EQUIPMENT FOR MANUFACTURING LIQUID HYDROGEN

Abstract

An equipment for manufacturing liquid hydrogen according to the present disclosure, which is configured to perform the first isothermal process, the first isobaric process, the isenthalpic process, the second isothermal process, and the second isobaric process in the diagram of temperature T and enthalphy S for liquefying gaseous hydrogen, comprises: a compressor located on a hydrogen flow path to perform the first isothermal process; a precooler and a heat exchanger which are connected to the compressor, on the hydrogen flow path, in this order to perform the first isobaric process; a Joule-Thomson valve connected to the heat exchanger, on the hydrogen flow path, to perform the isenthalpic process; a first cryocooler and second cryocoolers connected to the Joule-Thomson valve sequentially, on the hydrogen flow path, to perform the third isobaric process between the isenthalpic process and the second isothermal process; and a storage tank which is connected to the first cryocooler and the second cryocoolers to perform the second isothermal process on the hydrogen flow path.

Claims

1. An equipment for manufacturing liquid hydrogen, which is configured to perform the first isothermal process, the first isobaric process, the isenthalpic process, the second isothermal process, and the second isobaric process in the diagram of temperature T and enthalphy S for liquefying gaseous hydrogen, comprising: a compressor located on a hydrogen flow path to perform the first isothermal process; a precooler and a heat exchanger which are connected to the compressor, on the hydrogen flow path, sequentially to perform the first isobaric process; a Joule-Thomson valve connected to the heat exchanger, on the hydrogen flow path, to perform the isenthalpic process; a first cryocooler and second cryocoolers connected to the Joule-Thomson valve, on the hydrogen flow path sequentially, to perform the third isobaric process between the isenthalpic process and the second isothermal process; and a storage tank which is connected to the first cryocooler and the second cryocoolers to perform the second isothermal process on the hydrogen flow path, wherein the third isobaric process connects the isenthalpic process and the second isothermal process therebetween in the diagram of temperature T and enthalphy S.

2. The equipment for manufacturing liquid hydrogen according to claim 1, wherein the compressor mixes and compresses internal gaseous hydrogen and external gaseous hydrogen to produce circulating gaseous hydrogen while maintaining the highest temperature in the diagram when the first isothermal process is performed, wherein the internal gaseous hydrogen which is supplied from the precooler has absolute temperature of 300K and pressure range of 2 bar to 4 bar, and wherein the external gaseous hydrogen which is supplied to the compressor from the outside has absolute temperature of 300K and pressure of 60 bar.

3. The equipment for manufacturing liquid hydrogen according to claim 2, wherein the circulating gaseous hydrogen has absolute temperature of 300K and pressure range of 40 bar to 80 bar at the output end of the compressor.

4. The equipment for manufacturing liquid hydrogen according to claim 1, wherein the precooler and the heat exchanger gradually lower the temperature of the circulating gaseous hydrogen from the compressor in this order to produce the 1.sup.st and the 2.sup.nd low-temperature gaseous hydrogens when the first isobaric process is performed.

5. The equipment for manufacturing liquid hydrogen according to claim 4, wherein the precooler operates at the initial stage of the first isobaric process to receive the circulating gaseous hydrogen from the compressor and let the circulating gaseous hydrogen and liquefied natural gas be heat-exchanged to produce the 1.sup.st low-temperature gaseous hydrogen from the circulating gaseous hydrogen.

6. The equipment for manufacturing liquid hydrogen according to claim 5, wherein the 1.sup.st low-temperature gaseous hydrogen has absolute temperature range of 77K to 80K and pressure range of 40 bar to 80 bar at the output end of the precooler.

7. The equipment for manufacturing liquid hydrogen according to claim 4, wherein the heat exchanger operates at the final stage of the first isobaric process to receive the 1.sup.st low-temperature gaseous hydrogen from the precooler and cools the 1.sup.st low-temperature gaseous hydrogen to produce the 2.sup.nd low-temperature gaseous hydrogen.

8. The equipment for manufacturing liquid hydrogen according to claim 7, wherein the 2.sup.nd low-temperature gaseous hydrogen has absolute temperature range of 60K to 76K and pressure range of 40 bar to 80 bar at the output end of the heat exchanger.

9. The equipment for manufacturing liquid hydrogen according to claim 1, wherein the Joule-Thomson valve, when performing the isenthalpic process, receives the 2.sup.nd low-temperature gaseous hydrogen from the heat exchanger, expands the volume of the 2.sup.nd low-temperature gaseous hydrogen, and cools the 2.sup.nd low-temperature gaseous hydrogen to produce the 3.sup.rd low-temperature gaseous hydrogen, wherein the 3.sup.rd low-temperature gaseous hydrogen is maintained below the maximum inversion temperature at which gaseous state of the 3.sup.rd low-temperature gaseous hydrogen is converted into liquid state.

10. The equipment for manufacturing liquid hydrogen according to claim 9, wherein the 3.sup.rd low-temperature gaseous hydrogen has absolute temperature range of 40K to 60K and pressure range of 2 bar to 4 bar at the output end of the Joule-Thomson valve.

11. The equipment for manufacturing liquid hydrogen according to claim 1, wherein the first cryocooler, when performing the third isobaric process, receives the 3.sup.rd low-temperature gaseous hydrogen from the Joule-Thomson valve, cools the 3.sup.rd low-temperature gaseous hydrogen to produce gaseous hydrogen for storing and liquid hydrogen for storing, and supplies them to the storage tank, and wherein the gaseous hydrogen for storing can be made to have a bigger mass ratio than that of the liquid hydrogen for storing from the 3.sup.rd low-temperature gaseous hydrogen coming from the Joule-Thomson valve.

12. The equipment for manufacturing liquid hydrogen according to claim 11, wherein the gaseous hydrogen for storing and the liquid hydrogen for storing have absolute temperature range of 20K to 30K and pressure range of 2 bar to 4 bar at the output end of the first cryocooler.

13. The equipment for manufacturing liquid hydrogen according to claim 1, wherein the second cryocoolers are connected to the first cryocooler via the storage tank on the hydrogen flow path, receives the gaseous hydrogen for storing from the storage tank, when performing the third isobaric process, cools the gaseous hydrogen for storing to produce the 1st low-temperature gaseous hydrogen for storing, and supplies the 1.sup.st low-temperature gaseous hydrogen for storing to the storage tank.

14. The equipment for manufacturing liquid hydrogen according to claim 13, wherein the 1.sup.st low-temperature gaseous hydrogen for storing has absolute temperature range of 10K to 20K and pressure range of 2 bar to 4 bar at the output terminals of the second cryocoolers to keep the temperature of the internal atmosphere inside the storage tank constant and is partially liquefied with a portion of the gaseous hydrogen for storing in the storage tank.

15. The equipment for manufacturing liquid hydrogen according to claim 1, wherein the second isothermal process is performed such that the storage tank receives and stores the gaseous hydrogen for storing and the liquid hydrogen for storing from the first cryocooler, that the gaseous hydrogen for storing contacts with the 1.sup.st low-temperature gaseous hydrogen for storing from the second cryocoolers inside the storage tank to produce a 2.sup.nd low-temperature gaseous hydrogen for storing on the hydrogen flow path, and that the 1.sup.st low-temperature gaseous hydrogen for storing and the 2.sup.nd low-temperature gaseous hydrogen for storing are mixed up to produce low-temperature gaseous hydrogen for storing at the lowest temperature on the diagram during the flow of the low-temperature gaseous hydrogen for storing from the inside the storage tank toward the outside the storage tank.

16. The equipment for manufacturing liquid hydrogen according to claim 1, wherein the second isobaric process is performed such that, when viewed along the hydrogen flow path, the temperature of the low-temperature gaseous hydrogen for storing from the storage tank is gradually increased by heating the low-temperature gaseous hydrogen for storing with the heat exchanger and the precooler in this order to produce gaseous hydrogen for raising the temperature and the internal gaseous hydrogen.

17. The equipment for manufacturing liquid hydrogen according to claim 16, wherein the gaseous hydrogen for raising the temperature is formed by heating the low-temperature gaseous hydrogen for storing with the heat exchanger and has absolute temperature range of 140K to 150K and pressure range of 2 bar to 4 bar at the output end of the heat exchanger.

18. The equipment for manufacturing liquid hydrogen according to claim 16, wherein the internal gaseous hydrogen is formed by heating the gaseous hydrogen for raising the temperature with the liquefied natural gas at the precooler and has absolute temperature of 300K and pressure range of 2 bar to 4 bar at the output end of the precooler.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0033] The above and other aspects, features, and advantages of certain preferable embodiments of the present disclosure will be more apparent from the following description taken in conjunction with the accompanying drawings, in which:

[0034] FIG. 1 is a schematic layout diagram showing the internal structure of an equipment for manufacturing liquid hydrogen according to the present disclosure.

[0035] FIG. 2 is a block diagram schematically showing an operating order of the equipment for manufacturing liquid hydrogen of FIG. 1.

[0036] FIG. 3 is the temperature T and enthalpy S diagram showing the precoolable Linde-Thomson cycle on a hydrogen flow path in the equipment for manufacturing liquid hydrogen of FIG. 1.

DETAILED DESCRIPTION

[0037] Referring FIGS. 1 to 3, the equipment for manufacturing liquid hydrogen 100 according to the present disclosure is configured to perform the first isothermal process, the first isobaric process, the isenthalpic process, the second isothermal process, and the second isobaric process in the temperature T and enthalphy S diagram of FIG. 3 to liquefy gaseous hydrogen.

[0038] In a schematic view, the hydrogen liquefaction apparatus 100, as shown in FIG. 1 or FIG. 2, comprises a compressor 10, a precooler 30, a heat exchanger 40, a Joule-Thomson valve 50, a first cryocooler 60, a storage tank 70, and second cryocoolers 80, 90 on a hydrogen flow path.

[0039] The compressor 10 is located on the hydrogen flow path to perform the first isothermal process (a-b in FIG. 1 or FIG. 3). The precooler 30 and the heat exchanger 40 are connected to the compressor 10 on the hydrogen flow path in this order to perform the first isobaric process (b-c and c-d in FIG. 1 or FIG. 3; hereinafter referred to as b-d).

[0040] The Joule-Thomson valve 50 is connected to the heat exchanger 40 on the hydrogen flow path to perform the isenthalpic process (d-e in FIG. 1 or FIG. 3). A first cryocooler 60 and second cryocoolers 80, 90 are connected to the Joule-Thomson valve 50, on the hydrogen flow path in this order, to perform the third isobaric process (e-f and f-h in FIG. 1 or FIG. 3; hereinafter referred to as e-h) between the isenthalpic process (d-e) and the second isothermal process (h-g3 in FIG. 1 or FIG. 3).

[0041] The storage tank 70 is connected to the first cryocooler 60 and the second cryocoolers 80, 90 to perform the second isothermal process (h-g3), on the hydrogen flow path. Here, the third isobaric process (e-h) connects the isenthalpic process (d-e) and the second isothermal process (h-g3) therebetween in the diagram of FIG. 3.

[0042] In more detail, referring FIGS. 1 to 3, the compressor 10 mixes and compresses the internal gaseous hydrogen (not shown in the drawings) and external gaseous hydrogen (g1 in FIG. 1) to produce circulating gaseous hydrogen (not shown in the drawings) while maintaining the highest temperature in the diagram when the first isothermal process (a-b) is performed.

[0043] The internal gaseous hydrogen having absolute temperature of 300K and pressure range of 2 bar to 4 bar is supplied from the precooler 30. The external gaseous hydrogen g1 having absolute temperature of 300K and pressure of 60 bar is periodically supplied to the compressor 10 from the outside. The circulating gaseous hydrogen has absolute temperature of 300K and pressure range of 40 bar to 80 bar at the output end of the compressor 10.

[0044] Referring FIGS. 1 to 3, the precooler 30 and the heat exchanger 40, in this order, gradually lower the temperature of the circulating gaseous hydrogen from the compressor 10 to produce the 1.sup.st and the 2.sup.nd low-temperature gaseous hydrogens (not shown in the drawings) when the first isobaric process (b-d) is performed.

[0045] Here, referring FIGS. 1 to 3, the precooler 30 operates at the initial stage (b-c) of the first isobaric process (b-d) to receive the circulating gaseous hydrogen from the compressor 10 and let the circulating gaseous hydrogen and the liquefied natural gas (20 in FIG. 1) be heat-exchanged to produce the 1.sup.st low-temperature gaseous hydrogen from the circulating gaseous hydrogen. The liquefied natural gas 20 may obtain heat from the circulating gaseous hydrogen.

[0046] The 1.sup.st low-temperature gaseous hydrogen has absolute temperature range of 77K to 80K and pressure range of 40 bar to 80 bar at the output end of the precooler 30. Referring FIG. 1 to FIG. 3, the heat exchanger 40 operates at the final stage (c-d) of the first isobaric process (b-d) to receive the 1.sup.st low-temperature gaseous hydrogen from the pre-cooler 30 and cools the 1.sup.st low-temperature gaseous hydrogen to produce the 2.sup.nd low-temperature gaseous hydrogen.

[0047] The 2.sup.nd low-temperature gaseous hydrogen has absolute temperature range of 60K to 76K and pressure range of 40 bar to 80 bar at the output end of the heat exchanger 40. The Joule-Thomson valve 50, referring FIG. 1 to FIG. 3, operates at the isenthalpic process (d-e) to receive the 2.sup.nd low-temperature gaseous hydrogen from the heat exchanger 40, expands the volume of the 2.sup.nd low-temperature gaseous hydrogen and cools the 2.sup.nd low-temperature gaseous hydrogen to produce the 3.sup.rd low-temperature gaseous hydrogen (not shown in the drawings).

[0048] The 3.sup.rd low-temperature gaseous hydrogen is maintained below the maximum inversion temperature at which gaseous state of the 3.sup.rd low-temperature gaseous hydrogen is converted into liquid state. The 3.sup.rd low-temperature gaseous hydrogen has absolute temperature range of 40K to 60K and pressure range of 2 bar to 4 bar at the output end of the Joule-Thomson valve 50.

[0049] Referring FIG. 1 to FIG. 3, the first cryocooler 60, when performing the initial stage (e-f) of the third isobaric process (e-h), receives the 3.sup.rd low-temperature gaseous hydrogen from the Joule-Thomson valve (50), cools the 3.sup.rd low-temperature gaseous hydrogen to produce gaseous hydrogen for storing (g2 in FIG. 1) and liquid hydrogen for storing (LH2 in FIG. 1), and supplies them to the storage tank 70. The gaseous hydrogen for storing (g2) can be made to have a bigger mass ratio than that of the liquid hydrogen for storing (LH2) from the 3.sup.rd low-temperature gaseous hydrogen coming from the Joule-Thomson valve 50.

[0050] The gaseous hydrogen for storing g2 and the liquid hydrogen for storing LH2 have absolute temperature range of 20K to 30K and pressure range of 2 bar to 4 bar at the output end of the first cryocooler 60. Referring FIG. 1 to FIG. 3, the second cryocoolers 80 and 90 are connected to the first cryocooler 60 via the storage tank 70, when performing the final stage (f-h) of the third isobaric process (e-h), receive the gaseous hydrogen for storing g2 from the storage tank 70, cool the gaseous hydrogen for storing g2 to produce a 1.sup.st low-temperature gaseous hydrogen for storing (not shown in the drawing), and supply the 1.sup.st low-temperature gaseous hydrogen for storing to the storage tank 70.

[0051] The 1.sup.st low-temperature gaseous hydrogen for storing has absolute temperature range of 10K to 20K and pressure range of 2 bar to 4 bar at the output terminals of the second cryocoolers 80 and 90 to keep the temperature of the internal atmosphere inside the storage tank 70 constant and is partially liquefied with a portion of the gaseous hydrogen for storing g2 in the storage tank.

[0052] Referring FIG. 1 to FIG. 3, the second isothermal process (h-g3) is performed such that the storage tank 70 receives and stores the gaseous hydrogen for storing g2 and the liquid hydrogen for storing LH2 from the first cryocooler 60, that the gaseous hydrogen for storing g2 contacts with the 1.sup.st low-temperature gaseous hydrogen for storing from the second cryocoolers 80, 90 inside the storage tank 70 to produce a 2.sup.nd low-temperature gaseous hydrogen for storing on the hydrogen flow path, and that the 1.sup.st low-temperature gaseous hydrogen for storing and the 2.sup.nd low-temperature gaseous hydrogen for storing are mixed up to produce low-temperature gaseous hydrogen for storing g3.

[0053] Referring the diagram, the second isothermal process (h-g3) is performed at the lowest temperature along the hydrogen flow path during the flow of the low-temperature gaseous hydrogen for storing g3 from the inside toward the outside the storage tank 70.

[0054] Referring FIG. 1 to FIG. 3, the second isobaric process (g3-i and i-a) is performed such that, when viewed along the hydrogen flow path, the temperature of the low-temperature gaseous hydrogen for storing g3 from the storage tank 70 is gradually increased by heating the low-temperature gaseous hydrogen for storing g3 with the heat exchanger 40 and the precooler 30 in this order to produce gaseous hydrogen for raising the temperature (not shown in the drawings) and the internal gaseous hydrogen (not shown in the drawings).

[0055] The gaseous hydrogen for raising the temperature is formed by heating the low-temperature gaseous hydrogen for storing g3 with the heat exchanger 40 and has absolute temperature range of 140K to 150K and pressure range of 2 bar to 4 bar at the output end of the heat exchanger 40. The internal gaseous hydrogen is formed by heating the gaseous hydrogen for raising the temperature with the liquefied natural gas 20 at the precooler 30 and has absolute temperature of 300K and pressure range of 2 bar to 4 bar at the output end of the precooler 30.