CN207797509U - A kind of device producing liquid hydrogen - Google Patents
A kind of device producing liquid hydrogen Download PDFInfo
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- CN207797509U CN207797509U CN201721909668.3U CN201721909668U CN207797509U CN 207797509 U CN207797509 U CN 207797509U CN 201721909668 U CN201721909668 U CN 201721909668U CN 207797509 U CN207797509 U CN 207797509U
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Abstract
The utility model is related to a kind of production liquid hydrogen devices comprising hydrogen gas compressor, refrigeration working medium compressor, the first order~fourth stage heat exchanger, one-stage expansion machine and compound expansion machine and for connecting the feed hydrogen tracheae of above equipment, pressurized hydrogen tracheae, cooled hydrogen pipe, liquid nitrogen pipe, supercharging refrigeration working medium pipe, circularly cooling working medium tube.Compared with prior art, the shortcomings that high-grade temperature section needs hydrogen recycle compressor largely to do work when the utility model overcomes liquefaction of hydrogen, realize different temperatures section, the distribution of different colds reduces the energy consumption of whole device, and device operates steadily, is reliable, is efficient, low energy consumption, the working media of power-equipment is Single Medium, convenient for the maintenance of equipment, equipment fault is reduced, operation control is easily achieved full-automation.
Description
Technical field
The utility model is related to liquefaction of hydrogen fields, and in particular to a kind of to use the device that hydrogen is raw material production liquid hydrogen.
Background technology
Hydrogen is as the ideal energy carrier that can be obtained from number of ways.Hydrogen Energy is generally acknowledged clean energy resource, as low-carbon and
The zero carbon energy is being shown one's talent.The storage and transportation of Hydrogen Energy is the applicable key of hydrogen, liquid hydrogen with the high advantage of its volume energy density,
It will be as the principal mode of mass transit hydrogen.
For hydrogen after overcompression, deep cooling is allowed to become liquid hydrogen to~-250 DEG C or less, and the density of liquid hydrogen is gas under normal pressure
845 times of state hydrogen, the mass density and bulk density of liquid hydrogen are higher.It will be placed in liquid hydrogen storage to special heat-insulation vacuum container
It is transported on truck, locomotive, ship or aircraft.Can meet so larger defeated hydrogen amount and faster, economical liquid hydrogen is transported
It is sent to destination.
The condensing temperature of hydrogen is very low, so hydrogen is only pre-cooling to certain temperature hereinafter, throttling expansion ability again
Generate cold effect.This characteristic will produce the liquefaction process of hydrogen certain difficulty.There are three types of liquid for existing production liquid hydrogen technique
Change cycle, that is, the liquefaction of hydrogen cycle that throttles, the liquefaction of hydrogen cycle with expanding machine and helium refrigeration liquefaction of hydrogen cycle.Helium refrigeration liquefaction of hydrogen follows
Ring is to use helium as refrigeration working medium, provides the cold needed for hydrogen condensation liquefaction by helium refrigeration, which eliminates
The danger of High Pressure Hydrogen is handled, operational security is reliable, but current helium refrigeration system flow sheet equipment complexity, fluctuation of service, energy consumption
Height, and be not easy to carry out daily maintenance.
Utility model content
The utility model is directed to problems of the prior art, provides a kind of using the dress that hydrogen is raw material production liquid hydrogen
It sets, device flow used by the utility model is simple, stable, easy to maintain, low energy consumption.
To achieve the above object, the utility model adopts the following technical solution：
The utility model provides a kind of device producing liquid hydrogen comprising hydrogen gas compressor, refrigeration working medium compressor, first
Grade~fourth stage heat exchanger, one-stage expansion machine and compound expansion machine and corresponding connecting pipe, the connecting pipe include：
Feed hydrogen tracheae, for raw hydrogen to be delivered to hydrogen gas compressor；
Pressurized hydrogen tracheae, the pressurized hydrogen for exporting hydrogen gas compressor are transported through the first order~fourth stage successively
Heat exchanger；
Cooled hydrogen pipe, after by the cooled hydrogen of fourth stage heat exchanger exit via being delivered to after expansion dropping equipment
Continuous container；
Liquid nitrogen pipe, for liquid nitrogen to be delivered to first order heat exchanger to carry out the precooling of pressurized hydrogen；
Be pressurized refrigeration working medium pipe, for by the supercharging refrigeration working medium of refrigeration working medium compressor outlet pass sequentially through the first order~
Compound expansion machine is delivered to after third level heat exchanger；
Circularly cooling working medium tube, the circularly cooling working medium for exporting compound expansion machine pass sequentially through the fourth stage~the first
It is delivered to refrigeration working medium compressor after grade heat exchanger；
Wherein, the supercharging refrigeration working medium pipe setting supercharging refrigeration work between the second level heat exchanger and third level heat exchanger
Matter shunt valve is used to part supercharging refrigeration working medium being delivered to one-stage expansion machine；The outlet setting cycle of one-stage expansion machine
Refrigeration working medium shunt valve is used to converge to the supercharging refrigeration working medium after swell refrigeration the cycle system of fourth stage heat exchanger exit
Cold working medium tube.
In order to optimize above-mentioned apparatus, the technical measures that the utility model is taken further include：
Further, the successive container is gas-liquid separator, and the hydrogen that do not liquefy is arranged in the top of the gas-liquid separator
Liquid hydrogen pipe is arranged in the bottom of pipe, the gas-liquid separator, and the hydrogen pipe that do not liquefy is connected to feed hydrogen tracheae, the liquid hydrogen pipe
It is connected to liquid hydrogen storage tank.
Alternatively, optionally, further, the successive container is gas-liquid separator, is set at the top of the gas-liquid separator
The hydrogen pipe that do not liquefy is set, liquid hydrogen pipe is arranged in the bottom of the gas-liquid separator；The compound expansion machine and fourth stage heat exchanger it
Between circularly cooling working medium tube on level V heat exchanger is set, the hydrogen pipe that do not liquefy is connected to level V heat exchanger with will not
Liquefaction hydrogen is liquefied and converges to the liquid hydrogen pipe, and the liquid hydrogen pipe is connected to liquid hydrogen storage tank.
Further, the equal catalyst filling in the first order~level V heat exchanger, with the mistake being cooled in raw hydrogen
The conversion of n- parahydrogen is carried out at the same time in journey；Alternatively, being respectively provided in the upstream of the first order~level V heat exchanger or downstream n- secondary
Hydrogen converter, the catalyst filling in each converter, to carry out the conversion of n- parahydrogen；Parahydrogen in the wherein described liquid hydrogen product
Content is >=99wt%.
Further, the expansion dropping equipment is throttle valve or hydrogen liquid expander.
Further, the first order~level V heat exchanger, one-stage expansion machine, compound expansion machine, gas-liquid separator with
And expansion dropping equipment is arranged in cold insulated cabinet.
Further, the pipeline being connected to the cold insulated cabinet is all made of flanged joint, the flange and the cold insulated cabinet
Sealing element is respectively provided between tank wall, the sealing element is rubber slab or glass cement.
Further, the cold insulated cabinet loads cold insulation material, preferably pearlife.
Using hydrogen as raw material in the device of production liquid hydrogen of the present invention, raw hydrogen passes through after supercharging
Multi-stage heat exchanger carries out heat exchange with refrigeration working medium, and to realize the precooling of hydrogen and cool down step by step, hydrogen after cooling is expanded
Liquid hydrogen product is obtained after decompression；Wherein, the swell refrigeration process of at least one refrigeration working medium, institute are set between heat exchangers at different levels
It is liquid nitrogen to state pre- cold medium, and the refrigeration working medium is selected from least one of hydrogen, helium, ne-He mixture.The liquid nitrogen is
Normal pressure liquid nitrogen or negative pressure liquid nitrogen, preferably normal pressure liquid nitrogen.
The process operation parameter of each equipment is as follows：The pressure of the pressurized hydrogen of hydrogen gas compressor outlet is 3.5~4.5MPa,
The pressure of the supercharging refrigeration working medium of refrigeration working medium compressor outlet is 1.0~1.5MPa；Pressurized hydrogen after level-one precooling and increasing
It is 78~82K to press the temperature of refrigeration working medium, and two level pressurized hydrogen after cooling and the temperature for being pressurized refrigeration working medium are 58~62K,
28~34K of three-level pressurized hydrogen after cooling and the temperature of supercharging refrigeration working medium, the temperature of level Four pressurized hydrogen after cooling
For 19~23K；The temperature of the supercharging refrigeration working medium of one-stage expansion machine outlet is 31~35K, the cycle system of compound expansion machine outlet
The temperature of cold working medium is 17~21K；It is liquid hydrogen that pressurized hydrogen has 90~97vl% liquefaction after expansion is depressured.
Compared with prior art, the utility model has the advantages that：
The utility model is pre-chilled raw hydrogen using liquid nitrogen, is using the closed-loop refrigeration circulatory system of refrigeration working medium
Raw hydrogen provides cold, and high-grade temperature section needs hydrogen recycle compressor largely to do work scarce when overcoming liquefaction of hydrogen
The condensation of point, hydrogen mainly provides cold by the expansion of hydrogen after cooling itself decompression；
The utility model using expanding machine carry out refrigeration working medium swell refrigeration, by this class expansion mechanism at helium freeze system
System, operates steadily, is reliable, is efficient, low energy consumption, and operation control is easily achieved full-automation；Production described in the utility model
The method of the liquid hydrogen technique realizes different temperatures section, and the distribution of different colds reduces the energy consumption of whole device；
The utility model adds catalysis to carry out n- parahydrogen conversion in the liquefaction process of hydrogen so that final system
The content of parahydrogen is >=99wt% in standby liquid hydrogen product, and the quality and its storage stability of product has been effectively ensured in this；
The utility model relates generally to hydrogen refrigeration system and helium refrigeration cycle, and two systems are relatively independent, flow letter
Single, strong operability；And the power-equipment that the present apparatus uses is less, and the working media of power-equipment is Single Medium, is convenient for
The maintenance of equipment reduces equipment fault.
Description of the drawings
Fig. 1 is a kind of using the flow diagram that hydrogen is raw material production liquid hydrogen in one embodiment of the utility model；
Reference numeral in figure is as follows：
Hydrogen gas compressor 101, refrigeration working medium compressor 102, first order heat exchanger 103, second level heat exchanger 104, third
It is grade heat exchanger 105, fourth stage heat exchanger 106, level V heat exchanger 107, one-stage expansion machine 108, compound expansion machine 109, follow-up
Equipment 110, expansion dropping equipment 111, cold insulated cabinet 112；
Feed hydrogen tracheae 1, pressurized hydrogen tracheae 2, cooled hydrogen pipe 3, liquid nitrogen pipe 4, supercharging refrigeration working medium pipe 5, circularly cooling
Working medium tube 6, supercharging refrigeration working medium shunt valve 7, circularly cooling working medium shunt valve 8, the hydrogen pipe 9 that do not liquefy, liquid hydrogen pipe 10.
Specific implementation mode
The utility model provides a kind of method producing liquid hydrogen, and this method is using hydrogen as raw material, and raw hydrogen is through increasing
After pressure, heat exchange is carried out by multi-stage heat exchanger and refrigeration working medium, to realize the precooling of hydrogen and cool down step by step, hydrogen after cooling
Liquid hydrogen product is obtained after the expanded decompression of gas；Wherein, the swell refrigeration of at least one refrigeration working medium is set between heat exchangers at different levels
Process, the pre- cold medium are liquid nitrogen, and the refrigeration working medium is selected from least one of hydrogen, helium, ne-He mixture, this reality
A kind of device applied to the production liquid hydrogen in the above method is also provided with novel.
With reference to the accompanying drawings and examples, specific embodiment of the present utility model is further described.Implement below
Example is only used for clearly illustrating the technical solution of the utility model, and the protection model of the utility model cannot be limited with this
It encloses.
Embodiment 1
The present embodiment is a preferred versions using the device that hydrogen is raw material production liquid hydrogen.
As shown in Figure 1, in this embodiment, the refrigeration working medium used is helium.Raw hydrogen passes through 1 quilt of feed hydrogen tracheae
It is delivered to hydrogen gas compressor 101, is sent into cold insulated cabinet 112 after being compressed into 4MPa；Cycle helium passes through circularly cooling working medium
Pipe 6 is transported to refrigeration working medium compressor 102, is sent into cold insulated cabinet 112 after being compressed into 1.3MPa.
In first order heat exchanger 103, pressurized hydrogen and refrigeration working medium compressor 102 that hydrogen gas compressor 101 exports go out
Mouthful supercharging helium with from liquid nitrogen pipe 4 normal pressure liquid nitrogen and from second level heat exchanger 104 export cycle low-temperature helium into
Row heat exchange is pre-chilled with realizing pressurized hydrogen and being pressurized the level-one of helium, is both cooled to about 80K in advance.It is normal in liquid nitrogen pipe 4
Cold insulated cabinet 112 is sent out after hydraulic fluid nitrogen re-heat to room temperature.The cycle low-temperature helium exported from second level heat exchanger 104 is arrived by re-heat
It is sent after room temperature to the entrance of refrigeration working medium compressor 102.
In second level heat exchanger 104, the pressurized hydrogen and supercharging helium after level-one precooling are by from third level heat exchanger
The further cooling (two level cooling) of the cycle low-temperature helium of 105 outlets, two level pressurized hydrogen after cooling and supercharging helium temperature
About 60K.Two level supercharging helium after cooling is divided into two-way, and shunt ratio is by Flux Valve Control, wherein passing through all the way
Third level heat exchanger 105 is entered by supercharging refrigeration working medium pipe 5, another way is swollen into level-one by being pressurized refrigeration working medium shunt valve 7
Swollen machine 108 carries out swell refrigeration, and the helium temperature after expansion is about 33K, and the helium after expansion is bypassed by circularly cooling working medium
Pipe 8 converges in the circularly cooling working medium tube 6 of the outlet of fourth stage heat exchanger 106；
In third level heat exchanger 105, two level pressurized hydrogen after cooling and supercharging helium are by from fourth stage heat exchanger
The further cooling (three-level cooling) of the cycle low-temperature helium of 106 outlets, three-level pressurized hydrogen after cooling and the temperature for being pressurized helium
The 30K of degree.Supercharging helium after cooling enters 109 progress swell refrigeration of compound expansion machine, expansion by being pressurized refrigeration working medium pipe 5
Helium temperature afterwards is about 19K, and level V heat exchanger is connected to via circularly cooling working medium tube 6 as circularly cooling working medium
107；
In fourth stage heat exchanger 106, work that three-level pressurized hydrogen after cooling is exported from level V heat exchanger 107
For the low-temperature helium further cooling (level Four cooling) of circularly cooling working medium.The temperature of pressurized hydrogen after cooling is about 21K；
The pressurized hydrogen that fourth stage heat exchanger 106 exports (is saved via the expansion dropping equipment 111 on cooled hydrogen pipe 3
Flow valve) after expansion decompression, about the hydrogen of 95vl% becomes liquid hydrogen in pressurized hydrogen, and the fluid after liquefaction is admitted to gas-liquid point
From device 110, the not liquefied hydrogen of Base top contact is entered by the hydrogen pipe 9 that do not liquefy in level V heat exchanger 107, swollen with two level
The cycle low-temperature helium that swollen machine 109 exports exchanges heat, and the hydrogen that do not liquefy is cooled to liquid hydrogen, and from 110 bottom of gas-liquid separator
The liquid hydrogen that the liquid hydrogen pipe 10 in portion is drawn is sent out cold insulated cabinet 112 as product after converging and is sent to liquid hydrogen storage tank.
Low-temperature circulating helium after heat exchanger 107,106 re-heats, converge by the low-temperature helium exported with one-stage expansion machine 8
Afterwards, it is sent into heat exchanger 105,104,103 and continues re-heat, until room temperature.
In this embodiment, the catalyst filling in the hydrogen heat exchanger channels of heat exchanger 103~107 so that feed hydrogen exists
N- secondary conversion is carried out at the same time in cooled process, to ensure the parahydrogen containing 99wt% or more in final products.
In this embodiment, the first order~level V heat exchanger 103~107, one-stage expansion machine 108, compound expansion machine
109, gas-liquid separator 110 and expansion dropping equipment 111 are arranged in cold insulated cabinet 112, are connected to the cold insulated cabinet 112
Pipeline is all made of flanged joint, rubber slab is respectively provided between the flange and the tank wall of the cold insulated cabinet 112, and in the cold insulated cabinet
Cold insulation material pearlife is loaded in 112.
Embodiment 2
The present embodiment is the alternative embodiment of embodiment 1, and there are following differences with the structure of embodiment 1：Do not show in figure
Go out, in this embodiment, the refrigeration working medium used is ne-He mixture, and the liquid nitrogen used is negative pressure liquid nitrogen.The present embodiment is not
Level V heat exchanger is set.Three-level pressurized hydrogen after cooling enters fourth stage heat exchanger, and exports from compound expansion machine
Circularly cooling working medium exchanges heat, and level Four pressurized hydrogen after cooling is after the expansion decompression of hydrogen liquid expander into gas-liquid point
From device, the hydrogen cycle that do not liquefy of gas-liquid separator top exit converges to raw hydrogen, the liquid of gas-liquid separator outlet at bottom
Hydrogen is sent as product to liquid hydrogen storage tank, to obtain liquid hydrogen product.
N- parahydrogen converter is set in the upstream of heat exchangers at different levels or downstream in embodiment, is filled in each converter
Catalyst, to carry out the conversion of n- parahydrogen, to ensure the parahydrogen containing 99wt% or more in final products.
In the present embodiment, the pressure of the pressurized hydrogen of hydrogen gas compressor outlet is 3.8MPa, and refrigeration working medium compressor goes out
The pressure of the supercharging refrigeration working medium of mouth is 1.2MPa；The temperature of pressurized hydrogen and supercharging refrigeration working medium after level-one precooling is 78K,
Two level pressurized hydrogen after cooling and the temperature for being pressurized refrigeration working medium are 58K, three-level pressurized hydrogen after cooling and supercharging refrigeration
The temperature of the 28K of the temperature of working medium, level Four pressurized hydrogen after cooling are 19K；The supercharging refrigeration working medium of one-stage expansion machine outlet
Temperature be 31K, compound expansion machine outlet circularly cooling working medium temperature be 17K；Pressurized hydrogen has after expansion is depressured
93vl% liquefaction is liquid hydrogen.
By above-described embodiment it is found that hydrogen is pre-chilled using normal pressure liquid nitrogen or negative pressure liquid nitrogen for the utility model, hydrogen liquid
Change uses hydrogen refrigeration cycle, helium refrigeration or using ne-He mixture as the cycle of refrigeration working medium, and final stage expansion is using throttling
Valve expansion either hydrogen liquid expander, and the utility model is provided with expanding machine, for producing~40K and cold when~20K
Amount；The utility model is also provided with several n- parahydrogen converters during liquefied, and the design of above-mentioned flow overcomes hydrogen
The shortcomings that high-grade temperature section needs hydrogen recycle compressor largely to do work when liquefaction operates steadily, is reliable, is efficient, energy consumption
Low, operation control is easily achieved full-automation, realizes different temperatures section, the distribution of different colds reduces whole device
Energy consumption；The quality and its storage stability of product has been effectively ensured in n- parahydrogen conversion；And the present apparatus use power-equipment compared with
It is few, and the medium of power-equipment work is Single Medium, is convenient for the maintenance of equipment, reduces equipment fault.
Specific embodiment of the utility model is described in detail above, but it is intended only as example, this practicality is new
Type is not restricted to particular embodiments described above.To those skilled in the art, any that the utility model is carried out
Equivalent modifications and substitute also all among the scope of the utility model.Therefore, in the spirit and model for not departing from the utility model
Impartial conversion and modification made by under enclosing, should all cover in the scope of the utility model.
Claims (7)
1. a kind of device producing liquid hydrogen, which is characterized in that including hydrogen gas compressor (101), refrigeration working medium compressor (102),
The first order~fourth stage heat exchanger (103~106), one-stage expansion machine (108) and compound expansion machine (109) and corresponding connection
Pipeline, the connecting pipe include：
Feed hydrogen tracheae (1), for raw hydrogen to be delivered to hydrogen gas compressor (101)；
Pressurized hydrogen tracheae (2), for the pressurized hydrogen that hydrogen gas compressor (101) exports to be transported through the first order~the successively
Level Four heat exchanger (103~106)；
Cooled hydrogen pipe (3) is used for the cooled hydrogen of fourth stage heat exchanger exit (106) via expansion dropping equipment (111)
After be delivered to successive container (110)；
Liquid nitrogen pipe (4), for liquid nitrogen to be delivered to first order heat exchanger (103) to carry out the precooling of pressurized hydrogen；
It is pressurized refrigeration working medium pipe (5), for the supercharging refrigeration working medium that refrigeration working medium compressor (102) exports to be passed sequentially through first
Compound expansion machine (109) is delivered to after grade~third level heat exchanger (103~105)；
Circularly cooling working medium tube (6), for by the circularly cooling working medium that compound expansion machine (109) exports pass sequentially through the fourth stage~
Refrigeration working medium compressor (102) is delivered to after first order heat exchanger (106~103)；
Wherein, supercharging refrigeration working medium pipe (5) setting between the second level heat exchanger (104) and third level heat exchanger (105)
It is pressurized refrigeration working medium shunt valve (7), is used to part supercharging refrigeration working medium being delivered to one-stage expansion machine (108)；Level-one is swollen
The outlet setting circularly cooling working medium shunt valve (8) of swollen machine (108), is used to converge the supercharging refrigeration working medium after swell refrigeration
The circularly cooling working medium tube (6) exported to fourth stage heat exchanger (106).
2. a kind of device producing liquid hydrogen according to claim 1, which is characterized in that the successive container (110) is gas
The hydrogen pipe (9) that do not liquefy is arranged in the top of liquid/gas separator, the gas-liquid separator, and liquid hydrogen is arranged in the bottom of the gas-liquid separator
It manages (10)；Is arranged in circularly cooling working medium tube (6) between the compound expansion machine (109) and fourth stage heat exchanger (103)
Pyatyi heat exchanger (107), the hydrogen pipe (9) that do not liquefy are connected to level V heat exchanger and are liquefied simultaneously with the hydrogen that will not liquefy
The liquid hydrogen pipe (10) is converged to, the liquid hydrogen pipe (10) is connected to liquid hydrogen storage tank.
3. according to a kind of device producing liquid hydrogen according to any one of claims 1 to 2, which is characterized in that the first order~
Equal catalyst filling in level V heat exchanger (103~107), it is n- secondary to be carried out at the same time during raw hydrogen is cooled
The conversion of hydrogen；Alternatively, n- parahydrogen converter is set in the upstream of the first order~level V heat exchanger (103~107) or downstream,
The catalyst filling in each converter, to carry out the conversion of n- parahydrogen.
4. a kind of device producing liquid hydrogen according to claim 1, which is characterized in that the expansion dropping equipment (111)
For throttle valve or hydrogen liquid expander.
5. according to a kind of device producing liquid hydrogen according to any one of claims 1 to 2, which is characterized in that the first order
~level V heat exchanger (103~107), one-stage expansion machine (108), compound expansion machine (109), gas-liquid separator (110) and
Expansion dropping equipment (111) is arranged in cold insulated cabinet (112).
6. a kind of device producing liquid hydrogen according to claim 5, which is characterized in that be connected to the cold insulated cabinet (112)
Pipeline be all made of flanged joint, be respectively provided with sealing element between the flange and the tank wall of the cold insulated cabinet (112).
7. a kind of device producing liquid hydrogen according to claim 5, which is characterized in that filling in the cold insulated cabinet (112)
Cold insulation material.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201721909668.3U CN207797509U (en) | 2017-12-29 | 2017-12-29 | A kind of device producing liquid hydrogen |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201721909668.3U CN207797509U (en) | 2017-12-29 | 2017-12-29 | A kind of device producing liquid hydrogen |
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| CN207797509U true CN207797509U (en) | 2018-08-31 |
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ID=63277115
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108036582A (en) * | 2017-12-29 | 2018-05-15 | 上海启元空分技术发展股份有限公司 | A kind of method and its device for producing liquid hydrogen |
| CN111412695A (en) * | 2020-03-25 | 2020-07-14 | 西安交通大学 | Super supercooled liquid oxygen acquisition system based on liquid oxygen and liquid nitrogen mixing and vacuumizing |
| CN111692836A (en) * | 2019-03-12 | 2020-09-22 | 有进超低温(株) | Hydrogen liquefaction apparatus using cold energy of liquefied natural gas |
| 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 |
| CN114543441A (en) * | 2022-02-21 | 2022-05-27 | 杭州中泰深冷技术股份有限公司 | Hydrogen liquefaction system and method for helium expansion combined mixed refrigerant refrigeration |
| CN114543442A (en) * | 2022-02-21 | 2022-05-27 | 杭州中泰深冷技术股份有限公司 | Hydrogen liquefaction system and method |
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2017
- 2017-12-29 CN CN201721909668.3U patent/CN207797509U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108036582A (en) * | 2017-12-29 | 2018-05-15 | 上海启元空分技术发展股份有限公司 | A kind of method and its device for producing liquid hydrogen |
| CN111692836A (en) * | 2019-03-12 | 2020-09-22 | 有进超低温(株) | Hydrogen liquefaction apparatus using cold energy of liquefied natural gas |
| CN111412695A (en) * | 2020-03-25 | 2020-07-14 | 西安交通大学 | Super supercooled liquid oxygen acquisition system based on liquid oxygen and liquid nitrogen mixing and vacuumizing |
| 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 |
| CN114543441A (en) * | 2022-02-21 | 2022-05-27 | 杭州中泰深冷技术股份有限公司 | Hydrogen liquefaction system and method for helium expansion combined mixed refrigerant refrigeration |
| CN114543442A (en) * | 2022-02-21 | 2022-05-27 | 杭州中泰深冷技术股份有限公司 | Hydrogen liquefaction system and method |
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| TR01 | Transfer of patent right |
Effective date of registration: 20210519 Address after: 201800 rooms 202 and 204, building 3, 150 Heyu Road, Jiading District, Shanghai Patentee after: SHANGHAI QIYUAN GAS DEVELOPMENT Co.,Ltd. Address before: 201800 150 Heyu Road, Jiading District, Shanghai Patentee before: SHANGHAI QIYUAN AIR SEPARATE TECHNOLOGY DEVELOPMENT Co.,Ltd. |
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