Method of hydrogen liquefaction using optimized claude refrigeration cycles

A hydrogen liquefaction method, comprising:

• providing a purified gaseous hydrogen feed stream, wherein the purified gaseous hydrogen feed stream comprises about 75% ortho-hydrogen and 25% para-hydrogen, and further wherein the purified gaseous hydrogen feed stream comprises a pressure within the range of 800 kPa·G to 4,000 kPa·G and a temperature of about 300K;
• providing a first hydrogen circulation compressor and a second hydrogen circulation compressor, wherein the first hydrogen circulation compressor discharges a first hydrogen circulation compressor final stage discharge stream, and further wherein the second hydrogen circulation compressor discharges a second hydrogen circulation compressor final stage discharge stream;
• combining the purified gaseous hydrogen feed stream and a mixed intermediate-pressure circulation gaseous hydrogen stream inside the second hydrogen circulation compressor forming the second hydrogen circulation compressor final stage discharge stream, wherein the second hydrogen circulation compressor final stage discharge stream comprises a higher pressure within the range of 3,200 kPa·G to 4,000 kPa·G;
• splitting the second hydrogen circulation compressor final stage discharge stream into a first split gaseous hydrogen stream and a second split gaseous hydrogen stream;
• cooling the first split gaseous hydrogen stream to about 82K inside a precooling main heat exchanger to form a first cold gaseous hydrogen stream;
• purifying the first cold gaseous hydrogen stream inside a swing hydrogen absorption bed system to form a deep purified cold gaseous hydrogen stream;
• passing the deep purified cold gaseous hydrogen stream through a fixed-bed catalyst ortho-para hydrogen converter, wherein the deep purified cold gaseous hydrogen stream forms a first p-H2 enriched gaseous hydrogen stream, wherein the first p-H2 enriched gaseous hydrogen stream comprises a new equilibrium composition of about 53% ortho-hydrogen and about 47% para-hydrogen, and further wherein the first p-H2 enriched gaseous hydrogen stream increases in temperature due to the exothermic process of the ortho to para hydrogen conversion;
• cooling the first p-H2 enriched gaseous hydrogen stream inside the precooling main heat exchanger to form a first cold p-H2 enriched gaseous hydrogen stream, wherein the temperature of the first cold p-H2 enriched gaseous hydrogen stream is reduced to 82K;
• cooling the first cold p-H2 enriched gaseous hydrogen stream inside a catalyst filled intermediate-temperature ortho-para hydrogen converter of an intermediate temperature main heat exchanger to form a second cold p-H2 enriched gaseous hydrogen stream, wherein the second cold p-H2 enriched gaseous hydrogen stream comprises a temperature of about 40K;
• converting ortho-hydrogen to para-hydrogen in the second cold p-H2 enriched gaseous hydrogen stream inside the catalyst filled intermediate-temperature ortho-para hydrogen converter of the intermediate temperature main heat exchanger, wherein the second cold p-H2 enriched gaseous hydrogen stream comprises a new equilibrium composition of about 11% ortho-hydrogen and about 89% para-hydrogen;
• cooling the second cold p-H2 enriched gaseous hydrogen stream inside a catalyst filled low-temperature ortho-para hydrogen converter of a cold temperature main heat exchanger to form a subcooled high-pressure p-H2 enriched liquid hydrogen stream, wherein the subcooled high-pressure p-H2 enriched liquid hydrogen stream comprises a temperature of about 23.5K;
• converting ortho-hydrogen to para-hydrogen in the subcooled high-pressure p-H2 enriched liquid hydrogen stream inside the catalyst filled low-temperature ortho-para hydrogen converter of the cold temperature main heat exchanger, wherein the subcooled high-pressure p-H2 enriched liquid hydrogen stream comprises a new equilibrium composition of about 1% ortho-hydrogen and about 89% para-hydrogen;
• reducing the pressure of the subcooled high-pressure p-H2 enriched liquid hydrogen stream with a Joule-Thomson valve (J/T valve) to form a low-pressure liquid hydrogen product stream, wherein the low-pressure liquid hydrogen product stream comprises a pressure of about 50 kPa·G and temperature of about 21.7K;
• feeding the low-pressure liquid hydrogen product stream into a liquid hydrogen storage tank;
• removing a flashed gaseous hydrogen stream from the liquid hydrogen storage tank through a pressure control valve;
• feeding the flashed gaseous hydrogen stream into a liquid hydrogen storage tank pressure control valve, wherein the flashed gaseous hydrogen stream exits the liquid hydrogen storage tank pressure control valve as an optimized hydrogen Claude cycle hydrogen makeup stream;
• and
• sending the hydrogen Claude cycle hydrogen makeup stream to a hydrogen Claude half-opened cycle system, wherein the hydrogen Claude cycle hydrogen makeup stream mixes with a low-pressure thermosiphon hydrogen vapor stream to form a mixed first hydrogen thermosiphon vapor stream.