Helium refrigeration hydrogen liquefaction system and method
By designing a four-stage pre-cooling compression and mixed refrigerant, the problems of high equipment load and high energy consumption in the traditional helium-cooled hydrogen liquefaction process are solved, achieving a reduction in equipment cost and energy consumption as well as an improvement in liquefaction effect.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Patents(China)
- Current Assignee / Owner
- 江苏富瑞能源服务有限公司
- Filing Date
- 2023-12-29
- Publication Date
- 2026-07-31
AI Technical Summary
Traditional helium-cooled hydrogen liquefaction processes suffer from high equipment load, high energy consumption, and high costs, and have not been widely adopted by large commercial hydrogen production companies.
It adopts a four-stage pre-cooling compression assembly and a helium refrigerant distributor structure in the liquefaction section. It combines a mixed refrigerant of methane, ethane, propane, n-butane, isobutane, and nitrogen with a molar ratio of helium, hydrogen, and neon. By rationally controlling the pressure ratio of the compression stage, it utilizes the expansion cooling of the helium refrigerant to provide sufficient cooling capacity.
It effectively reduced the compressor shaft power to 250KW, reduced equipment costs and energy consumption, improved liquefaction efficiency, and reduced refrigerant costs.
Smart Images
Figure CN117628835B_ABST
Abstract
Description
Technical Field
[0001] This invention relates to the field of hydrogen liquefaction technology. Background Technology
[0002] Traditional helium-cooled hydrogen liquefaction processes use nitrogen pre-cooling, and then the pre-cooled hydrogen is heated by even colder helium. This process is safe, but has high energy consumption and a large equipment load.
[0003] Nitrogen is readily available and pollution-free, but liquid nitrogen has a low latent heat of vaporization. When relying solely on liquid nitrogen to meet cooling requirements, the compressor load will be too high, which also limits the supply of liquid nitrogen for low-temperature cooling needs.
[0004] Currently, helium-cooled hydrogen liquefaction processes are complex and costly, thus limiting their adoption by large commercial hydrogen production companies. To reduce compressor load and further lower hydrogen liquefaction costs, improvements have been made to the helium-cooled hydrogen liquefaction process. Summary of the Invention
[0005] The technical problem to be solved by the present invention is to provide a helium-cooled hydrogen liquefaction system and method, which can effectively reduce equipment load, save energy consumption, and improve liquefaction effect.
[0006] To solve the above problems, the technical solution adopted by the present invention is: a helium-cooled hydrogen liquefaction system, comprising: a precooling section and a liquefaction section. The precooling section includes: a precooling heat exchanger, a first-stage precooling compression assembly, a second-stage precooling compression assembly, a third-stage precooling compression assembly, and a fourth-stage precooling compression assembly. Each stage of the precooling compression assembly includes a compressor and a cooler. The precooling heat exchanger is provided with a precooling hydrogen channel, a precooling refrigerant channel, and a precooling refrigerant return channel. The inlet of the precooling hydrogen channel is connected to a hydrogen input pipe, and the outlet of the precooling hydrogen channel is provided with a precooling hydrogen output pipe. A precooling hydrogen throttling valve is installed on the precooling hydrogen output pipe. The outlet of the precooling refrigerant channel, the first-stage precooling compression assembly, the second-stage precooling compression assembly, the third-stage precooling compression assembly, and the fourth-stage precooling compression assembly are connected in sequence. The cooler outlet of the fourth-stage precooling compression assembly is connected to the inlet of the precooling refrigerant return channel. The outlet of the precooling refrigerant return channel is equipped with a precooling refrigerant throttle valve, and the outlet of the precooling refrigerant return channel is connected to the inlet of the precooling refrigerant channel through the precooling refrigerant throttle valve. The liquefaction section includes: a first heat exchanger, a second heat exchanger, a third heat exchanger, and a fourth heat exchanger. Each heat exchanger is equipped with a liquefaction section hydrogen channel. The liquefaction section hydrogen channels in the first, second, third, and fourth heat exchangers are connected sequentially. The outlet of the liquefaction section hydrogen channel in the fourth heat exchanger is connected to a liquid hydrogen delivery pipe, which is connected to a liquid hydrogen storage tank. A liquid hydrogen throttling valve is installed on the liquid hydrogen delivery pipe between the fourth heat exchanger and the liquid hydrogen storage tank. The output end of the pre-cooled hydrogen output pipe is connected to the inlet of the liquefaction section hydrogen channel in the first heat exchanger. The first heat exchanger is also provided with a first helium expansion side channel and a first helium refrigeration channel; the second heat exchanger is also provided with a second helium expansion side channel and a second helium refrigeration channel; the third heat exchanger is also provided with a third helium refrigeration channel; and the fourth heat exchanger is also provided with a fourth helium refrigeration channel. The outlet of the first helium expansion side channel in the first heat exchanger is equipped with a first distributor, which has a first distribution outlet pipe and a second distribution outlet pipe. The first distribution outlet pipe is connected to the inlet of the second helium expansion side channel in the second heat exchanger. The outlet of the second helium expansion side channel is connected to the inlet of the first expander. The outlet of the first expander is connected to the inlet of the fourth helium refrigeration channel in the fourth heat exchanger. The second distribution output pipe is connected to the inlet of the second expander. The outlet of the second expander and the outlet of the fourth helium refrigeration channel are both connected to the input end of the second distributor. The output end of the second distributor is connected to the inlet of the third helium refrigeration channel in the third heat exchanger. The third helium refrigeration channel, the second helium refrigeration channel, and the first helium refrigeration channel are connected in sequence. The outlet of the first helium refrigeration channel in the first heat exchanger is connected to the input end of the liquefaction section compression assembly, and the output end of the liquefaction section compression assembly is connected to the inlet of the first helium expansion side channel in the first heat exchanger.
[0007] Furthermore, in the aforementioned helium-cooled hydrogen liquefaction system, the helium compression assembly in the liquefaction section includes: a first-stage compressor, a first-stage cooler, a second-stage compressor, a second-stage cooler, a third-stage compressor, and a third-stage cooler connected in sequence; the output end of the third-stage cooler is connected to the inlet of the first helium expansion side channel in the first heat exchanger.
[0008] Furthermore, in the aforementioned helium-cooled hydrogen liquefaction system, the upper end of the liquid hydrogen storage tank is connected to a gaseous hydrogen output pipe, and the lower end of the liquid hydrogen storage tank is connected to a liquid hydrogen output pipe.
[0009] A helium-cooled hydrogen liquefaction method includes using the aforementioned helium-cooled hydrogen liquefaction system. In the precooling section, the precooling refrigerant used in the precooling heat exchanger, primary precooling compression assembly, secondary precooling compression assembly, tertiary precooling compression assembly, and quaternary precooling compression assembly is a mixed refrigerant containing methane, ethane, propane, n-butane, isobutane, and nitrogen, with a molar ratio of 0.2102:0.2970:0.2737:0.003:0.00013:0.2148. In the liquefaction section, the helium refrigerant is mixed with hydrogen and neon, with a molar ratio of helium, hydrogen, and neon of 86:13:1.
[0010] Furthermore, in the aforementioned helium-cooled hydrogen liquefaction method, the hydrogen liquefaction step includes: the volume ratio of helium refrigerant in the first distribution outlet pipe and the second distribution outlet pipe is 20%:80%.
[0011] The advantages of this invention are: a helium-cooled hydrogen liquefaction system and method, wherein the precooling section of the helium-cooled hydrogen liquefaction system adopts four-stage compression, thereby effectively reducing the compressor shaft power to 250KW by reasonably controlling the pressure ratio of the compression stages. This not only effectively reduces equipment costs but also effectively reduces hydrogen liquefaction energy consumption. In the liquefaction section, the helium refrigerant is divided into two streams by a first distributor. One stream, accounting for 20% of the volume, enters the first expansion stage through a second heat exchanger for expansion and cooling before entering the fourth heat exchanger for final liquid hydrogen cooling. The other stream, accounting for 80% of the volume, expands and cools through a second expander, mixes with the 20% stream output from the fourth heat exchanger, and then enters the third heat exchanger to provide cooling. This structure facilitates the expansion and cooling of the helium refrigerant, thereby providing sufficient cooling for hydrogen liquefaction. During hydrogen liquefaction, the pre-cooling section 100 uses a mixed refrigerant with a molar ratio of methane, ethane, propane, n-butane, isobutane, and nitrogen of 0.2102:0.2970:0.2737:0.003:0.00013:0.2148. Adding methane and ethane increases the refrigerant's vaporization rate, and methane has a significantly higher latent heat of vaporization than nitrogen. The addition of propane effectively increases the refrigerant's liquefaction rate. Isobutane and n-butane have large molecular weights, meaning they have high specific heat and heat of vaporization, and low adiabatic indices, thus effectively increasing the circulation volume and reducing the compressor load. In other words, the mixed refrigerant with the above molar ratio provides a more ideal cooling effect. In the liquefaction section, the helium refrigerant is a mixed refrigerant consisting of helium, hydrogen, and neon in a molar ratio of 86:13:1. Its advantages are that hydrogen is readily available, which can effectively reduce the cost of refrigerant, and the high latent heat of vaporization of neon can greatly improve the refrigeration effect. Attached Figure Description
[0012] Figure 1 This is a schematic diagram illustrating the working principle of a helium-cooled hydrogen liquefaction system according to the present invention. Detailed Implementation
[0013] The present invention will now be described in further detail with reference to the accompanying drawings and preferred embodiments.
[0014] A helium-cooled hydrogen liquefaction system includes a precooling section 100 and a liquefaction section 200. The precooling section 100 includes a precooling heat exchanger 1, a primary precooling compression assembly, a secondary precooling compression assembly, a tertiary precooling compression assembly, and a quaternary precooling compression assembly. Each stage of the precooling compression assembly includes a compressor and a cooler. The precooling heat exchanger 1 is provided with a precooling hydrogen channel 101, a precooling refrigerant channel 102, and a precooling refrigerant return channel 103. The inlet of the precooling hydrogen channel 101 is connected to a hydrogen input pipe 1011, and the outlet of the precooling hydrogen channel 101 is provided with a precooling hydrogen output pipe 11. A precooling hydrogen throttling valve 12 is installed on the precooling hydrogen output pipe 11. The outlet of the precooling refrigerant channel 102, the first-stage precooling compression assembly, the second-stage precooling compression assembly, the third-stage precooling compression assembly, and the fourth-stage precooling compression assembly are connected in sequence. The cooler outlet in the fourth-stage precooling compression assembly is connected to the inlet of the precooling refrigerant return channel 103. A precooling refrigerant throttle valve 13 is installed at the outlet end of the precooling refrigerant return channel 103. The outlet end of the precooling refrigerant return channel 103 is connected to the inlet of the precooling refrigerant channel 102 through the precooling refrigerant throttle valve 13.
[0015] Specifically, the first-stage precooling compression assembly includes a first-stage compressor 21 and a first-stage cooler 22; the second-stage precooling compression assembly includes a second-stage compressor 23 and a second-stage cooler 24; the third-stage precooling compression assembly includes a third-stage compressor 25 and a third-stage cooler 26; and the fourth-stage precooling compression assembly includes a fourth-stage compressor 27 and a fourth-stage cooler 28. The first-stage compressor 21, first-stage cooler 22, second-stage compressor 23, second-stage cooler 24, third-stage compressor 25, third-stage cooler 26, fourth-stage compressor 27, and fourth-stage cooler 28 are connected sequentially. The outlet of the precooling refrigerant passage 102 is connected to the first-stage compressor 21, and the outlet of the fourth-stage cooler 28 is connected to the inlet of the precooling refrigerant return passage 103.
[0016] The liquefaction section 200 includes a first heat exchanger 3, a second heat exchanger 4, a third heat exchanger 5, and a fourth heat exchanger 6. Each heat exchanger is equipped with a liquefaction section hydrogen channel. The output end of the pre-cooled hydrogen output pipe 11 is connected to the liquefaction section hydrogen channel in the first heat exchanger 3. The liquefaction section hydrogen channels in the first heat exchanger 3, second heat exchanger 4, third heat exchanger 5, and fourth heat exchanger 6 are sequentially connected. Specifically, the first heat exchanger 3 is equipped with a first liquefaction section hydrogen channel 31, the second heat exchanger 4 is equipped with a second liquefaction section hydrogen channel 41, the third heat exchanger 5 is equipped with a third liquefaction section hydrogen channel 51, and the fourth heat exchanger 6 is equipped with a fourth liquefaction section hydrogen channel 61. The first liquefaction section hydrogen channel 31, the second liquefaction section hydrogen channel 41, the third liquefaction section hydrogen channel 51, and the fourth liquefaction section hydrogen channel 61 are sequentially connected. The output end of the pre-cooled hydrogen output pipe 11 is connected to the inlet of the first liquefaction section hydrogen channel 31.
[0017] The outlet of the hydrogen channel 61 in the fourth liquefaction section of the fourth heat exchanger 6 is connected to the liquid hydrogen delivery pipe 7, which is connected to the liquid hydrogen storage tank 8. A liquid hydrogen throttling valve 71 is installed on the liquid hydrogen delivery pipe 7 between the fourth heat exchanger 6 and the liquid hydrogen storage tank 8. In this example, the upper end of the liquid hydrogen storage tank 8 is connected to the gaseous hydrogen output pipe 81, and the lower end of the liquid hydrogen storage tank 8 is connected to the liquid hydrogen output pipe 82.
[0018] The first heat exchanger 3 is also provided with a first helium expansion side channel 32 and a first helium refrigeration channel 33; the second heat exchanger 4 is also provided with a second helium expansion side channel 42 and a second helium refrigeration channel 43; the third heat exchanger 5 is also provided with a third helium refrigeration channel 52; and the fourth heat exchanger 6 is also provided with a fourth helium refrigeration channel 62.
[0019] The outlet of the first helium expansion side channel 32 of the first heat exchanger 3 is provided with a first distributor 34. The first distributor 34 is provided with a first distribution output pipe 341 and a second distribution output pipe 342. The first distribution output pipe 341 is connected to the inlet of the second helium expansion side channel 42 of the second heat exchanger 4. The outlet of the second helium expansion side channel 42 is connected to the inlet of the first expander 9. The outlet of the first expander 9 is connected to the inlet of the fourth helium refrigeration channel 62 in the fourth heat exchanger 6.
[0020] The second distribution output pipe 342 is connected to the inlet of the second expander 30, and the outlet of the second expander 30 and the outlet of the fourth helium refrigeration channel 62 are both connected to the input end of the second distributor 40. The output end of the second distributor 40 is connected to the inlet of the third helium refrigeration channel 52 in the third heat exchanger 5, and the third helium refrigeration channel 52, the second helium refrigeration channel 43, and the first helium refrigeration channel 33 are connected in sequence.
[0021] The outlet of the first helium refrigeration channel 33 in the first heat exchanger 3 is connected to the input end of the liquefaction section compression assembly, and the output end of the liquefaction section compression assembly is connected to the inlet of the first helium expansion side channel 32 in the first heat exchanger 3.
[0022] In this embodiment, the liquefaction section compression assembly includes: a first-stage liquefaction section compressor 50, a first-stage liquefaction section cooler 60, a second-stage liquefaction section compressor 70, a second-stage liquefaction section cooler 80, a third-stage liquefaction section compressor 90, and a third-stage liquefaction section cooler 901, connected in sequence. The output end of the third-stage liquefaction section cooler 901 is connected to the inlet of the first helium expansion side channel 32 within the first heat exchanger 3.
[0023] The following describes a method for hydrogen liquefaction using the helium-cooled hydrogen liquefaction system described above.
[0024] The steps are as follows: Room temperature hydrogen enters the precooling hydrogen channel 101 in the precooling heat exchanger 1 through the hydrogen inlet pipe 1011 for precooling. The precooling refrigerant used in the precooling section 100 is a mixed refrigerant containing methane, ethane, propane, n-butane, isobutane, and nitrogen. The molar ratio of methane, ethane, propane, n-butane, isobutane, and nitrogen in the mixed refrigerant is 0.2102:0.2970:0.2737:0.003:0.00013:0.2148.
[0025] The pre-cooled refrigerant is first compressed by a primary compressor 21 and cooled by a primary cooler 22, reaching a pressure of 2.89 bar and a temperature of 298 K. Then, it is compressed by a secondary compressor 23 and cooled by a secondary cooler 24, reaching a pressure of 7.48 bar and a temperature of 298 K. Next, it is compressed by a tertiary compressor 25 and cooled by a tertiary cooler 26, reaching a pressure of 19.39 bar and a temperature of 298 K. Finally, it is compressed by a quaternary compressor 27 and cooled by a quaternary cooler 28, reaching a pressure of 50 bar and a temperature of 298 K. The pre-cooled refrigerant at 50 bar and 298 K is then deeply cooled in the pre-cooled refrigerant return channel 103 and returns to the expansion valve 13, forming a low-temperature pre-cooled refrigerant at 1.2 bar and a temperature of 78 K. This 78 K low-temperature pre-cooled refrigerant enters the pre-cooled refrigerant channel 102 in the pre-cooling heat exchanger to provide cooling for hydrogen pre-cooling. After heat exchange in the pre-cooled hydrogen channel 101, the hydrogen gas is throttled by the pre-cooled hydrogen throttle valve 12 and its temperature drops to 80K.
[0026] In the liquefaction section 200, hydrogen and neon are mixed into the helium refrigerant, and the molar ratio of helium, hydrogen and neon is 86:13:1.
[0027] Hydrogen gas pre-cooled to 80K is sequentially cooled to 50K via the first liquefaction section hydrogen channel 31 in the first heat exchanger 3, then to 40K via the second liquefaction section hydrogen channel 41 in the second heat exchanger 4, then to 30K via the third liquefaction section hydrogen channel 51 in the third heat exchanger 5, and finally to 20K via the fourth liquefaction section hydrogen channel 61 in the fourth heat exchanger 6 to form liquid hydrogen. This liquid hydrogen then passes through the liquid hydrogen throttle valve 71 to reach a temperature of 20K and a pressure of one atmosphere before entering the liquid hydrogen storage tank 8. The gaseous hydrogen formed by flash evaporation in the liquid hydrogen storage tank 8 is output through the gaseous hydrogen output pipe 81, and the liquid hydrogen in the liquid hydrogen storage tank 8 is output through the liquid hydrogen output pipe 82.
[0028] The helium refrigerant at the outlet of the first helium refrigeration channel 33 of the first heat exchanger 3 is compressed by the first-stage compressor 50 of the liquefaction section and cooled by the first-stage cooler 60 of the liquefaction section, reaching a pressure of 10 bar and a temperature of 298 K; then it is compressed by the second-stage compressor 70 of the liquefaction section and cooled by the second-stage cooler 80 of the liquefaction section, reaching a pressure of 22 bar and a temperature of 298 K; and then it is compressed by the third-stage compressor 90 of the liquefaction section and cooled by the third-stage cooler 901 of the liquefaction section, reaching a pressure of 50 bar and a temperature of 298 K.
[0029] Helium refrigerant at a pressure of 50 bar and a temperature of 298 K, output from the liquefaction section's three-stage cooler 901, enters the first distributor 34 via the first helium expansion side channel 32 of the first heat exchanger 3. 20% of the volume of helium refrigerant in the first distributor 34 enters the first expander 9 via the first distribution outlet pipe 341 and the second helium expansion side channel 42 of the second heat exchanger 4, expanding and cooling to a pressure of 4.75 bar and a temperature of 19.8 K. This 19.8 K cryogenic helium refrigerant enters the fourth helium refrigeration channel 62 of the fourth heat exchanger 6, thus providing cooling to the fourth heat exchanger 6. The helium refrigerant at the outlet of the fourth helium refrigeration channel 62 has a pressure of 4.65 bar and a temperature of 29.5 K.
[0030] 80% of the helium refrigerant in the first distributor 34 enters the second expander 30 via the second distribution outlet pipe 342, where it expands and cools to a pressure of 4.65 bar and a temperature of 25.0 K. This cooled refrigerant then mixes with the helium refrigerant from the outlet of the fourth helium refrigeration channel 62 in the second distributor 40. The second distributor 40 outputs helium refrigerant at a pressure of 4.65 bar and a temperature of 25.9 K to the third helium refrigeration channel 52 in the third heat exchanger 5, thus providing cooling to the third heat exchanger 5. The helium refrigerant at the outlet of the third helium refrigeration channel 52 has a pressure of 4.55 bar and a temperature of 29.4 K, and enters the second helium refrigeration channel 43 in the second heat exchanger 4, thus providing cooling to the second heat exchanger 4. The helium refrigerant at the outlet of the second helium refrigeration channel 43 in the second heat exchanger 4 has a pressure of 4.45 bar and a temperature of 35.5 K, and enters the first helium refrigeration channel 33 in the first heat exchanger 3, providing cooling to the first heat exchanger 3. The helium refrigerant at the outlet of the first helium refrigeration channel 33 has a pressure of 4.35 bar and a temperature of 294.9 K. It then enters the helium compression assembly in the liquefaction section for pressurization, thus continuously circulating to provide cooling capacity.
[0031] This invention provides a helium-cooled hydrogen liquefaction system and a hydrogen liquefaction method. The precooling section of the helium-cooled hydrogen liquefaction system employs a four-stage compression process. By rationally controlling the pressure ratio of each compression stage, the shaft power of the compressor is effectively reduced to 250 kW. This not only effectively reduces equipment costs but also significantly lowers hydrogen liquefaction energy consumption. In the liquefaction section, a first distributor divides the helium refrigerant into two streams. One stream, comprising 20% of the refrigerant by volume, passes through a second heat exchanger and enters the first expansion stage for expansion and cooling before entering the fourth heat exchanger for final liquid hydrogen cooling. The other stream, comprising 80% of the refrigerant by volume, expands and cools through a second expander, mixes with the 20% stream from the fourth heat exchanger, and then enters the third heat exchanger to provide cooling. This structure facilitates the expansion and cooling of the helium refrigerant, thus providing sufficient cooling for hydrogen liquefaction. During hydrogen liquefaction, the pre-cooling section 100 uses a mixed refrigerant with a molar ratio of methane, ethane, propane, n-butane, isobutane, and nitrogen of 0.2102:0.2970:0.2737:0.003:0.00013:0.2148. Adding methane and ethane increases the refrigerant's vaporization rate, and methane has a significantly higher latent heat of vaporization than nitrogen. The addition of propane effectively increases the refrigerant's liquefaction rate. Isobutane and n-butane have large molecular weights, meaning they have high specific heat and heat of vaporization, and low adiabatic indices, thus effectively increasing the circulation volume and reducing the compressor load. In other words, the mixed refrigerant with the above molar ratio provides a more ideal cooling effect. In the liquefaction section, the helium refrigerant is a mixed refrigerant consisting of helium, hydrogen, and neon in a molar ratio of 86:13:1. Its advantages are that hydrogen is readily available, which can effectively reduce the cost of refrigerant, and the high latent heat of vaporization of neon can greatly improve the refrigeration effect.
Claims
1. A helium refrigeration hydrogen liquefaction system, comprising: The precooling section and liquefaction section are characterized in that: the precooling section includes: a precooling heat exchanger, a primary precooling compression assembly, a secondary precooling compression assembly, a tertiary precooling compression assembly, and a quaternary precooling compression assembly; each stage of the precooling compression assembly includes a compressor and a cooler; the precooling heat exchanger is provided with a precooling hydrogen channel, a precooling refrigerant channel, and a precooling refrigerant return channel; the inlet of the precooling hydrogen channel is connected to a hydrogen input pipe, and the outlet of the precooling hydrogen channel is provided with a precooling hydrogen output pipe, on which a precooling hydrogen throttling valve is installed. The outlet of the precooling refrigerant channel, the first-stage precooling compression assembly, the second-stage precooling compression assembly, the third-stage precooling compression assembly, and the fourth-stage precooling compression assembly are connected in sequence. The cooler outlet of the fourth-stage precooling compression assembly is connected to the inlet of the precooling refrigerant return channel. The outlet of the precooling refrigerant return channel is equipped with a precooling refrigerant throttle valve, and the outlet of the precooling refrigerant return channel is connected to the inlet of the precooling refrigerant channel through the precooling refrigerant throttle valve. The liquefaction section includes: a first heat exchanger, a second heat exchanger, a third heat exchanger, and a fourth heat exchanger. Each heat exchanger is equipped with a liquefaction section hydrogen channel. The liquefaction section hydrogen channels in the first, second, third, and fourth heat exchangers are connected sequentially. The outlet of the liquefaction section hydrogen channel in the fourth heat exchanger is connected to a liquid hydrogen delivery pipe, which is connected to a liquid hydrogen storage tank. A liquid hydrogen throttling valve is installed on the liquid hydrogen delivery pipe between the fourth heat exchanger and the liquid hydrogen storage tank. The output end of the pre-cooled hydrogen output pipe is connected to the inlet of the liquefaction section hydrogen channel in the first heat exchanger. The first heat exchanger is also provided with a first helium expansion side channel and a first helium refrigeration channel; the second heat exchanger is also provided with a second helium expansion side channel and a second helium refrigeration channel; the third heat exchanger is also provided with a third helium refrigeration channel; and the fourth heat exchanger is also provided with a fourth helium refrigeration channel. The outlet of the first helium expansion side channel in the first heat exchanger is equipped with a first distributor, which has a first distribution outlet pipe and a second distribution outlet pipe. The first distribution outlet pipe is connected to the inlet of the second helium expansion side channel in the second heat exchanger. The outlet of the second helium expansion side channel is connected to the inlet of the first expander. The outlet of the first expander is connected to the inlet of the fourth helium refrigeration channel in the fourth heat exchanger. The second distribution output pipe is connected to the inlet of the second expander. The outlet of the second expander and the outlet of the fourth helium refrigeration channel are both connected to the input end of the second distributor. The output end of the second distributor is connected to the inlet of the third helium refrigeration channel in the third heat exchanger. The third helium refrigeration channel, the second helium refrigeration channel, and the first helium refrigeration channel are connected in sequence. The outlet of the first helium refrigeration channel in the first heat exchanger is connected to the input end of the liquefaction section compression assembly, and the output end of the liquefaction section compression assembly is connected to the inlet of the first helium expansion side channel in the first heat exchanger.
2. The helium refrigeration hydrogen liquefier system of claim 1, wherein: The liquefaction section compression assembly includes: a liquefaction section primary compressor, a liquefaction section primary cooler, a liquefaction section secondary compressor, a liquefaction section secondary cooler, a liquefaction section tertiary compressor, and a liquefaction section tertiary cooler connected in sequence; the output end of the liquefaction section tertiary cooler is connected to the inlet of the first helium expansion side channel in the first heat exchanger.
3. The helium refrigeration hydrogen liquefier system of claim 1, wherein: The upper end of the liquid hydrogen storage tank is connected to a gaseous hydrogen output pipe, and the lower end of the liquid hydrogen storage tank is connected to a liquid hydrogen output pipe.
4. A method for helium refrigeration hydrogen liquefaction, comprising using the helium refrigeration hydrogen liquefaction system according to any one of claims 1 to 3, characterized in that: The precooling refrigerant used in the precooling heat exchanger, primary precooling compression assembly, secondary precooling compression assembly, tertiary precooling compression assembly, and quaternary precooling compression assembly in the precooling section is a mixed refrigerant containing methane, ethane, propane, n-butane, isobutane, and nitrogen, with the molar ratio of methane, ethane, propane, n-butane, isobutane, and nitrogen being [missing information]. 0.2102:0.2970:0.2737:0.003:0.00013:0.2148; The helium refrigerant in the liquefaction section is mixed with hydrogen and neon, and the molar ratio of helium, hydrogen and neon is 86:13:
1.
5. A helium refrigeration hydrogen liquefaction method according to claim 4, characterized by: The hydrogen liquefaction step includes: the volume ratio of helium refrigerant in the first distribution outlet pipe and the second distribution outlet pipe is 20%:80%.