CN211601324U - Ortho-para hydrogen conversion system - Google Patents
Ortho-para hydrogen conversion system Download PDFInfo
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- CN211601324U CN211601324U CN201922472049.8U CN201922472049U CN211601324U CN 211601324 U CN211601324 U CN 211601324U CN 201922472049 U CN201922472049 U CN 201922472049U CN 211601324 U CN211601324 U CN 211601324U
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 100
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 124
- 239000001257 hydrogen Substances 0.000 claims abstract description 116
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 116
- 238000001816 cooling Methods 0.000 claims abstract description 57
- 239000002826 coolant Substances 0.000 claims abstract description 42
- 238000005057 refrigeration Methods 0.000 claims abstract description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical group N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 86
- 239000001307 helium Substances 0.000 abstract description 82
- 229910052734 helium Inorganic materials 0.000 abstract description 82
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 abstract description 82
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 42
- 239000007788 liquid Substances 0.000 abstract description 33
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 230000000694 effects Effects 0.000 abstract description 3
- 229910001873 dinitrogen Inorganic materials 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 8
- 150000002431 hydrogen Chemical class 0.000 description 8
- 238000000034 method Methods 0.000 description 7
- 239000012535 impurity Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 3
- 239000003507 refrigerant Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000009413 insulation Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- VNNRSPGTAMTISX-UHFFFAOYSA-N chromium nickel Chemical compound [Cr].[Ni] VNNRSPGTAMTISX-UHFFFAOYSA-N 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 235000014413 iron hydroxide Nutrition 0.000 description 1
- NCNCGGDMXMBVIA-UHFFFAOYSA-L iron(ii) hydroxide Chemical compound [OH-].[OH-].[Fe+2] NCNCGGDMXMBVIA-UHFFFAOYSA-L 0.000 description 1
- 230000013011 mating Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0005—Light or noble gases
- F25J1/001—Hydrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/0062—Light or noble gases, mixtures thereof
- F25J1/0065—Helium
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0204—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
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- Engineering & Computer Science (AREA)
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- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
The utility model discloses an ortho-para hydrogen conversion system, including the cold box, be equipped with coolant system, hydrogen system, refrigeration working medium system and heat transfer system in the cold box, coolant is nitrogen gas, and the refrigeration working medium is the helium, and hydrogen passes through eight grade heat transfer device heat exchanges to and through ortho-para hydrogen conversion device conversion, para hydrogen content has reached more than 95% in the liquid hydrogen after the conversion. The first heat exchange device of the utility model takes the cold nitrogen and the helium which flows back from the secondary heat exchanger as cooling media, thereby improving the cooling effect and reducing the energy consumption of the system operation; the hydrogen after the second, third and fourth orthoparahydrogen conversion devices reflows and is cooled again by the corresponding heat exchange devices, so that the energy consumption of the system is reduced, and the capability of hydrogen liquefaction is improved through the cooperation of a cooling medium system, a helium system and a hydrogen system.
Description
Technical Field
The utility model relates to an ortho-para hydrogen conversion system.
Background
Normal hydrogen gas is composed of both ortho-hydrogen and para-hydrogen molecules, and liquefaction is difficult due to the low critical temperature and conversion temperature of hydrogen, the low latent heat of vaporization, and the theoretical minimum work of liquefaction being highest among all gases. During liquefaction, ortho-hydrogen is required to be quickly and nearly completely converted into para-hydrogen under the action of a catalyst, so that the phenomenon that the ortho-hydrogen is continuously converted into the para-hydrogen in the storage of the liquid hydrogen to generate conversion heat, and the volatilization loss of the liquid hydrogen is caused is avoided. The hydrogen liquefaction adopts the cyclic processes of compression, expansion, cooling and compression. The difficulty of this technique is therefore the production and storage of liquid hydrogen, avoiding the conversion of orthohydrogen to parahydrogen.
When hydrogen is used for replacing oil, natural gas and coal for large-scale wide use, the hydrogen storage density is one of key economic indexes. 1. The hydrogen storage density is high, the density of liquid hydrogen is about 800 times of that of gaseous hydrogen, and compared with a hydrogen storage container with the same volume, the hydrogen storage quality of the liquid hydrogen storage system is greatly improved. The energy agency (IEA) of United nations proposes that the mass hydrogen storage density is more than 5 percent and the volume hydrogen storage density is more than 50kg H2/m3And the hydrogen discharge temperature is lower than 423K. The U.S. department of energy (DOE) proposes that the hydrogen storage density is not less than 6.5% by mass and not less than 62kg H by volume2/m3The actual hydrogen storage capacity of the vehicular hydrogen storage system is more than 3.1kg (equivalent to the fuel required for a car running for 500 km). The volume of the transportation tank truck is limited, but with the change of density, the quantity of hydrogen which can be transported by each tank truck has a great difference, and the conceivable cost has a great difference.
The existing hydrogen refrigeration process has the following defects that 1, the stress of a hydrogen turbine and a compressor rotor is high, and the related technology in China is immature at present; 2. hydrogen working medium has hydrogen embrittlement phenomenon to the material; 3. high operation pressure, easy leakage and high risk.
SUMMERY OF THE UTILITY MODEL
The present invention provides a liquid hydrogen production and an ortho-para hydrogen conversion system that addresses the above-mentioned deficiencies in the prior art.
The technical scheme of the utility model as follows:
an ortho-para hydrogen conversion system comprises a cold box (1), wherein the cold box (1) is used for providing a low-temperature environment and insulating heat, and a cooling medium system, a hydrogen system, a refrigeration working medium system and a heat exchange system are arranged in the cold box (1); wherein,
the heat exchange system comprises a first heat exchange device (10), a second heat exchange device (20), a third heat exchange device (30), a fourth heat exchange device (40), a fifth heat exchange device (50), a sixth heat exchange device (60), a seventh heat exchange device (70) and an eighth heat exchange device (80), wherein the heat exchange devices are used for exchanging heat between at least two media;
the cooling medium system comprises a cooling medium inflow pipe (11), a cooling device (13) for cooling the cooling medium and a cooling medium outflow pipe (12), wherein the cooling medium inflow pipe (11) is connected with a first inlet end of the cooling device (13), the cooling medium outflow pipe (12) is connected with a first outlet end of the cooling device (13), and the other end of the cooling medium outflow pipe (12) is connected with a fourth inlet end of the first heat exchange device (10); the cooling medium is preferably nitrogen, the nitrogen is easy to obtain and low in cost, the nitrogen enters the cooling device (13) from the outside of the cold box (1) through the cooling medium inflow pipe (11), the cold box (1) preliminarily cools the nitrogen, the cooling device (13) further cools the nitrogen into liquid nitrogen, and the balance between the liquid nitrogen and the gaseous nitrogen is adopted in the cooling device (13); gaseous nitrogen flows out of the cooling medium outflow pipe (12) and enters the first heat exchange device (10) to play a role in preliminary precooling of the first heat exchange device (10);
helium is used as a refrigerating working medium, and the adiabatic index of the helium is high; the helium system comprises a first pipeline (21), a second pipeline (22) and a compressor (7), the first pipeline (21) is sequentially connected with the first heat exchange device (10), the second heat exchange device (20), the third heat exchange device (30), the fourth heat exchange device (40), the sixth heat exchange device (60) and the seventh heat exchange device (70) in series, and the first pipeline (21) is further connected with a second inlet end of the eighth heat exchange device (80); a second outlet end of the eighth heat exchange device (80) is connected with a second pipeline (22), and the second pipeline (22) is also sequentially connected in series with the seventh heat exchange device (70), the sixth heat exchange device (60), the fifth heat exchange device (50), the fourth heat exchange device (40), the third heat exchange device (30) and the first heat exchange device (10); the second pipeline (22) is connected with the inlet end of the compressor (7) outside the cold box (1), and the outlet end of the compressor (7) is connected with the first pipeline (21); the first pipeline (21) is also provided with at least two turboexpanders (3), including a first turboexpander (31) arranged between the fourth heat exchange device (40) and the sixth heat exchange device (60), and a second turboexpander (32) arranged at the second outlet end of the seventh heat exchange device (70); the turbine expander (3) carries out adiabatic expansion refrigeration on the helium,
the hydrogen system comprises a first hydrogen pipeline (4), and the first hydrogen pipeline (4) is sequentially connected with the first heat exchange device (10), the second heat exchange device (20), the third heat exchange device (30), the fourth heat exchange device (40), the fifth heat exchange device (50), the sixth heat exchange device (60), the seventh heat exchange device (70) and the eighth heat exchange device (80) in series; the first hydrogen pipeline (4) is provided with at least four orthoparahydrogen conversion devices, and comprises a first orthoparahydrogen conversion device (51) arranged between the second heat exchange device (20) and the third heat exchange device (30), a second orthoparahydrogen conversion device (52) arranged at a first outlet end of the fourth heat exchange device (40), a third orthoparahydrogen conversion device (53) arranged at a first outlet end of the sixth heat exchange device (60), and a fourth orthoparahydrogen conversion device (54) arranged at a first outlet end of the eighth heat exchange device (80). Four-stage ortho-para hydrogen converter; more nearly continuous conversion; reducing the heat of conversion; energy is saved; easy to manufacture and maintain.
Preferably, the outlet end of the second para-hydrogen conversion device (52) is connected with the fourth inlet end of the fourth heat exchange device (40) through the first hydrogen pipeline (4), and the fourth outlet end of the fourth heat exchange device (40) is connected with the fifth heat exchange device (50); the outlet end of the third para-hydrogen conversion device (53) is connected with the fourth inlet end of the sixth heat exchange device (60) through the first hydrogen pipeline (4), and the fourth outlet end of the sixth heat exchange device (60) is connected with the seventh heat exchange device (70); the outlet end of the fourth para-hydrogen conversion device (54) is connected with the third inlet end of the eighth heat exchange device (80) through the first hydrogen pipeline (4), and the third outlet end of the eighth heat exchange device (80) is connected to the outside of the cold box (1).
Preferably, the first ortho-para hydrogen conversion device (51) is arranged in a storage tank (5) for providing a low-temperature environment; and a second outlet end of the cooling device (13) is connected with an inlet end of the storage tank (5), and a second inlet end of the cooling device (13) is connected with an outlet end of the storage tank (5).
Preferably, the third outlet end of the cooling device (13) is further connected to the second inlet end of the second heat exchange device (20), and the second outlet end of the second heat exchange device (20) is connected to the third inlet end of the cooling device (13).
Preferably, the first pipeline (21) is connected in sequence with the second inlet end of the first heat exchange device (10), the second outlet end of the first heat exchange device (10), the second inlet end of the second heat exchange device (20), the second outlet end of the second heat exchange device (20), the second inlet end of the third heat exchange device (30), the second outlet end of the third heat exchange device (30), the second inlet end of the fourth heat exchange device (40), the second outlet end of the fourth heat exchange device (40), the second inlet end of the sixth heat exchange device (60), the second outlet end of the sixth heat exchange device (60), the second inlet end of the seventh heat exchange device (70), the second outlet end of the seventh heat exchange device (70) and the second inlet end of the eighth heat exchange device (80); the second pipeline (22) is connected in sequence with a second outlet end of the eighth heat exchange device (80), a third inlet end of the seventh heat exchange device (70), a third outlet end of the seventh heat exchange device (70), a third inlet end of the sixth heat exchange device (60), a third outlet end of the sixth heat exchange device (60), a third inlet end of the fifth heat exchange device (50), a third outlet end of the fifth heat exchange device (50), a third inlet end of the fourth heat exchange device (40), a third outlet end of the fourth heat exchange device (40), a third inlet end of the third heat exchange device (30), a third outlet end of the third heat exchange device (30), a third inlet end of the first heat exchange device (10), and a third outlet end of the first heat exchange device (10), and is connected to the outside of the cold box (1) from the third outlet end of the first heat exchange device (10).
Preferably, the outlet end of the compressor (7) is connected with an oil remover, and the outlet end of the oil remover is connected with the first pipeline (11).
Preferably, the first hydrogen pipeline (4) is provided with at least one first purifier (6.1), and the first purifier (6.1) is arranged between the first heat exchange device (10) and the second heat exchange device (20).
Preferably, said first circuit (21) is provided with at least two purifiers, comprising a second purifier (6.2) arranged between said second heat exchange means (20) and said third heat exchange means (30), and a third purifier (6.3) arranged between said second turboexpander (32) and said eighth heat exchange means (80).
Preferably, the first heat exchange device (10), the second heat exchange device (20), the third heat exchange device (30), the fourth heat exchange device (40), the fifth heat exchange device (50), the sixth heat exchange device (60), the seventh heat exchange device (70) and the eighth heat exchange device (80) are all plate-fin heat exchangers. Leakage rate of plate-fin heat exchanger<109Pa.m3And the leakage rate of the refrigerant in the system is reduced, the risk of system operation is reduced, and the system is safer.
Compared with the prior art, the beneficial effects of the utility model are as follows:
first, the utility model discloses an ortho-para hydrogen conversion system, through the coolant system, the helium system, the mating reaction of hydrogen system, and the hydrogen backward flow after the conversion of second ortho-para hydrogen conversion device cools off again to fourth heat transfer device, the hydrogen backward flow after the conversion of third ortho-para hydrogen conversion device cools off again to sixth heat transfer device, the hydrogen backward flow after the conversion of third ortho-para hydrogen conversion device cools off again to eighth heat transfer device, the system energy consumption is reduced, the liquefied ability of hydrogen has been improved simultaneously, the continuous operation duration of system has been improved, the liquefied efficiency of hydrogen has been improved; the first heat exchange device of the utility model takes the cold nitrogen and the helium which flows back from the secondary heat exchanger as cooling media, thereby improving the cooling effect and reducing the energy consumption of the system operation; the purity of the liquefied hydrogen is improved through the filtering and purifying of the first purifier, and the purity of helium in the helium system is improved through the second purifier and the third purifier which are arranged on the first pipeline, so that the running stability of the helium system is improved; the liquid hydrogen obtained by the ortho-para hydrogen conversion system of the utility model has the para-hydrogen content reaching more than 95 percent, and reduces the evaporation loss of the liquid hydrogen caused by the conversion of the ortho-para hydrogen in the transportation process.
Secondly, the helium turboexpander has higher operating efficiency than a hydrogen turboexpander, and helium working medium does not corrode equipment materials; the refrigeration working medium adopted in the utility model is helium working medium which is always in gaseous state at the operation temperature of the system, thereby eliminating the problem caused by multiphase expansion; at the same time, helium is inert and is also safe to the environment in the event of a leak; the utility model discloses a practical heat transfer device is plate-fin heat exchanger, plate-fin heat exchanger leakage rate<109Pa.m3And the leakage rate of the refrigerant in the system is reduced, the risk of system operation is reduced, and the system is safer.
Of course, it is not necessary for any particular product to achieve all of the above-described advantages at the same time.
Drawings
Figure 1 is a schematic diagram of an ortho-para hydrogen conversion system of example 1 of the present invention.
Detailed Description
The present invention will be further described with reference to the following specific examples. It should be understood that these examples are only for illustrating the present invention, and are not intended to limit the scope of the present invention. In practical applications, the improvement and adjustment made by those skilled in the art according to the present invention still belong to the protection scope of the present invention.
Example 1
This example provides an ortho-para hydrogen conversion system, and referring to fig. 1, fig. 1 is a schematic diagram of an ortho-para hydrogen conversion system according to example 1 of the present invention. The heat-preservation cold box comprises a cold box (1), wherein the cold box (1) is used for providing a low-temperature environment and preserving heat, and a cooling medium system, a hydrogen system, a refrigeration working medium system and a heat exchange system are arranged in the cold box (1); wherein,
the heat exchange system comprises a first heat exchange device (10), a second heat exchange device (20), a third heat exchange device (30), a fourth heat exchange device (40), a fifth heat exchange device (50), a sixth heat exchange device (60), a seventh heat exchange device (70) and an eighth heat exchange device (80), wherein the heat exchange devices are used for exchanging heat between at least two media;
the cooling medium system comprises a cooling medium inflow pipe (11), a cooling device (13) for cooling the cooling medium and a cooling medium outflow pipe (12), wherein the cooling medium inflow pipe (11) is connected with a first inlet end of the cooling device (13), the cooling medium outflow pipe (12) is connected with a first outlet end of the cooling device (13), and the other end of the cooling medium outflow pipe (12) is connected with a fourth inlet end of the first heat exchange device (10); the cooling medium is preferably nitrogen, the nitrogen is easy to obtain and low in cost, the nitrogen enters the cooling device (13) from the outside of the cold box (1) through the cooling medium inflow pipe (11), the cold box (1) preliminarily cools the nitrogen, the cooling device (13) further cools the nitrogen into liquid nitrogen, and the balance between the liquid nitrogen and the gaseous nitrogen is adopted in the cooling device (13); gaseous nitrogen flows out of the cooling medium outflow pipe (12) and enters the first heat exchange device (10), so that the preliminary precooling effect on the first heat exchange device (10) is achieved, and the energy consumption of system operation is reduced.
In the embodiment, helium is used as a refrigerating working medium without using hydrogen, so that the device is safer and has a high heat insulation index. The helium system comprises a first pipeline (21), a second pipeline (22) and a compressor (7), wherein the compressor (7) is a helium screw compressor. The first pipeline (21) is sequentially connected in series with the first heat exchange device (10), the second heat exchange device (20), the third heat exchange device (30), the fourth heat exchange device (40), the sixth heat exchange device (60) and the seventh heat exchange device (70), and the first pipeline (21) is also connected with a second inlet end of the eighth heat exchange device (80); a second outlet end of the eighth heat exchange device (80) is connected with a second pipeline (22), and the second pipeline (22) is also sequentially connected in series with the seventh heat exchange device (70), the sixth heat exchange device (60), the fifth heat exchange device (50), the fourth heat exchange device (40), the third heat exchange device (30) and the first heat exchange device (10); the second pipeline (22) is connected with the inlet end of the compressor (7) outside the cold box (1), the outlet end of the compressor (7) is connected with the first pipeline (21), and high-pressure helium gas compressed by the compressor (7) enters the cold box (1) and circulates between the first pipeline (21) and the second pipeline (22).
In this embodiment, the first pipeline (21) is further provided with at least two turboexpanders (3), and the turboexpanders (3) are helium turboexpanders, so that the operation efficiency of the turboexpanders is improved; the turbo expander (3) adiabatically expands the helium to reach the temperature of ortho-para hydrogen conversion in this example. Preferably, the turboexpander (3) comprises a first turboexpander (31) arranged between the fourth heat exchange device (40) and the sixth heat exchange device (60), and a second turboexpander (32) arranged at the rear end of the seventh heat exchange device (70). After being cooled by the first heat exchange device (10), the second heat exchange device (20), the third heat exchange device (30) and the fourth heat exchange device (40), the helium is subjected to adiabatic expansion refrigeration by the first turbo expander (31), the refrigerated helium is further cooled by the sixth heat exchange device (60) and the seventh heat exchange device (70), the helium flowing out of the second outlet end of the seventh heat exchange device (70) is subjected to further adiabatic expansion refrigeration by the second turbo expander (32), the cooled helium is low-temperature helium and low-pressure helium of about 18.5K, the cooled helium enters the second inlet end of the eighth heat exchange device (80), and is sequentially subjected to backflow reheating by each stage of heat exchange devices, finally exits the cooling box (1) from the third outlet end of the first heat exchange device (10), is converted into normal-temperature helium, and is compressed by the helium screw compressor and enters the cooling box (1) again for circulation.
In this embodiment, the hydrogen system includes a first hydrogen pipeline (4), and the first hydrogen pipeline (4) is sequentially connected in series to the first heat exchange device (10), the second heat exchange device (20), the third heat exchange device (30), the fourth heat exchange device (40), the fifth heat exchange device (50), the sixth heat exchange device (60), the seventh heat exchange device (70), and the eighth heat exchange device (80).
In this embodiment, the first hydrogen pipeline (4) is provided with at least four orthoparahydrogen conversion devices, the orthohydrogen conversion devices are orthohydrogen converters, a chromium-nickel catalyst and an iron hydroxide catalyst are arranged in the orthohydrogen converter, orthohydrogen-parahydrogen conversion is realized under the action of the catalysts, and the content of parahydrogen in a liquid hydrogen product after conversion by the four-stage orthohydrogen converter is at least 95%. The device comprises a first ortho-para hydrogen conversion device (51) arranged between the second heat exchange device (20) and the third heat exchange device (30), a second ortho-para hydrogen conversion device (52) arranged at the first outlet end of the fourth heat exchange device (40), a third ortho-para hydrogen conversion device (53) arranged at the first outlet end of the sixth heat exchange device (60), and a fourth ortho-para hydrogen conversion device (54) arranged at the first outlet end of the eighth heat exchange device (80). After the hydrogen is cooled to a preset temperature by the first heat exchange device (10) and the second heat exchange device (20), the hydrogen is subjected to ortho-para hydrogen conversion by the first ortho-para hydrogen conversion device (51), and the para-hydrogen content is controlled within a preset range; then the hydrogen is cooled to a preset range by a third heat exchange device (30) and a fourth heat exchange device (40), and the second ortho-para hydrogen conversion device (52) carries out ortho-para hydrogen conversion; the hydrogen is cooled to a predetermined range by a fifth heat exchange device (50) and a sixth heat exchange device (60), the ortho-para hydrogen is converted by a third ortho-para hydrogen conversion device (53), and finally the hydrogen is cooled to a predetermined range by a seventh heat exchange device (70) and an eighth heat exchange device (80), and the ortho-para hydrogen is converted by a fourth ortho-para hydrogen conversion device (53). The use of the four-stage ortho-para hydrogen converter enables the ortho-para hydrogen conversion of hydrogen to be closer to continuous conversion, reduces the conversion heat, saves more energy and is easy to manufacture and maintain.
Preferably, the outlet end of the second ortho-para hydrogen conversion device (52) is connected with the fourth inlet end of the fourth heat exchange device (40) through the first hydrogen pipeline (4), the fourth outlet end of the fourth heat exchange device (40) is connected with the fifth heat exchange device (50), ortho-para hydrogen is converted into an exothermic process, hydrogen is subjected to adiabatic conversion in the second ortho-para hydrogen conversion device (52), and meanwhile, the temperature is raised, so that the converted hydrogen needs to flow back to the fourth heat exchange device (40) for cooling again, and the energy consumption of the system is reduced. The outlet end of the third ortho-para hydrogen conversion device (53) is connected with the fourth inlet end of the sixth heat exchange device (60) through the first hydrogen pipeline (4), the fourth outlet end of the sixth heat exchange device (60) is connected with the seventh heat exchange device (70), and the hydrogen converted by the third ortho-para hydrogen conversion device (53) flows back to the sixth heat exchange device (60) to be cooled again to the preset temperature; the outlet end of the fourth ortho-para hydrogen conversion device (54) is connected with the third inlet end of the eighth heat exchange device (80) through the first hydrogen pipeline (4), the third outlet end of the eighth heat exchange device (80) is connected to the outside of the cold box (1), and hydrogen subjected to heat insulation conversion by the fourth ortho-para hydrogen conversion device (54) flows back to the eighth heat exchange device (80) again to be cooled and then flows out of the cold box to be stored in the liquid hydrogen Dewar (100).
Preferably, the first para-hydrogen conversion device (51) is arranged in a storage tank (5) for providing a low-temperature environment and is used for carrying out constant-temperature conversion; and a second outlet end of the cooling device (13) is connected with an inlet end of the storage tank (5), and a second inlet end of the cooling device (13) is connected with an outlet end of the storage tank (5). Liquid nitrogen stored in the cooling device (13) enters the storage tank (5), the liquid nitrogen circulates between the storage tank (5) and the cooling device (13), and the first para-hydrogen conversion device (51) is soaked in the liquid nitrogen, so that the first para-hydrogen conversion device (51) is always kept at a preset temperature for carrying out constant-temperature conversion on hydrogen.
Preferably, a third outlet end of the cooling device (13) is further connected to a third inlet end of the second heat exchange device (20), a third outlet end of the second heat exchange device (20) is connected to a third inlet end of the cooling device (13), liquid nitrogen in the cooling device (13) precools the second heat exchange device (20), and the liquid nitrogen circulates between the cooling device (13) and the second heat exchange device (20), so that the circulation process enables the second heat exchange device (20) to be always made of liquid nitrogen as a heat exchange medium, the hydrogen conversion efficiency of the system is improved, the energy consumption is reduced, and meanwhile, the stability of the system operation is improved.
Preferably, the first pipeline (21) is sequentially connected to a second inlet end of the first heat exchange device (10), a second outlet end of the first heat exchange device (10), a second inlet end of the second heat exchange device (20), a second outlet end of the second heat exchange device (20), a second inlet end of the third heat exchange device (30), a second outlet end of the third heat exchange device (30), a second inlet end of the fourth heat exchange device (40), a second outlet end of the fourth heat exchange device (40), a second inlet end of the sixth heat exchange device (60), a second outlet end of the sixth heat exchange device (60), a second inlet end of the seventh heat exchange device (70), a second outlet end of the seventh heat exchange device (70), and a second inlet end of the eighth heat exchange device (80). Helium enters the first heat exchange device (10) from the second inlet end of the first heat exchange device (10) and is cooled, and sequentially enters the second heat exchange device (20), the third heat exchange device (30), the fourth heat exchange device (40), the sixth heat exchange device (60) and the seventh heat exchange device (70) for gradual cooling, and adiabatic expansion refrigeration of the two turboexpanders, so that the helium is finally cooled to the temperature of about 18.5K.
In this embodiment, the second pipeline (22) is sequentially connected to the second outlet end of the eighth heat exchange device (80), the third inlet end of the seventh heat exchange device (70), the third outlet end of the seventh heat exchange device (70), the third inlet end of the sixth heat exchange device (60), the third outlet end of the sixth heat exchange device (60), the third inlet end of the fifth heat exchange device (50), the third outlet end of the fifth heat exchange device (50), the third inlet end of the fourth heat exchange device (40), the third outlet end of the fourth heat exchange device (40), the third inlet end of the third heat exchange device (30), the third outlet end of the third heat exchange device (30), the third inlet end of the first heat exchange device (10), and the third outlet end of the first heat exchange device (10), and is connected to the outside of the cold box (1) from the third outlet end of the first heat exchange device (10). After the helium is cooled to about 18.5K, the helium flows back from the eighth-stage heat exchange device (80) to pass through the seventh heat exchange device (70), the sixth heat exchange device (60), the fifth heat exchange device (50), the fourth heat exchange device (40), the third heat exchange device (30) and the first heat exchange device (10) in sequence to serve as a refrigerating working medium.
Preferably, first hydrogen pipeline (4) are equipped with at least one first clarifier (6.1), first clarifier (6.1) are located first heat transfer device (10) with between second heat transfer device (20), hydrogen is after cooling in first heat transfer device (10), and partly impurity takes place to condense, filters the impurity after the condensation through first clarifier (6.1), improves the purity of hydrogen, maintains the stability of hydrogen system operation.
Preferably, said first circuit (21) is provided with at least two purifiers, comprising a second purifier (6.2) arranged between said second heat exchange means (20) and said third heat exchange means (30), and a third purifier (6.3) arranged between said second turboexpander (32) and said eighth heat exchange means (80). After the helium is cooled to a preset temperature by liquid nitrogen in the second heat exchange device (20), part of impurities are condensed, and the condensed impurities are filtered by the second purifier (6.2) to maintain the operation stability of a helium system. The helium is cooled to about 18.5K through the second turbo expander (32), at the temperature, trace impurities in the helium can be condensed, and the third purifier (6.3) is used for filtering and purifying the trace impurities in the helium, so that the purity of the helium is further improved, and the operation stability of a helium system is further improved.
Preferably, the outlet end of the compressor (7) is further connected with an oil remover, the oil remover is arranged outside the cold box (1), and the outlet end of the oil remover is connected with the first pipeline (21) and used for filtering and removing oil from the compressed high-pressure helium gas, so that damage to other components on the pipeline, such as a valve or a turbine expander, caused by condensation of oil gas in the pipeline after the helium gas is cooled is avoided, and stable operation of the system is influenced.
Preferably, the first heat exchange device (10), the second heat exchange device (20), the third heat exchange device (30), the fourth heat exchange device (40), the fifth heat exchange device (50), the sixth heat exchange device (60), the seventh heat exchange device (70) and the eighth heat exchange device (80) are all plate-fin heat exchangers. Leakage rate of plate-fin heat exchanger<109Pa.m3And the leakage rate of the refrigerant in the system is reduced, the risk of system operation is reduced, and the system is safer.
Preferably, the cooling medium inflow pipe (11) is provided with a first valve (81) for opening or closing the cooling medium inflow pipe (11) and controlling the nitrogen gas to flow into the cooling device (13); and a second valve (82) is arranged at the rear end of the fourth heat exchange device (40) and used for controlling the on-off of the first pipeline (21), and is arranged between the second outlet end of the fourth heat exchange device (40) and the first turboexpander (31). The first hydrogen pipeline (4) is provided with a third valve (83) which is arranged between the seventh heat exchange device (70) and the eighth heat exchange device (80); and the rear end of the third outlet end of the eighth heat exchange device (80) is connected with a third valve (73) for opening or closing the first hydrogen pipeline (4).
The operation of the ortho-para hydrogen conversion system of this example is as follows:
a cooling medium system, namely a nitrogen system, starts to work, normal-temperature nitrogen flows into a cooling device (13) from a cooling medium inflow pipe (11), and the cooling device (13) cools the nitrogen into liquid nitrogen and stores the liquid nitrogen; and cold nitrogen flows out of the cooling device (13) through the cooling medium outflow pipe (12) and enters the fourth inlet end of the first heat exchange device (10) to be used as a cooling medium of the first heat exchange device (10), and the reheated nitrogen flows out of the cold box (1) from the fourth outlet end of the first heat exchange device (10) to be recycled. Liquid nitrogen stored in the cooling device (13) circulates between the cooling device (13) and the second heat exchange device (20) and serves as a cooling medium of the second heat exchange device (20). Meanwhile, liquid nitrogen in the cooling device (13) circulates between the cooling device (13) and the storage tank (5), and a low-temperature environment is provided for the first para-hydrogen conversion device.
When the helium system starts to work, the normal-temperature helium is compressed by the helium screw compressor (7), and after being filtered by an oil remover to remove oil, the high-pressure helium is cooled by cold nitrogen at the first outlet end of the cooling device (13) and low-temperature helium flowing back from the third outlet end of the second heat exchange device (20) in the first heat exchange device (10); helium flowing out of the second outlet end of the first heat exchange device (10) enters the second inlet end of the second heat exchange device (20) and is cooled by liquid nitrogen at the third outlet end of the cooling device (13); helium flowing out of the second outlet end of the second heat exchange device (20) enters the second inlet end of the third heat exchange device (30), and after being cooled by low-temperature helium flowing back from the fourth heat exchange device (40), the helium enters the fourth heat exchange device (40) from the second inlet end of the fourth heat exchange device (40) and is cooled by low-temperature helium flowing back from the fifth heat exchange device (50); helium flowing out of the second outlet end of the fourth heat exchange device (40) flows through the first turbo expander (31) for adiabatic expansion refrigeration, the refrigerated helium flows into the sixth heat exchange device (60) from the second inlet end of the sixth heat exchange device (60) and is cooled by low-temperature helium flowing back from the third outlet end of the seventh heat exchange device (70), the cooled helium flows into the seventh heat exchange device (70) from the second outlet end of the sixth heat exchange device (60) and is cooled by low-temperature helium flowing back from the second outlet end of the eighth heat exchange device (80), the helium flowing out of the second outlet end of the seventh heat exchange device (70) is subjected to adiabatic expansion refrigeration through the second turbo expander (32), and is cooled to about 18.5K to serve as a refrigeration working medium. The low-temperature low-pressure helium gas refrigerated by the second turboexpander (32) sequentially passes through the seventh heat exchange device (70), the sixth heat exchange device (60), the fifth heat exchange device (50), the fourth heat exchange device (40), the third heat exchange device (30) and the first heat exchange device (10) in a reverse flow mode from the eighth heat exchange device (80), the reheated helium gas flows out of the cold box (1) from the third outlet end of the first heat exchange device (10), is compressed by the helium gas screw compressor (7) and then enters the first pipeline (21) to be recycled.
When the hydrogen system works, raw material hydrogen is compressed by the hydrogen compressor, enters the first heat exchange device (10) from the first hydrogen pipeline (4), is cooled by cold nitrogen at the first outlet end of the cooling device (13) and low-temperature helium reflowing from the third outlet end of the second heat exchange device (20), flows out of the first outlet end of the first heat exchange device (10), flows into the second heat exchange device (20) from the first inlet end of the second heat exchange device (20), and is cooled by liquid nitrogen at the third outlet end of the cooling device (13); hydrogen flowing out of the first outlet end of the second heat exchange device (20) flows into the first ortho-para hydrogen conversion device (51) for ortho-para hydrogen conversion, and flows into the third heat exchange device (30) from the outlet end of the first ortho-para hydrogen conversion device (51), the hydrogen is cooled by low-temperature helium returning from the third outlet end of the fourth heat exchange device (40) and then enters the first inlet end of the fourth heat exchange device (40), and the hydrogen is cooled by low-temperature helium returning from the third outlet end of the fifth heat exchange device (50); the cooled hydrogen flows into a second ortho-para hydrogen conversion device (52) from a first outlet end of a fourth heat exchange device (40) to carry out ortho-para hydrogen conversion, the hydrogen flowing out from an outlet end of the second ortho-para hydrogen conversion device (52) enters the fourth heat exchange device (40) from a fourth inlet end of the fourth heat exchange device (40) to be cooled again, the hydrogen flowing out from a fourth outlet end of the fourth heat exchange device (40) enters a first inlet end of a fifth heat exchange device (50), is cooled by low-temperature helium flowing back from the sixth heat exchange device (60), flows out from the first outlet end of the fifth heat exchange device (50) to enter a first inlet end of the sixth heat exchange device (60), is cooled by the low-temperature helium flowing back from the seventh heat exchange device (70) to enter a third ortho-para hydrogen conversion device (53), and the converted hydrogen enters the sixth heat exchange device (60) from a fourth inlet end of the sixth heat exchange device (60), after cooling, the fourth outlet end of the sixth heat exchange device (60) enters the first inlet end of the seventh heat exchange device (70) and is cooled by low-temperature helium returning from the eighth heat exchange device (80), the cooled helium enters the eighth heat exchange device (80) from the first inlet end of the eighth heat exchange device (80), the cooled helium is cooled by the low-temperature helium refrigerated by the second turbo expander (32) and then enters the fourth normal-secondary hydrogen conversion device (54) from the first outlet end of the eighth heat exchange device (80), the converted hydrogen enters the eighth heat exchange device (80) from the third outlet end of the eighth heat exchange device (80) and is cooled again and then flows out from the third outlet end of the eighth heat exchange device (80), and liquid nitrogen flowing out of the cold box (1) is stored in the liquid nitrogen dewar (100).
The ortho-para hydrogen conversion system of the utility model improves the hydrogen liquefaction capacity of hydrogen through the cooperation of the cooling medium system, the helium system, the hydrogen system and the helium screw compressor; the purity of the liquefied hydrogen is improved through the filtering and purifying of the first purifier, and meanwhile, the continuous operation time of the system is prolonged, so that the efficiency of hydrogen liquefaction is improved, and the power consumption of the system in operation is reduced; the second purifier and the third purifier are arranged on the first pipeline, so that the purity of helium in the helium system is improved, and the running stability of the helium system is improved; through the utility model discloses a liquid hydrogen that positive-parahydrogen conversion system obtained obtains the liquid hydrogen product that parahydrogen content 95% above, reduces the liquid hydrogen evaporation loss that the conversion of the normal parahydrogen arouses in the transportation. Compared with gaseous hydrogen, the method has the advantages that the amount of transported hydrogen is increased and the transportation cost is reduced under the condition of the same transportation volume.
The utility model discloses a helium turboexpander, operating efficiency is higher than hydrogen turboexpander, and the helium working medium then does not have the corruption to the equipment material. The utility model discloses well refrigeration working medium who adopts is the helium working medium, and the helium working medium is gaseous state all the time under the operating temperature of system to the problem of bringing because heterogeneous expansion has been eliminated. While helium is inert, it is also environmentally safe in the event of a leak.
The above disclosure is only illustrative of the preferred embodiments of the present invention. The preferred embodiments are not intended to be exhaustive or to limit the invention to the precise embodiments disclosed. Obviously, many modifications and variations are possible in light of the above teaching. The embodiments were chosen and described in order to best explain the principles of the invention and its practical application, to thereby enable others skilled in the art to best utilize the invention. The present invention is limited only by the claims and their full scope and equivalents.
Claims (9)
1. The ortho-para hydrogen conversion system is characterized by comprising a cold box (1), wherein a cooling medium system, a hydrogen system, a refrigeration working medium system and a heat exchange system are arranged in the cold box (1); wherein,
the heat exchange system comprises a first heat exchange device (10), a second heat exchange device (20), a third heat exchange device (30), a fourth heat exchange device (40), a fifth heat exchange device (50), a sixth heat exchange device (60), a seventh heat exchange device (70) and an eighth heat exchange device (80);
the cooling medium system comprises a cooling medium inflow pipe (11), a cooling device (13) for cooling the cooling medium and a cooling medium outflow pipe (12), wherein the cooling medium inflow pipe (11) is connected with a first inlet end of the cooling device (13), the cooling medium outflow pipe (12) is connected with a first outlet end of the cooling device (13), and the other end of the cooling medium outflow pipe (12) is connected with a fourth inlet end of the first heat exchange device (10);
the refrigeration working medium system comprises a first pipeline (21), a second pipeline (22) and a compressor (7), the first pipeline (21) is sequentially connected with the first heat exchange device (10), the second heat exchange device (20), the third heat exchange device (30), the fourth heat exchange device (40), the sixth heat exchange device (60) and the seventh heat exchange device (70) in series, and the first pipeline (21) is further connected with a second inlet end of the eighth heat exchange device (80); a second outlet end of the eighth heat exchange device (80) is connected with a second pipeline (22), and the second pipeline (22) is also sequentially connected in series with the seventh heat exchange device (70), the sixth heat exchange device (60), the fifth heat exchange device (50), the fourth heat exchange device (40), the third heat exchange device (30) and the first heat exchange device (10); the second pipeline (22) is connected with the inlet end of the compressor (7) outside the cold box (1), and the outlet end of the compressor (7) is connected with the first pipeline (21); the first pipeline (21) is also provided with at least two turboexpanders (3), including a first turboexpander (31) arranged between the fourth heat exchange device (40) and the sixth heat exchange device (60), and a second turboexpander (32) arranged at the second outlet end of the seventh heat exchange device (70);
the hydrogen system comprises a first hydrogen pipeline (4), and the first hydrogen pipeline (4) is sequentially connected with the first heat exchange device (10), the second heat exchange device (20), the third heat exchange device (30), the fourth heat exchange device (40), the fifth heat exchange device (50), the sixth heat exchange device (60), the seventh heat exchange device (70) and the eighth heat exchange device (80) in series; the first hydrogen pipeline (4) is provided with at least four orthoparahydrogen conversion devices, including a first orthoparahydrogen conversion device (51) arranged between the second heat exchange device (20) and the third heat exchange device (30), a second orthoparahydrogen conversion device (52) arranged at a first outlet end of the fourth heat exchange device (40), a third orthoparahydrogen conversion device (53) arranged at a first outlet end of the sixth heat exchange device (60), and a fourth orthoparahydrogen conversion device (54) arranged at a first outlet end of the eighth heat exchange device (80).
2. An ortho-para hydrogen conversion system according to claim 1 wherein the outlet of said second ortho-para hydrogen conversion means (52) is connected to the fourth inlet of said fourth heat exchange means (40) via said first hydrogen line (4), and the fourth outlet of said fourth heat exchange means (40) is connected to said fifth heat exchange means (50); the outlet end of the third para-hydrogen conversion device (53) is connected with the fourth inlet end of the sixth heat exchange device (60) through the first hydrogen pipeline (4), and the fourth outlet end of the sixth heat exchange device (60) is connected with the seventh heat exchange device (70); the outlet end of the fourth para-hydrogen conversion device (54) is connected with the third inlet end of the eighth heat exchange device (80) through the first hydrogen pipeline (4), and the third outlet end of the eighth heat exchange device (80) is connected to the outside of the cold box (1).
3. An ortho-para hydrogen conversion system according to claim 1, wherein said first ortho-para hydrogen conversion apparatus (51) is disposed in a storage tank (5) for providing a low temperature environment; and a second outlet end of the cooling device (13) is connected with an inlet end of the storage tank (5), and a second inlet end of the cooling device (13) is connected with an outlet end of the storage tank (5).
4. An ortho-para hydrogen conversion system according to claim 1 wherein the third outlet end of said cooling means (13) is further connected to the second inlet end of said second heat exchange means (20), and the second outlet end of said second heat exchange means (20) is connected to the third inlet end of said cooling means (13).
5. An ortho-para hydrogen conversion system according to claim 1, the first pipeline (21) is sequentially connected with a second inlet end of the first heat exchange device (10), a second outlet end of the first heat exchange device (10), a second inlet end of the second heat exchange device (20), a second outlet end of the second heat exchange device (20), a second inlet end of the third heat exchange device (30), a second outlet end of the third heat exchange device (30), a second inlet end of the fourth heat exchange device (40), a second outlet end of the fourth heat exchange device (40), a second inlet end of the sixth heat exchange device (60), a second outlet end of the sixth heat exchange device (60), a second inlet end of the seventh heat exchange device (70), a second outlet end of the seventh heat exchange device (70) and a second inlet end of the eighth heat exchange device (80); the second pipeline (22) is connected in sequence with a second outlet end of the eighth heat exchange device (80), a third inlet end of the seventh heat exchange device (70), a third outlet end of the seventh heat exchange device (70), a third inlet end of the sixth heat exchange device (60), a third outlet end of the sixth heat exchange device (60), a third inlet end of the fifth heat exchange device (50), a third outlet end of the fifth heat exchange device (50), a third inlet end of the fourth heat exchange device (40), a third outlet end of the fourth heat exchange device (40), a third inlet end of the third heat exchange device (30), a third outlet end of the third heat exchange device (30), a third inlet end of the first heat exchange device (10), and a third outlet end of the first heat exchange device (10), and is connected to the outside of the cold box (1) from the third outlet end of the first heat exchange device (10).
6. An ortho-para hydrogen conversion system according to claim 1 wherein the outlet of said compressor (7) is connected to an oil remover, the outlet of said oil remover being connected to said first conduit (21).
7. An ortho-para hydrogen conversion system according to claim 1 wherein said first hydrogen line (4) is provided with at least one first purifier (6.1), said first purifier (6.1) being disposed between said first heat exchange means (10) and said second heat exchange means (20).
8. An n-sec hydrogen conversion system according to claim 1 wherein the first conduit (21) is provided with at least two purifiers, including a second purifier (6.2) disposed between the second heat exchange means (20) and the third heat exchange means (30), and a third purifier (6.3) disposed between the second turboexpander (32) and the eighth heat exchange means (80).
9. An ortho-para hydrogen conversion system according to claim 1 wherein said first heat exchange means (10), said second heat exchange means (20), said third heat exchange means (30), said fourth heat exchange means (40), said fifth heat exchange means (50), said sixth heat exchange means (60), and said seventh heat exchange means (70) and said eighth heat exchange means (80) are all plate and fin heat exchangers.
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| CN113606494A (en) * | 2021-07-29 | 2021-11-05 | 中国科学院合肥物质科学研究院 | Device for producing orthohydrogen and parahydrogen with different components |
| CN114353563A (en) * | 2022-01-10 | 2022-04-15 | 浙江大学 | Temperature-division-area combined type low-temperature hydrogen plate-fin heat exchanger for continuously converting normal hydrogen and parahydrogen |
| WO2022135515A1 (en) * | 2020-12-25 | 2022-06-30 | 江苏国富氢能技术装备股份有限公司 | Hydrogen liquefaction system having ortho-parahydrogen conversion function |
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| CN112557577A (en) * | 2020-10-22 | 2021-03-26 | 合肥综合性国家科学中心能源研究院(安徽省能源实验室) | System for testing dynamic performance of catalytic conversion of para-hydrogen |
| CN112361712A (en) * | 2020-10-30 | 2021-02-12 | 北京航天试验技术研究所 | Hydrogen liquefaction equipment adopting helium refrigeration cycle system |
| WO2022135515A1 (en) * | 2020-12-25 | 2022-06-30 | 江苏国富氢能技术装备股份有限公司 | Hydrogen liquefaction system having ortho-parahydrogen conversion function |
| CN113030367A (en) * | 2021-02-08 | 2021-06-25 | 上海司氢科技有限公司 | Device for testing catalytic performance of catalyst for reaction of para-hydrogen |
| CN113606494A (en) * | 2021-07-29 | 2021-11-05 | 中国科学院合肥物质科学研究院 | Device for producing orthohydrogen and parahydrogen with different components |
| CN114353563A (en) * | 2022-01-10 | 2022-04-15 | 浙江大学 | Temperature-division-area combined type low-temperature hydrogen plate-fin heat exchanger for continuously converting normal hydrogen and parahydrogen |
| CN114353563B (en) * | 2022-01-10 | 2022-10-04 | 浙江大学 | Temperature-division combined type low-temperature hydrogen plate-fin heat exchanger for continuous conversion of normal-secondary hydrogen |
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