller controls the first valve or the second valve to be opened according to the feedback of the temperature sensor. The application automatically classifies the cold energy of hydrogen evaporated gas to recycle hydrogen evaporation below a predetermined temperature value as a cold source required for heat exchange of raw hydrogen gas. Compared with a compression refrigeration mode, the application greatly saves electric energy and effectively reduces the power consumption.

Description

Technical Field

[0001] This application relates to the field of hydrogen liquefaction technology, and in particular to a liquid hydrogen tanker vapor gas cooling energy recovery device and its working method. Background Technology

[0002] Liquid hydrogen reverse-filling systems generally lack expensive liquid hydrogen pumps, requiring liquid hydrogen tank trucks to maintain high pressure to drive the flow of liquid hydrogen and complete the reverse-filling operation. To prevent air from entering the tank truck's vapor space and forming an explosive mixture, a certain liquid level must be maintained after reverse-filling to ensure the vapor space remains saturated with hydrogen vapor. However, this design causes the tank truck to continuously heat up due to thermal leakage during its return journey to the liquid hydrogen plant, triggering liquid hydrogen vaporization and generating a large amount of hydrogen vapor gas, leading to a pressure increase within the tank truck. To ensure safety before loading, excess pressure must be released promptly to avoid the risk of overpressure.

[0003] Currently, the hydrogen vapor discharged during the depressurization process is usually reheated in an ambient air vaporizer and then compressed in a circulating compressor, ultimately being reused as recycled hydrogen in the liquefaction process. Although this process achieves the recovery and utilization of hydrogen molecules, the high-grade cold energy carried by the liquid hydrogen evaporation is not effectively utilized due to direct emission, resulting in significant energy waste. Summary of the Invention

[0004] To address the aforementioned technical problems and achieve at least one advantage of this application, this application provides a liquid hydrogen tanker vapor energy recovery device, the liquid hydrogen tanker vapor energy recovery device comprising:

[0005] A hydrogen liquefaction heat exchanger, the hydrogen liquefaction heat exchanger having a cooling tube group and a heating tube group, the heating tube group including a first heating pipe;

[0006] The intermediate hydrogen conversion unit is connected to the cooling tube group. After the raw material hydrogen is introduced into the cooling tube group, it is cooled in the hydrogen liquefaction heat exchanger and then converted by the intermediate hydrogen conversion unit.

[0007] The processing unit has a cooling pipe assembly connected to it to introduce the converted raw material hydrogen into it. The first heating pipe is connected to the processing unit. The converted raw material hydrogen is processed by the processing unit to obtain hydrogen, which is then introduced into the first heating pipe, heated in the hydrogen liquefaction heat exchanger, and then discharged.

[0008] A staged recovery unit includes a staged recovery pipe assembly, a temperature sensor, and a valve assembly. The staged recovery pipe assembly includes a main pipe, a cooling pipe assembly, and a gas return pipe assembly. The main pipe is connected to a liquid hydrogen tanker. The valve assembly includes at least one first valve and at least one second valve, which are respectively installed on the cooling pipe assembly and the gas return pipe assembly. The temperature sensor is installed on the main pipe to detect the temperature of the hydrogen vapor flowing through it. The cooling pipe assembly and the gas return pipe assembly are connected to the portions of the main pipe furthest from the temperature sensor from the liquid hydrogen tanker. One end of the cooling pipe assembly furthest from the main pipe is connected to a first heating pipe. The temperature sensor is communicatively connected to a controller. The first valve and the second valve are controllably connected to the controller.

[0009] According to one embodiment of this application, the cold pipe assembly includes a first cold pipe and a second cold pipe. Two first valves are provided, one on the first cold pipe and the other on the second cold pipe. One end of the first cold pipe and one end of the second cold pipe are both connected to the main pipeline. The other ends of the first cold pipe and the second cold pipe are both connected to the first heating pipeline. The position where the first cold pipe is connected to the first heating pipeline is between the position where the processing unit is connected to the first heating pipeline and the position where the second cold pipe is connected to the first heating pipeline. A first recovery temperature and a second recovery temperature are defined for temperatures below a predetermined value, wherein the first recovery temperature is lower than the second recovery temperature. After the temperature sensor detects that the temperature of the hydrogen vapor in the main pipeline is the first recovery temperature or the second recovery temperature, the controller controls the first valve on the first cold pipe or the first valve on the second cold pipe to be opened based on the feedback from the temperature sensor.

[0010] According to one embodiment of this application, the processing unit includes a processing group, a connecting pipe group, and a pressure-reducing valve group. The processing group includes a liquid hydrogen separator, the connecting pipe group includes a first feed pipe, and the pressure-reducing valve group includes a first pressure-reducing valve. One end of the first feed pipe is connected to the cooling pipe group to be introduced with converted raw material hydrogen. The liquid hydrogen separator is connected to the other end of the first feed pipe. The first pressure-reducing valve is installed on the first feed pipe to reduce the pressure of the converted raw material hydrogen flowing to the liquid hydrogen separator to obtain a hydrogen mixture. The hydrogen mixture introduced into the liquid hydrogen separator through the first feed pipe undergoes gas-liquid separation in the liquid hydrogen separator to obtain liquid hydrogen and hydrogen gas. The processing group includes a liquid hydrogen subcooler. The liquid hydrogen separator is connected to the liquid hydrogen subcooler through a pipe to introduce liquid hydrogen into the liquid hydrogen subcooler. The liquid hydrogen is cooled in the liquid hydrogen subcooler. The connecting pipe assembly includes a first discharge pipe connected to the liquid hydrogen subcooler. Liquid hydrogen cooled by the liquid hydrogen subcooler is discharged through the first discharge pipe. The connecting pipe assembly also includes a second inlet pipe. The pressure reducing valve assembly includes a second pressure reducing valve. The two ends of the second inlet pipe are respectively connected to the first discharge pipe and the liquid hydrogen subcooler. The second pressure reducing valve is installed on the second inlet pipe. A portion of the liquid hydrogen flowing through the first discharge pipe is introduced into the second inlet pipe and, after being depressurized by the second pressure reducing valve, is introduced into the liquid hydrogen subcooler. The depressurized liquid hydrogen serves as a cold source to exchange heat and increase its temperature in the liquid hydrogen subcooler to obtain hydrogen gas. The connecting pipe assembly also includes a second discharge pipe. The two ends of the second discharge pipe are respectively connected to the liquid hydrogen subcooler and one end of the first heating pipe. Hydrogen gas in the liquid hydrogen subcooler is introduced into the first heating pipe through the second discharge pipe.

[0011] According to one embodiment of this application, the pressure-reducing valve assembly further includes a fourth pressure-reducing valve, which is installed on the first discharge pipe. The second feed pipe is connected to the first discharge pipe at a position between the fourth pressure-reducing valve and the liquid hydrogen subcooler, which are each connected to the first discharge pipe. The liquid hydrogen tanker evaporation gas cooling energy recovery equipment further includes a storage unit. A portion of the liquid hydrogen flowing through the first discharge pipe is depressurized by the fourth pressure-reducing valve and then guided to the storage unit.

[0012] According to one embodiment of this application, the connecting pipe assembly further includes a third discharge pipe, and the heating pipe assembly includes a second heating pipe. The two ends of the third discharge pipe are respectively connected to one end of the liquid hydrogen separator and one end of the second heating pipe. The hydrogen obtained by gas-liquid separation in the liquid hydrogen separator is introduced into the second heating pipe through the third discharge pipe to exchange heat and be heated in the hydrogen liquefaction heat exchanger.

[0013] According to one embodiment of this application, the hydrogen liquefaction heat exchanger further includes a cooling pipe assembly, which includes a first cooling pipe. The connecting pipe assembly also includes a third feed pipe, one end of which is connected to the first cooling pipe. Circulating hydrogen is introduced into the first cooling pipe to exchange heat and cool down in the hydrogen liquefaction heat exchanger before being introduced into the third feed pipe. The pressure reducing valve assembly also includes a third pressure reducing valve, which is installed on the third feed pipe. The end of the third feed pipe away from the first cooling pipe is connected to the portion of the first feed pipe located between the first pressure reducing valve and the liquid hydrogen separator. The circulating hydrogen introduced into the third feed pipe is depressurized by the third pressure reducing valve to obtain a hydrogen mixture. The hydrogen mixture depressurized by the third pressure reducing valve is introduced into the first feed pipe and introduced into the liquid hydrogen separator together with the hydrogen mixture depressurized by the first pressure reducing valve.

[0014] According to one embodiment of this application, the cooling pipe assembly further includes a second cooling pipe, the processing unit further includes an expander unit, and the connecting pipe assembly further includes a make-up cooling pipe. The expander unit is installed on the make-up cooling pipe, and the two ends of the make-up cooling pipe are respectively connected to one end of the second cooling pipe and the third discharge pipe. Circulating hydrogen is introduced into the second cooling pipe to exchange heat and cool down in the hydrogen liquefaction heat exchanger, and then introduced into the make-up cooling pipe and expanded and cooled by the expander unit before being introduced into the third discharge pipe. It is then introduced into the second heating pipe together with the hydrogen obtained from gas-liquid separation in the liquid hydrogen separator. The cooling amount obtained by the circulating hydrogen flowing through the second cooling pipe in the hydrogen liquefaction heat exchanger is less than the cooling amount obtained by the circulating hydrogen flowing through the first cooling pipe in the hydrogen liquefaction heat exchanger.

[0015] According to one embodiment of this application, the liquid hydrogen tanker evaporation gas cold energy recovery equipment includes a pipeline group, which includes an inlet pipe group and an outlet pipe group. The inlet pipe group includes a first inlet pipe and a second inlet pipe, and the outlet pipe group includes a first outlet pipe and a second outlet pipe. The first inlet pipe is connected to the cooling pipe group to introduce raw material hydrogen into the cooling pipe group. The second inlet pipe is connected to the cooling absorption pipe group to introduce circulating hydrogen into the cooling absorption pipe group. The first outlet pipe is connected to the end of the first heating pipe away from the second discharge pipe, and the first outlet pipe is used to discharge the hydrogen that has been heated by flowing through the first heating pipe. The second outlet pipe is connected to the end of the second heating pipe away from the third discharge pipe, and the second outlet pipe is used to discharge the hydrogen that has been heated by flowing through the second heating pipe. The liquid hydrogen tanker evaporation gas cold energy recovery equipment includes a temperature control mechanism. The temperature control mechanism includes a liquid nitrogen temperature zone heat exchanger, a hydrogen booster unit, and a nitrogen cooling unit. The liquid nitrogen temperature zone heat exchanger is installed on the first inlet pipe, the second inlet pipe, the first outlet pipe, and the second outlet pipe. The nitrogen cooling unit is connected to the liquid nitrogen temperature zone heat exchanger to supply cooling to it. The ends of the first outlet pipe and the second outlet pipe, away from the hydrogen liquefaction heat exchanger, are connected to the hydrogen booster unit. Hydrogen flowing through the first outlet pipe and the second outlet pipe is heated by heat exchange in the liquid nitrogen temperature zone heat exchanger and then guided to the hydrogen booster unit for compression to obtain circulating hydrogen. The end of the second inlet pipe away from the hydrogen liquefaction heat exchanger is connected to the hydrogen booster unit to introduce circulating hydrogen. The circulating hydrogen flowing through the second inlet pipe is cooled by heat exchange in the liquid nitrogen temperature zone heat exchanger and then introduced into the cold absorption pipe assembly after low-temperature adsorption.

[0016] According to one embodiment of this application, the gas return pipe assembly includes a first gas return pipe and a second gas return pipe. Two second valves are provided, one on each of the first and second gas return pipes. One end of the first gas return pipe and one end of the second gas return pipe are both connected to the main pipeline. The other end of the first gas return pipe is connected to the portion of the first outlet pipe located between the hydrogen liquefaction heat exchanger and the liquid nitrogen temperature zone heat exchanger. The other end of the second gas return pipe is connected to the portion of the first outlet pipe located between the liquid nitrogen temperature zone heat exchanger and the hydrogen booster unit. The temperature control mechanism further includes... An ambient air vaporizer is installed on the second gas return pipe to vaporize the liquid portion of the hydrogen vaporized gas flowing through the second gas return pipe. Temperatures higher than a predetermined value are defined as a third recovery temperature and a fourth recovery temperature, wherein the third recovery temperature is lower than the fourth recovery temperature. After a temperature sensor detects that the temperature of the hydrogen vaporized gas in the main pipe is the third recovery temperature or the fourth recovery temperature, the controller controls the second valve located on the first gas return pipe or the second valve located on the second gas return pipe to open based on feedback from the temperature sensor.

[0017] To address the aforementioned technical problems and achieve at least one advantage of this application, this application provides a method for operating a liquid hydrogen tanker evaporator gas cooling energy recovery device, the method comprising the following steps:

[0018] The temperature sensor detects the temperature of the hydrogen vapor in the main pipeline, and when the temperature is detected to be lower than a predetermined value, the controller controls the first valve to be opened so that the hydrogen vapor is introduced from the main pipeline into the cooling pipe group, and then from the cooling pipe group into the first heating pipeline.

[0019] After the raw material hydrogen is introduced into the cooling tube assembly, it is cooled and heated in the hydrogen liquefaction heat exchanger and then converted by the positive and negative hydrogen conversion unit. The converted raw material hydrogen is processed by the processing unit to obtain liquid hydrogen and hydrogen gas. The hydrogen gas is introduced into the first heating pipe to mix with the hydrogen vapor introduced into the first heating pipe, and together they serve as the cold source for the heat exchange operation in the hydrogen liquefaction heat exchanger.

[0020] The beneficial effects of this application include:

[0021] 1. This application automatically and reasonably classifies the cooling capacity of hydrogen vaporization gas, so as to recover and reuse the hydrogen vaporization below the predetermined temperature value as the cold source required for heat exchange of raw hydrogen. Compared with the method of using only compressor refrigeration, it greatly saves electricity and effectively reduces electricity costs.

[0022] 2. Since the temperature of the hydrogen vapor is lower than the predetermined temperature value, this application recovers the cold energy of the hydrogen vapor in stages so that the cold energy of the hydrogen vapor at different temperatures can be fully utilized, thereby achieving efficient recovery of cold energy.

[0023] 3. The hydrogen liquefaction heat exchanger, the processing unit, and the temperature control mechanism described in this application constitute a circulating system. The hydrogen vapor in the liquid hydrogen tanker enters the circulating system through the staged recovery unit. This not only allows hydrogen molecules to be recovered and improves the liquid hydrogen acquisition rate, but also allows for staged processing of the hydrogen vapor according to its actual temperature, realizing the cascade recovery of cold energy and improving the cold energy recovery rate.

[0024] 4. This application considers both the timely depressurization and hydrogen recovery operation and the non-depressurization operation. That is, in the depressurization and hydrogen recovery operation, by recovering and utilizing the cold energy, the load of the hydrogen booster unit and the expander unit can be increased while the load of the nitrogen cooling unit remains unchanged, which can meet the usage requirements. In conventional processes, it is necessary to increase the load of the nitrogen cycle compressor and nitrogen cycle expander, as well as the load of the hydrogen cycle compressor and hydrogen cycle expander, to generate enough cold energy to meet the heat exchange requirements in the liquid nitrogen temperature zone heat exchanger. In comparison, this application greatly narrows the variable load range of the equipment, reduces the difficulty of selection, and thus reduces investment costs. Attached Figure Description

[0025] Figure 1 A schematic diagram of the liquid hydrogen tanker evaporation gas cooling energy recovery device described in this application is shown.

[0026] Figure 2 A partial structural schematic diagram of the liquid hydrogen tanker evaporation gas cooling energy recovery device described in this application is shown.

[0027] Figure 3 This paper shows another partial structural schematic diagram of the liquid hydrogen tanker evaporation gas cooling energy recovery device described in this application.

[0028] Figure label:

[0029] 10. Hydrogen liquefaction heat exchanger; 11. Cooling tube assembly; 111. Cooling pipe; 12. Heating tube assembly; 121. First heating pipe; 122. Second heating pipe; 13. Cold suction tube assembly; 131. First cold suction pipe; 132. Second cold suction pipe;

[0030] 20. Negative-toluene hydrogen conversion unit; 21. Negative-toluene hydrogen converter; 22. Circulation pipeline;

[0031] 30. Processing unit; 31. Processing group; 311. Liquid hydrogen separator; 312. Liquid hydrogen subcooler; 32. Connecting pipe assembly; 321. First feed pipe; 322. First discharge pipe; 323. Second feed pipe; 324. Second discharge pipe; 325. Third discharge pipe; 326. Third feed pipe; 327. Cooling supply pipe; 33. Pressure reducing valve assembly; 331. First pressure reducing valve; 332. Second pressure reducing valve; 333. Third pressure reducing valve; 334. Fourth pressure reducing valve; 34. Expander unit;

[0032] 40. Graded recycling unit; 41. Graded recycling pipe assembly; 411. Main pipeline; 412. Cold use pipe assembly; 4121. First cold use pipe; 4122. Second cold use pipe; 413. Gas return pipe assembly; 4131. First gas return pipe; 4132. Second gas return pipe; 42. Temperature sensor; 43. Valve assembly; 431. First valve; 432. Second valve;

[0033] 50. Storage unit; 51. Liquid hydrogen storage tank; 52. Connecting unit; 521. Inlet pipe assembly; 522. Outlet pipe assembly; 53. Switching valve assembly; 531. First switching valve; 532. Second switching valve;

[0034] 60. Pipe assembly; 61. Inlet pipe assembly; 611. First inlet pipe; 612. Second inlet pipe; 62. Outlet pipe assembly; 621. First outlet pipe; 622. Second outlet pipe;

[0035] 70. Temperature control mechanism; 71. Liquid nitrogen temperature zone heat exchanger; 72. Hydrogen booster unit; 73. Nitrogen cooling unit; 74. Ambient air vaporizer. Detailed Implementation

[0036] The following description is intended to disclose this application and enable those skilled in the art to implement it. The preferred embodiments described below are merely examples, and other obvious variations will occur to those skilled in the art. The basic principles of this application defined in the following description can be applied to other embodiments, modifications, improvements, equivalents, and other technical solutions that do not depart from the spirit and scope of this application.

[0037] Those skilled in the art should understand that, in the disclosure of this application, the terms "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," and "outer," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, the above terms should not be construed as limitations on this application.

[0038] It is understood that the term "a" should be understood as "at least one" or "one or more", that is, in one embodiment, the number of an element can be one, while in another embodiment, the number of the element can be multiple, and the term "a" should not be understood as a limitation on the number.

[0039] refer to Figures 1 to 3 A preferred embodiment of the liquid hydrogen tanker evaporator gas cooling energy recovery device according to this application will be described in detail below. The liquid hydrogen tanker evaporator gas cooling energy recovery device includes a hydrogen liquefaction heat exchanger 10 and a neutral hydrogen conversion unit 20. The hydrogen liquefaction heat exchanger 10 has a cooling tube assembly 11. The neutral hydrogen conversion unit 20 is connected to the cooling tube assembly 11. After the raw material hydrogen is introduced into the cooling tube assembly 11, it exchanges heat and cools in the hydrogen liquefaction heat exchanger 10 and is converted by the neutral hydrogen conversion unit 20 to convert neutral hydrogen into neutral hydrogen.

[0040] The liquid hydrogen tanker evaporator gas cold energy recovery equipment also includes a processing unit 30. One end of the cooling pipe assembly 11 is connected to the processing unit 30 to introduce the converted raw material hydrogen into the processing unit 30. The hydrogen liquefaction heat exchanger 10 also has a heating pipe assembly 12, which includes a first heating pipe 121, one end of which is connected to the processing unit 30. The converted raw material hydrogen is processed by the processing unit 30 to obtain liquid hydrogen and hydrogen gas. After the hydrogen gas is introduced into the first heating pipe 121, it exchanges heat and is heated in the hydrogen liquefaction heat exchanger 10 before being discharged, so as to use the hydrogen gas as a cold source for the raw material hydrogen.

[0041] It is worth mentioning that the liquid hydrogen tanker vapor gas cooling energy recovery equipment also includes a staged recovery unit 40. The staged recovery unit 40 includes a staged recovery pipe assembly 41, a temperature sensor 42, and a valve assembly 43. The staged recovery pipe assembly 41 includes a main pipe 411, a cooling pipe assembly 412, and a gas return pipe assembly 413. One end of the main pipe 411 is connected to a liquid hydrogen tanker. The hydrogen vapor gas in the liquid hydrogen tanker is purged and replaced to ensure its oxygen content meets the standard before being introduced into the main pipe 411. The valve assembly 43 includes at least one first valve 431 and at least one second valve 432. The first valve 431 is installed in the cooling pipe assembly 412, and the second valve 432 is installed in the gas return pipe assembly 413. The temperature sensor 42 is installed on the main pipe 411 to detect the temperature of the hydrogen vapor gas flowing through the main pipe 411. The cooling pipe assembly 412 and the gas return pipe assembly 413 are connected to the portion of the main pipeline 411 located away from the temperature sensor 42 and the liquid hydrogen tanker. One end of the cooling pipe assembly 412, away from the main pipeline 411, is connected to the first heating pipe 121. The temperature sensor 42 is communicatively connected to a controller, and the first valve 431 and the second valve 432 are controllably connected to the controller. The controller controls the opening of either the first valve 431 or the second valve 432 based on feedback from the temperature sensor 42.

[0042] Preferably, the oxygen content in the hydrogen evaporation gas inside the main pipeline 411 is less than 1 ppb.

[0043] Specifically, when the temperature sensor 42 detects that the temperature of the hydrogen vapor in the main pipe 411 is higher than a predetermined value, the controller controls the second valve 432 to open, so that the hydrogen vapor is introduced from the main pipe 411 into the gas return pipe assembly 413; when the temperature sensor 42 detects that the temperature of the hydrogen vapor in the main pipe 411 is lower than a predetermined value, the controller controls the first valve 431 to open, so that the hydrogen vapor is introduced from the main pipe 411 into the cooling pipe assembly 412, and then from the cooling pipe assembly 412 into the first heating pipe 121, so as to mix with the hydrogen introduced from the processing unit 30 into the first heating pipe 121, and together serve as a cold source for cooling the raw material hydrogen in the hydrogen liquefaction heat exchanger 10 by heat exchange.

[0044] In this way, the present application automatically and reasonably classifies the cooling capacity of the hydrogen vaporized gas, so as to recover and reuse the hydrogen vaporized gas below the predetermined temperature value as the cold source required for the heat exchange of the raw hydrogen. Compared with the method of using only compressor refrigeration, it saves a lot of electricity and thus effectively reduces electricity costs.

[0045] Preferably, the cooling pipe assembly 412 includes a first cooling pipe 4121 and a second cooling pipe 4122. Two first valves 431 are provided, one on the first cooling pipe 4121 and the other on the second cooling pipe 4122. One end of the first cooling pipe 4121 and one end of the second cooling pipe 4122 are both connected to the main pipe 411, and the other ends of the first cooling pipe 4121 and the second cooling pipe 4122 are both connected to the first heating pipe 121. The position where the first cooling pipe 4121 is connected to the first heating pipe 121 is between the position where the processing unit 30 is connected to the first heating pipe 121 and the position where the second cooling pipe 4122 is connected to the first heating pipe 121. A first recovery temperature and a second recovery temperature are defined for temperatures below a predetermined value, wherein the first recovery temperature is lower than the second recovery temperature. After the temperature sensor 42 detects that the temperature of the hydrogen vapor in the main pipe 411 is the first recovery temperature or the second recovery temperature, the controller controls the first valve 431 set on the first cooling pipe 4121 or the first valve 431 set on the second cooling pipe 4122 to be opened according to the feedback of the temperature sensor 42.

[0046] Specifically, when the temperature sensor 42 detects that the temperature of the hydrogen vaporized gas in the main pipe 411 is the first recovery temperature, the controller controls the first valve 431 installed on the first cooling pipe 4121 to be opened, so that the hydrogen vaporized gas flowing through the main pipe 411 is introduced into the first heating pipe 121 through the first cooling pipe 4121; when the temperature sensor 42 detects that the temperature of the hydrogen vaporized gas in the main pipe 411 is the second recovery temperature, the controller controls the first valve 431 installed on the second cooling pipe 4122 to be opened, so that the hydrogen vaporized gas flowing through the main pipe 411 is introduced into the first heating pipe 121 through the second cooling pipe 4122. In this way, based on the fact that the temperature of the hydrogen vaporized gas is lower than the predetermined temperature value, the cold energy of the hydrogen vaporized gas is recovered in stages, so that the cold energy of the hydrogen vaporized gas at different temperatures is fully utilized, achieving efficient cold energy recovery.

[0047] Furthermore, the antho-parahydrogen converter unit 20 includes multiple antho-parahydrogen converters 21 and multiple circulation pipes 22, with each antho-parahydrogen converter 21 installed on a circulation pipe 22. The cooling pipe group 11 includes multiple cooling pipes 111, the number of which is one more than the number of antho-parahydrogen converters 21. Each circulation pipe 22 is connected to a cooling pipe 111 at both ends. The feedstock hydrogen gas is cooled after passing through each cooling pipe 111. The feedstock hydrogen gas in the cooling pipe 111 connected to the circulation pipe 22 is introduced into the corresponding circulation pipe 22 after cooling and converted by the corresponding antho-parahydrogen converter 21 before being introduced into another cooling pipe 111 connected to the corresponding circulation pipe 22.

[0048] Preferably, four positive and negative hydrogen converters 21 are provided, the number of circulation pipes 22 is the same as the number of positive and negative hydrogen converters 21, and five cooling pipes 111 are provided, so that the raw material hydrogen undergoes five rounds of cooling operations and four rounds of conversion operations. A cooling operation is performed before each round of conversion to ensure that the positive hydrogen in the raw material hydrogen is converted into negative hydrogen as much as possible, so as to prevent excessive positive hydrogen from remaining and avoid a situation where a large amount of positive hydrogen spontaneously converts into negative hydrogen and releases heat, causing the overall temperature to be too high, thus ensuring that the subsequent liquid hydrogen acquisition operation is not affected.

[0049] Specifically, the temperature of the raw material hydrogen flowing through one cooling pipe 111 and being converted by one intermediate hydrogen converter 21 is -213 to -211°C; the temperature of the raw material hydrogen flowing through two cooling pipes 111 and being converted by two intermediate hydrogen converters 21 is -230 to -228°C; the temperature of the raw material hydrogen flowing through three cooling pipes 111 and being converted by three intermediate hydrogen converters 21 is -236 to -234°C; the temperature of the raw material hydrogen flowing through four cooling pipes 111 and being converted by four intermediate hydrogen converters 21 is -242 to -240°C; and the temperature of the converted raw material hydrogen flowing through the last cooling pipe 111 and exiting the hydrogen liquefaction heat exchanger 10 after being converted by four intermediate hydrogen converters 21 is -242 to -240°C.

[0050] Further, the processing unit 30 includes a processing group 31, a connecting pipe group 32, and a pressure reducing valve group 33. The processing group 31 includes a liquid hydrogen separator 311. The connecting pipe group 32 includes a first feed pipe 321. The pressure reducing valve group 33 includes a first pressure reducing valve 331. One end of the first feed pipe 321 is connected to the cooling pipe group 11 to be introduced with converted raw material hydrogen. The liquid hydrogen separator 311 is connected to the other end of the first feed pipe 321. The first pressure reducing valve 331 is installed on the first feed pipe 321 to reduce the pressure of the converted raw material hydrogen flowing to the liquid hydrogen separator 311 to obtain a hydrogen mixture. The hydrogen mixture introduced into the liquid hydrogen separator 311 through the first feed pipe 321 undergoes gas-liquid separation in the liquid hydrogen separator 311 to obtain liquid hydrogen and hydrogen gas.

[0051] Furthermore, the processing unit 31 includes a liquid hydrogen subcooler 312. The liquid hydrogen separator 311 is connected to the liquid hydrogen subcooler 312 via a pipeline to introduce liquid hydrogen into the liquid hydrogen subcooler 312, where the liquid hydrogen is cooled. The connecting pipe assembly 32 includes a first discharge pipe 322, which is connected to the liquid hydrogen subcooler 312. The liquid hydrogen cooled by the liquid hydrogen subcooler 312 is discharged through the first discharge pipe 322. The connecting pipe assembly 32 further includes a second feed pipe 323, and the pressure reducing valve assembly 33 includes a second pressure reducing valve 332. The two ends of the second feed pipe 323 are respectively connected to the first discharge pipe 322 and the liquid hydrogen subcooler 312. The second pressure reducing valve 332 is installed on the second feed pipe 323. The liquid hydrogen flowing through the first discharge pipe 322 is introduced into the second feed pipe 323 and, after being depressurized by the second pressure reducing valve 332, is introduced into the liquid hydrogen subcooler 312. The depressurized liquid hydrogen serves as a cold source to exchange heat and increase temperature in the liquid hydrogen subcooler 312 to obtain hydrogen gas. The connecting pipe assembly 32 also includes a second discharge pipe 324, the two ends of which are respectively connected to one end of the liquid hydrogen subcooler 312 and one end of the first heating pipe 121. The hydrogen in the liquid hydrogen subcooler 312 is introduced into the first heating pipe 121 through the second discharge pipe 324 to serve as a cold source for heat exchange operation in the hydrogen liquefaction heat exchanger 10.

[0052] Furthermore, the connecting pipe assembly 32 also includes a third discharge pipe 325, and the heating pipe assembly 12 includes a second heating pipe 122. The two ends of the third discharge pipe 325 are respectively connected to the liquid hydrogen separator 311 and one end of the second heating pipe 122. The hydrogen obtained through gas-liquid separation in the liquid hydrogen separator 311 is introduced into the second heating pipe 122 through the third discharge pipe 325 to exchange heat and increase its temperature within the hydrogen liquefaction heat exchanger 10, thus serving as a cold source for the heat exchange operation within the hydrogen liquefaction heat exchanger 10. In this way, the hydrogen flowing through the first heating pipe 121 and the hydrogen flowing through the second heating pipe 122 work together to provide sufficient cold source, eliminating the need for additional cooling energy and effectively reducing operating costs.

[0053] Furthermore, the hydrogen liquefaction heat exchanger 10 also includes a cooling pipe assembly 13, which includes a first cooling pipe 131. The connecting pipe assembly 32 further includes a third feed pipe 326, one end of which is connected to the first cooling pipe 131. Circulating hydrogen is introduced into the first cooling pipe 131 to exchange heat and cool down within the hydrogen liquefaction heat exchanger 10 before being introduced into the third feed pipe 326. The pressure reducing valve assembly 33 further includes a third pressure reducing valve 333, which is installed on the third feed pipe 326. The end of the third feed pipe 326 away from the first cooling pipe 131 is connected to the portion of the first feed pipe 321 located between the first pressure reducing valve 331 and the liquid hydrogen separator 311. The circulating hydrogen introduced into the third feed pipe 326 is depressurized by the third pressure reducing valve 333 to obtain a hydrogen mixture. The hydrogen mixture obtained by the pressure reducing valve 333 is introduced into the first feed pipe 321 and together with the hydrogen mixture depressurized by the first pressure reducing valve 331, it is introduced into the liquid hydrogen separator 311 to recover hydrogen molecules and improve the liquid hydrogen acquisition rate.

[0054] Furthermore, the cooling pipe assembly 13 further includes a second cooling pipe 132, the processing unit 30 further includes an expander unit 34, and the connecting pipe assembly 32 further includes a make-up cooling pipe 327. The expander unit 34 is installed on the make-up cooling pipe 327, and the two ends of the make-up cooling pipe 327 are respectively connected to one end of the second cooling pipe 132 and the third discharge pipe 325. Circulating hydrogen is introduced into the second cooling pipe 132 to exchange heat and cool down in the hydrogen liquefaction heat exchanger 10, and then introduced into the make-up cooling pipe 327. After being expanded and cooled by the expander unit 34, it is introduced into the third discharge pipe 325, so that it is introduced into the second heating pipe 122 together with the hydrogen obtained from gas-liquid separation in the liquid hydrogen separator 311. The cooling amount obtained by the circulating hydrogen flowing through the second cooling pipe 132 in the hydrogen liquefaction heat exchanger 10 is less than the cooling amount obtained by the circulating hydrogen flowing through the first cooling pipe 131 in the hydrogen liquefaction heat exchanger 10.

[0055] In this way, the cooling capacity of the circulating hydrogen flowing into the third discharge pipe 325 from the cooling pipe 327 comes from the hydrogen liquefaction heat exchanger 10 and the expander unit 34, saving the cooling energy in the hydrogen liquefaction heat exchanger 10. At the same time, it ensures that the temperature of the hydrogen flowing into the third discharge pipe 325 and being guided to the second cooling pipe 132 is low enough to provide a sufficient cooling source for the heat exchange operation in the hydrogen liquefaction heat exchanger 10.

[0056] Furthermore, the pressure-reducing valve assembly 33 also includes a fourth pressure-reducing valve 334, which is installed on the first discharge pipe 322. The second feed pipe 323 is connected to the first discharge pipe 322 at a position between the fourth pressure-reducing valve 334 and the liquid hydrogen subcooler 312, which are each connected to the first discharge pipe 322. The liquid hydrogen tanker evaporator gas cooling energy recovery equipment also includes a storage unit 50. A portion of the liquid hydrogen flowing through the first discharge pipe 322 is depressurized by the fourth pressure-reducing valve 334 and then guided to the storage unit 50 for storage.

[0057] Preferably, the storage unit 50 includes a liquid hydrogen storage tank 51, a connection unit 52, and a switching valve assembly 53. The connection unit 52 includes at least one inlet pipe assembly 521, with both ends of the inlet pipe assembly 521 connected to one end of the first outlet pipe 322 and the liquid hydrogen storage tank 51, respectively, to introduce liquid hydrogen into the liquid hydrogen storage tank 51. The switching valve assembly 53 includes at least one first switching valve 531, each of the first switching valves 531 being installed on one of the inlet pipe assemblies 521 to control the on / off state of the corresponding inlet pipe assembly 521. The connection unit 52 further includes an outlet pipe assembly 522, with both ends of the outlet pipe assembly 522 connected to the liquid hydrogen storage tank 51 and a liquid hydrogen tanker, respectively, through which liquid hydrogen in the liquid hydrogen storage tank 51 is introduced into the liquid hydrogen tanker. The valve assembly 53 further includes a second valve 532, which is installed on the outlet pipe assembly 522 to control the on / off state of the outlet pipe assembly 522.

[0058] Preferably, there are two inlet pipe groups 521, and the ends of the two inlet pipe groups 521 that are away from the first outlet pipe 322 are respectively connected to the high end and the low end of the liquid hydrogen storage tank 51, so as to be used according to the usage requirements.

[0059] Further, the liquid hydrogen tanker evaporator gas cooling energy recovery equipment includes a pipeline group 60, which includes an inlet pipe group 61 and an outlet pipe group 62. The inlet pipe group 61 includes a first inlet pipe 611 and a second inlet pipe 612, and the outlet pipe group 62 includes a first outlet pipe 621 and a second outlet pipe 622. The first inlet pipe 611 is connected to the cooling pipe group 11 to introduce raw material hydrogen into the cooling pipe group 11. The second inlet pipe 612 is connected to the cooling absorption pipe group 13 to introduce circulating hydrogen into the cooling absorption pipe group 13. The first outlet pipe 621 is connected to the end of the first heating pipe 121 away from the second discharge pipe 324, and the first outlet pipe 621 is used to discharge the hydrogen that has been heated by flowing through the first heating pipe 121. The second outlet pipe 622 is connected to the end of the second heating pipe 122 away from the third discharge pipe 325. The second outlet pipe 622 is used to discharge the hydrogen gas that has been heated by flowing through the second heating pipe 122.

[0060] Furthermore, the liquid hydrogen tanker evaporator gas cooling energy recovery equipment includes a temperature control mechanism 70, which comprises a liquid nitrogen temperature zone heat exchanger 71, a hydrogen booster unit 72, and a nitrogen cooling unit 73. The liquid nitrogen temperature zone heat exchanger 71 is installed on the first inlet pipe 611, the second inlet pipe 612, the first outlet pipe 621, and the second outlet pipe 622. The nitrogen cooling unit 73 is connected to the liquid nitrogen temperature zone heat exchanger 71 to supply cooling to it. The ends of the first outlet pipe 621 and the second outlet pipe 622, each away from the hydrogen liquefaction heat exchanger 10, are connected to the hydrogen booster unit 72. The hydrogen flowing through the first outlet pipe 621 and the second outlet pipe 622 is heated by heat exchange in the liquid nitrogen temperature zone heat exchanger 71 and then guided to the hydrogen booster unit 72 for compression to obtain circulating hydrogen. The end of the second inlet pipe 612 away from the hydrogen liquefaction heat exchanger 10 is connected to the hydrogen booster unit 72 to be introduced with circulating hydrogen. The circulating hydrogen flowing through the second inlet pipe 612 is cooled by heat exchange in the liquid nitrogen temperature zone heat exchanger 71 and then introduced into the cold absorption pipe group 13 after low-temperature adsorption operation.

[0061] Preferably, the hydrogen booster unit 72 is implemented to include a plurality of compressors arranged in series, and the liquid nitrogen temperature zone heat exchanger 71 is implemented to include a plurality of compressors and an expander arranged in series.

[0062] It is worth mentioning that the gas return pipe assembly 413 includes a first gas return pipe 4131 and a second gas return pipe 4132. Two second valves 432 are provided, one on the first gas return pipe 4131 and the other on the second gas return pipe 4132. One end of the first gas return pipe 4131 and one end of the second gas return pipe 4132 are both connected to the main pipe 411. The other end of the first gas return pipe 4131 is connected to the portion of the first outlet pipe 621 located between the hydrogen liquefaction heat exchanger 10 and the liquid nitrogen temperature zone heat exchanger 71. The other end of the second gas return pipe 4132 is connected to the portion of the first outlet pipe 621 located between the liquid nitrogen temperature zone heat exchanger 71 and the hydrogen booster unit 72. The temperature control mechanism 70 also includes an ambient air vaporizer 74, which is installed on the second gas return pipe 4132 to vaporize the liquid portion of the hydrogen vaporized gas flowing through the second gas return pipe 4132. A third recovery temperature and a fourth recovery temperature are defined for temperatures higher than a predetermined value, wherein the third recovery temperature is lower than the fourth recovery temperature. After the temperature sensor 42 detects that the temperature of the hydrogen vaporized gas in the main pipeline 411 is the third recovery temperature or the fourth recovery temperature, the controller controls the second valve 432 located in the first gas return pipe 4131 or the second valve 432 located in the second gas return pipe 4132 to open based on the feedback from the temperature sensor 42.

[0063] Specifically, when the temperature sensor 42 detects that the temperature of the hydrogen vaporized gas in the main pipeline 411 is the third recovery temperature, the controller controls the second valve 432 located in the first gas return pipe 4131 to be opened, so that the hydrogen vaporized gas flowing through the main pipeline 411 is introduced into the first outlet pipe 621 through the first gas return pipe 4131, and then introduced into the liquid nitrogen temperature zone heat exchanger 71 as a cold source; when the temperature sensor 42 detects that the temperature of the hydrogen vaporized gas in the main pipeline 411 is the fourth recovery temperature, the controller controls the second valve 432 located in the second gas return pipe 4132 to be opened, so that the hydrogen vaporized gas flowing through the main pipeline 411 is introduced into the first outlet pipe 621 through the second gas return pipe 4132, and then introduced into the hydrogen booster unit 72 for pressurization. In this way, based on the fact that the temperature of the hydrogen vapor gas is higher than a predetermined value, the hydrogen vapor gas is graded so that the lower temperature hydrogen vapor gas can be used as a cold source for heat exchange operation in the liquid nitrogen temperature zone heat exchanger 71 to recover cold energy and improve the utilization rate of cold energy.

[0064] In summary, the hydrogen liquefaction heat exchanger 10, the processing unit 30, and the temperature control mechanism 70 together constitute a circulation system. The hydrogen vapor in the liquid hydrogen tanker enters the circulation system through the staged recovery unit 40. This not only allows hydrogen molecules to be recovered and improves the liquid hydrogen acquisition rate, but also allows for staged processing of the hydrogen vapor according to its actual temperature, realizing the cascade recovery of cold energy. This ensures that the cold energy of the hydrogen vapor at different temperatures is fully utilized, thereby improving the cold energy recovery rate.

[0065] Furthermore, this application considers both the timely depressurization and hydrogen recovery operation and the no-depressurization operation. That is, in the depressurization and hydrogen recovery operation, by recovering and utilizing the cold energy, the load of the hydrogen booster unit 72 and the expander unit 34 can be increased while the load of the nitrogen cooling unit 73 remains unchanged, which can meet the usage requirements. In conventional processes, it is necessary to increase the load of the nitrogen cycle compressor and nitrogen cycle expander, as well as the load of the hydrogen cycle compressor and hydrogen cycle expander, to generate enough cold energy to meet the heat exchange requirements in the liquid nitrogen temperature zone heat exchanger 71. In comparison, this application greatly narrows the variable load range of the equipment, reduces the difficulty of selection, and thus reduces investment costs.

[0066] Preferably, the first recovery temperature is implemented to be no greater than -240℃, the second recovery temperature is implemented to be -240~-210℃, the third recovery temperature is implemented to be -210~-196℃, and the fourth recovery temperature is implemented to be no less than -196℃. The temperature of the raw material hydrogen after being depressurized by the first pressure-reducing valve 331 is -247~-245℃. The temperature of the hydrogen and liquid hydrogen obtained by gas-liquid separation in the liquid hydrogen separator 311 is both -247~-245℃. The temperature of the liquid hydrogen after being cooled by the liquid hydrogen subcooler 312 is -252~-250℃. The temperature of the liquid hydrogen after being depressurized by the second pressure-reducing valve 332 is -253~-251℃. The temperature of the hydrogen obtained by heat exchange in the liquid hydrogen subcooler 312 is -253~-251℃. The hydrogen obtained from the first heating pipe 12... The temperature of the discharged hydrogen is -157 to -155°C. The temperature of the circulating hydrogen introduced into the cooling pipe group 13 is -157 to -155°C. The temperature of the circulating hydrogen discharged from the first cooling pipe 131 is -244 to -242°C. The temperature of the circulating hydrogen after being depressurized by the third pressure reducing valve 333 is -247 to -245°C. The temperature of the circulating hydrogen discharged from the second cooling pipe 132 is -231 to -299°C. The temperature of the circulating hydrogen after being expanded by the expander unit 34 is -241 to -239°C.

[0067] The following is a proposed method for the operation of a liquid hydrogen tanker evaporation gas cooling energy recovery device, comprising the following steps:

[0068] The temperature sensor 42 detects the temperature of the hydrogen vapor in the main pipe 411, and when the detected temperature is lower than a predetermined value, the controller controls the first valve 431 to be opened so that the hydrogen vapor is introduced from the main pipe 411 into the cooling pipe group 412, and then from the cooling pipe group 412 into the first heating pipe 121.

[0069] After the raw material hydrogen is introduced into the cooling tube assembly 11, it is cooled and heated in the hydrogen liquefaction heat exchanger 10 and then converted by the positive and negative hydrogen conversion unit 20. The converted raw material hydrogen is processed by the processing unit 30 to obtain liquid hydrogen and hydrogen gas. The hydrogen gas is introduced into the first heating pipe 121 to mix with the hydrogen vapor introduced into the first heating pipe 121, and together they serve as the cold source for the heat exchange operation in the hydrogen liquefaction heat exchanger 10.

[0070] Preferably, the operating method of the liquid hydrogen tanker evaporation gas cooling energy recovery equipment includes the following steps:

[0071] When the temperature sensor 42 detects that the temperature of the hydrogen vapor in the main pipe 411 is the first recovery temperature, the controller controls the first valve 431 installed on the first cooling pipe 4121 to be opened, so that the hydrogen vapor flowing through the main pipe 411 is introduced into the first heating pipe 121 through the first cooling pipe 4121; when the temperature sensor 42 detects that the temperature of the hydrogen vapor in the main pipe 411 is the second recovery temperature, the controller controls the first valve 431 installed on the second cooling pipe 4122 to be opened, so that the hydrogen vapor flowing through the main pipe 411 is introduced into the first heating pipe 121 through the second cooling pipe 4122.

[0072] Preferably, the operating method of the liquid hydrogen tanker evaporation gas cooling energy recovery equipment includes the following steps:

[0073] The converted raw material hydrogen is introduced into the first feed pipe 321 and then depressurized by the first pressure reducing valve 331 before entering the liquid hydrogen separator 311, so as to obtain liquid hydrogen and hydrogen gas by gas-liquid separation in the liquid hydrogen separator 311.

[0074] The hydrogen obtained by gas-liquid separation is introduced into the second heating pipe 122 through the third discharge pipe 325. The hydrogen flows through the second heating pipe 122 to exchange heat in the hydrogen liquefaction heat exchanger 10 and be heated, so as to serve as a cold source for the heat exchange operation in the hydrogen liquefaction heat exchanger 10.

[0075] The liquid hydrogen obtained from gas-liquid separation is introduced into the liquid hydrogen subcooler 312 to be cooled and then discharged through the first discharge pipe 322. The liquid hydrogen flowing through the first discharge pipe 322 is introduced into the second feed pipe 323 and then depressurized by the second pressure reducing valve 332 before entering the liquid hydrogen separator 311. The depressurized liquid hydrogen serves as a cold source to exchange heat and raise the temperature in the liquid hydrogen subcooler 312 to obtain hydrogen gas. The hydrogen gas is introduced into the first heating pipe 121 through the second discharge pipe 324 to serve as a cold source for heat exchange operation in the hydrogen liquefaction heat exchanger 10.

[0076] Preferably, the operating method of the liquid hydrogen tanker evaporation gas cooling energy recovery equipment includes the following steps:

[0077] Circulating hydrogen is introduced into the first cooling pipe 131 to exchange heat and cool down in the hydrogen liquefaction heat exchanger 10, and then introduced into the third feed pipe 326. After being depressurized by the third pressure reducing valve 333, a hydrogen mixture is obtained. The hydrogen mixture is introduced into the first feed pipe 321 and together with the hydrogen mixture depressurized by the first pressure reducing valve 331, it is introduced into the liquid hydrogen separator 311 to recover hydrogen molecules and improve the liquid hydrogen acquisition rate.

[0078] Circulating hydrogen is introduced into the second cooling pipe 132 to exchange heat and cool down in the hydrogen liquefaction heat exchanger 10, and then introduced into the make-up cooling pipe 327. After being expanded and cooled by the expander unit 34, it is introduced into the third discharge pipe 325. Subsequently, it is introduced into the second heating pipe 122 together with the hydrogen obtained from gas-liquid separation in the liquid hydrogen separator 311, and together they serve as the cold source for heat exchange operation in the hydrogen liquefaction heat exchanger 10.

[0079] Preferably, the operating method of the liquid hydrogen tanker evaporation gas cooling energy recovery equipment includes the following steps:

[0080] Hydrogen gas heated by flowing through the first heating pipe 121 is discharged from the first outlet pipe 621. Hydrogen gas heated by flowing through the second heating pipe 122 is discharged from the second outlet pipe 622. Hydrogen gas flowing through the first outlet pipe 621 and the second outlet pipe 622 is heated by heat exchange in the liquid nitrogen temperature zone heat exchanger 71 and then guided to the hydrogen booster unit 72 for compression to obtain circulating hydrogen gas. Circulating hydrogen gas flows through the second inlet pipe 612 and is cooled by heat exchange in the liquid nitrogen temperature zone heat exchanger 71. After low-temperature adsorption, it is then introduced into the cold absorption pipe group 13.

[0081] Preferably, the operating method of the liquid hydrogen tanker evaporation gas cooling energy recovery equipment includes the following steps:

[0082] When the temperature sensor 42 detects that the temperature of the hydrogen vapor in the main pipe 411 is the third recovery temperature, the controller controls the second valve 432 set in the first gas return pipe 4131 to be opened, so that the hydrogen vapor flowing through the main pipe 411 is introduced into the first outlet pipe 621 through the first gas return pipe 4131, and then introduced into the liquid nitrogen temperature zone heat exchanger 71 as a cold source.

[0083] When the temperature sensor 42 detects that the temperature of the hydrogen vapor in the main pipeline 411 is the fourth recovery temperature, the controller controls the second valve 432 located in the second gas return pipe 4132 to be opened, so that the hydrogen vapor flowing through the main pipeline 411 is introduced into the first outlet pipe 621 through the second gas return pipe 4132, and then introduced into the hydrogen booster unit 72 for pressurization.

[0084] Those skilled in the art should understand that the embodiments of this application described above and shown in the accompanying drawings are merely examples and do not limit the scope of this application. The advantages of this application have been fully and effectively implemented. The functional and structural principles of this application have been demonstrated and explained in the embodiments, and any variations or modifications can be made to the implementation of this application without departing from the stated principles.

Claims

1. A liquid hydrogen tanker evaporator gas cooling energy recovery device, characterized in that, The liquid hydrogen tanker evaporator gas cooling energy recovery equipment includes: A hydrogen liquefaction heat exchanger, the hydrogen liquefaction heat exchanger having a cooling tube group and a heating tube group, the heating tube group including a first heating pipe; The intermediate hydrogen conversion unit is connected to the cooling tube group. After the raw material hydrogen is introduced into the cooling tube group, it is cooled in the hydrogen liquefaction heat exchanger and then converted by the intermediate hydrogen conversion unit. The processing unit has a cooling pipe assembly connected to it to introduce the converted raw material hydrogen into it. The first heating pipe is connected to it. The converted raw material hydrogen is processed by the processing unit to obtain hydrogen, which is then introduced into the first heating pipe, heated in the hydrogen liquefaction heat exchanger, and then discharged. A staged recovery unit includes a staged recovery pipe assembly, a temperature sensor, and a valve assembly. The staged recovery pipe assembly includes a main pipe, a cooling pipe assembly, and a gas return pipe assembly. The main pipe is connected to a liquid hydrogen tanker. The valve assembly includes at least one first valve and at least one second valve. The first valve and the second valve are respectively installed on the cooling pipe assembly and the gas return pipe assembly. The temperature sensor is installed on the main pipe to detect the temperature of the hydrogen vapor flowing through the main pipe. The cooling pipe assembly and the gas return pipe assembly are connected to the portions of the main pipe located away from the temperature sensor from the liquid hydrogen tanker. One end of the cooling pipe assembly away from the main pipe is connected to a first heating pipe. The temperature sensor is communicatively connected to a controller. The first valve and the second valve are controllably connected to the controller. The cold pipe assembly includes a first cold pipe and a second cold pipe. Two first valves are provided, one on the first cold pipe and the other on the second cold pipe. One end of each of the first and second cold pipes is connected to the main pipeline, and the other ends of both are connected to the first heating pipeline. The position where the first cold pipe is connected to the first heating pipeline is between the position where the processing unit is connected to the first heating pipeline and the position where the second cold pipe is connected to the first heating pipeline. Temperatures below a predetermined value are defined as a first recovery temperature and a second recovery temperature, where the first recovery temperature is lower than the second recovery temperature. After the temperature sensor detects that the temperature of the hydrogen vapor in the main pipeline is the first recovery temperature or the second recovery temperature, the controller, based on feedback from the temperature sensor, controls the first valve on the first cold pipe or the first valve on the second cold pipe to be opened. The processing unit includes a processing group, a connecting pipe group, and a pressure-reducing valve group. The processing group includes a liquid hydrogen separator. The connecting pipe group includes a first feed pipe. The pressure-reducing valve group includes a first pressure-reducing valve. One end of the first feed pipe is connected to the cooling pipe group to be introduced with converted raw material hydrogen. The liquid hydrogen separator is connected to the other end of the first feed pipe. The first pressure-reducing valve is installed on the first feed pipe to reduce the pressure of the converted raw material hydrogen flowing to the liquid hydrogen separator to obtain a hydrogen mixture. The hydrogen mixture introduced into the liquid hydrogen separator through the first feed pipe undergoes gas-liquid separation in the liquid hydrogen separator to obtain liquid hydrogen and hydrogen gas. The processing group includes a liquid hydrogen subcooler. The liquid hydrogen separator is connected to the liquid hydrogen subcooler through a pipe to introduce liquid hydrogen into the liquid hydrogen subcooler. The liquid hydrogen is cooled in the liquid hydrogen subcooler. The connecting pipe group includes... The first discharge pipe is connected to the liquid hydrogen subcooler. Liquid hydrogen cooled by the liquid hydrogen subcooler is discharged from the first discharge pipe. The connecting pipe assembly also includes a second inlet pipe. The pressure reducing valve assembly includes a second pressure reducing valve. The two ends of the second inlet pipe are respectively connected to the first discharge pipe and the liquid hydrogen subcooler. The second pressure reducing valve is installed on the second inlet pipe. A portion of the liquid hydrogen flowing through the first discharge pipe is introduced into the second inlet pipe and, after being depressurized by the second pressure reducing valve, is introduced into the liquid hydrogen subcooler. The depressurized liquid hydrogen serves as a cold source to exchange heat and increase its temperature in the liquid hydrogen subcooler to obtain hydrogen gas. The connecting pipe assembly also includes a second discharge pipe. The two ends of the second discharge pipe are respectively connected to the liquid hydrogen subcooler and one end of the first heating pipe. Hydrogen gas in the liquid hydrogen subcooler is introduced into the first heating pipe from the second discharge pipe.

2. The liquid hydrogen tanker evaporation gas cooling energy recovery equipment according to claim 1, characterized in that, The pressure-reducing valve assembly also includes a fourth pressure-reducing valve, which is installed on the first discharge pipe. The second feed pipe is connected to the first discharge pipe at a position between the fourth pressure-reducing valve and the liquid hydrogen subcooler, which are each connected to the first discharge pipe. The liquid hydrogen tanker evaporation gas cooling energy recovery equipment also includes a storage unit. A portion of the liquid hydrogen flowing through the first discharge pipe is depressurized by the fourth pressure-reducing valve and then guided to the storage unit.

3. The liquid hydrogen tanker evaporator gas cooling energy recovery equipment according to claim 1, characterized in that, The connecting pipe assembly also includes a third discharge pipe, and the heating pipe assembly includes a second heating pipe. The two ends of the third discharge pipe are respectively connected to the liquid hydrogen separator and one end of the second heating pipe. The hydrogen obtained by gas-liquid separation in the liquid hydrogen separator is introduced into the second heating pipe through the third discharge pipe to exchange heat and be heated in the hydrogen liquefaction heat exchanger.

4. The liquid hydrogen tanker evaporator gas cooling energy recovery equipment according to claim 3, characterized in that, The hydrogen liquefaction heat exchanger also includes a cooling pipe assembly, which includes a first cooling pipe. The connecting pipe assembly also includes a third feed pipe, one end of which is connected to the first cooling pipe. Circulating hydrogen is introduced into the first cooling pipe to exchange heat and cool down in the hydrogen liquefaction heat exchanger before being introduced into the third feed pipe. The pressure reducing valve assembly also includes a third pressure reducing valve, which is installed on the third feed pipe. The end of the third feed pipe away from the first cooling pipe is connected to the portion of the first feed pipe located between the first pressure reducing valve and the liquid hydrogen separator. The circulating hydrogen introduced into the third feed pipe is depressurized by the third pressure reducing valve to obtain a hydrogen mixture. The hydrogen mixture depressurized by the third pressure reducing valve is introduced into the first feed pipe and introduced into the liquid hydrogen separator together with the hydrogen mixture depressurized by the first pressure reducing valve.

5. The liquid hydrogen tanker evaporator gas cooling energy recovery equipment according to claim 4, characterized in that, The cooling pipe assembly further includes a second cooling pipe, the processing unit further includes an expander unit, and the connecting pipe assembly further includes a make-up cooling pipe. The expander unit is installed on the make-up cooling pipe, and the two ends of the make-up cooling pipe are respectively connected to one end of the second cooling pipe and the third discharge pipe. Circulating hydrogen is introduced into the second cooling pipe to exchange heat and cool down in the hydrogen liquefaction heat exchanger, then introduced into the make-up cooling pipe and expanded and cooled by the expander unit before being introduced into the third discharge pipe, so that it is introduced into the second heating pipe together with the hydrogen obtained by gas-liquid separation in the liquid hydrogen separator. The cooling amount obtained by the circulating hydrogen flowing through the second cooling pipe in the hydrogen liquefaction heat exchanger is less than the cooling amount obtained by the circulating hydrogen flowing through the first cooling pipe in the hydrogen liquefaction heat exchanger.

6. The liquid hydrogen tanker evaporator gas cooling energy recovery equipment according to claim 5, characterized in that, The liquid hydrogen tanker evaporation gas cold energy recovery equipment includes a pipeline assembly, which includes an inlet pipe assembly and an outlet pipe assembly. The inlet pipe assembly includes a first inlet pipe and a second inlet pipe, and the outlet pipe assembly includes a first outlet pipe and a second outlet pipe. The first inlet pipe is connected to the cooling pipe assembly to introduce raw material hydrogen into the cooling pipe assembly. The second inlet pipe is connected to the cooling absorption pipe assembly to introduce circulating hydrogen into the cooling absorption pipe assembly. The first outlet pipe is connected to the end of the first heating pipe away from the second discharge pipe, and is used to discharge the hydrogen that has been heated by flowing through the first heating pipe. The second outlet pipe is connected to the end of the second heating pipe away from the third discharge pipe, and is used to discharge the hydrogen that has been heated by flowing through the second heating pipe. The liquid hydrogen tanker evaporation gas cold energy recovery equipment includes a temperature control mechanism. The system includes a liquid nitrogen temperature zone heat exchanger, a hydrogen booster unit, and a nitrogen cooling unit. The liquid nitrogen temperature zone heat exchanger is installed on the first inlet pipe, the second inlet pipe, the first outlet pipe, and the second outlet pipe. The nitrogen cooling unit is connected to the liquid nitrogen temperature zone heat exchanger to supply cooling to it. The ends of the first outlet pipe and the second outlet pipe, away from the hydrogen liquefaction heat exchanger, are connected to the hydrogen booster unit. Hydrogen flowing through the first outlet pipe and the second outlet pipe is heated by heat exchange in the liquid nitrogen temperature zone heat exchanger and then guided to the hydrogen booster unit for compression to obtain circulating hydrogen. The end of the second inlet pipe, away from the hydrogen liquefaction heat exchanger, is connected to the hydrogen booster unit to introduce circulating hydrogen. The circulating hydrogen flowing through the second inlet pipe is cooled by heat exchange in the liquid nitrogen temperature zone heat exchanger and then introduced into the cold absorption pipe assembly after a low-temperature adsorption operation.

7. The liquid hydrogen tanker evaporator gas cooling energy recovery equipment according to claim 6, characterized in that, The gas return pipe assembly includes a first gas return pipe and a second gas return pipe. Two second valves are provided, one on each of the first and second gas return pipes. One end of the first gas return pipe and one end of the second gas return pipe are connected to the main pipeline. The other end of the first gas return pipe is connected to the portion of the first outlet pipe located between the hydrogen liquefaction heat exchanger and the liquid nitrogen temperature zone heat exchanger. The other end of the second gas return pipe is connected to the portion of the first outlet pipe located between the liquid nitrogen temperature zone heat exchanger and the hydrogen booster unit. The temperature control mechanism also includes an ambient air vaporizer, which is installed on the second gas return pipe to vaporize the liquid portion of the hydrogen vaporized gas flowing through the second gas return pipe. Temperatures higher than a predetermined value are defined as a third recovery temperature and a fourth recovery temperature, wherein the third recovery temperature is lower than the fourth recovery temperature. After the temperature sensor detects that the temperature of the hydrogen vaporized gas in the main pipeline is the third recovery temperature or the fourth recovery temperature, the controller controls the second valve located on the first gas return pipe or the second valve located on the second gas return pipe to open based on the feedback from the temperature sensor.

8. The operating method of the liquid hydrogen tanker evaporator gas cooling energy recovery device according to any one of claims 1 to 7, characterized in that, The operating method of the liquid hydrogen tanker evaporative gas cooling energy recovery equipment includes the following steps: The temperature sensor detects the temperature of the hydrogen vapor in the main pipeline, and when the temperature is detected to be lower than a predetermined value, the controller controls the first valve to be opened so that the hydrogen vapor is introduced from the main pipeline into the cooling pipe group, and then from the cooling pipe group into the first heating pipeline. After the raw material hydrogen is introduced into the cooling tube assembly, it is cooled and heated in the hydrogen liquefaction heat exchanger and then converted by the positive and negative hydrogen conversion unit. The converted raw material hydrogen is processed by the processing unit to obtain liquid hydrogen and hydrogen gas. The hydrogen gas is introduced into the first heating pipe to mix with the hydrogen vapor introduced into the first heating pipe, and together they serve as the cold source for the heat exchange operation in the hydrogen liquefaction heat exchanger.

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