CN217875296U - Cascade type liquid hydrogen hydrogenation station cold energy recovery system - Google Patents
Cascade type liquid hydrogen hydrogenation station cold energy recovery system Download PDFInfo
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- CN217875296U CN217875296U CN202221310717.2U CN202221310717U CN217875296U CN 217875296 U CN217875296 U CN 217875296U CN 202221310717 U CN202221310717 U CN 202221310717U CN 217875296 U CN217875296 U CN 217875296U
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- 239000001257 hydrogen Substances 0.000 title claims abstract description 212
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 212
- 239000007788 liquid Substances 0.000 title claims abstract description 147
- 238000011084 recovery Methods 0.000 title claims abstract description 51
- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 43
- 125000004435 hydrogen atom Chemical class [H]* 0.000 title 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 174
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 88
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 77
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims abstract description 50
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 44
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 42
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 42
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000000034 method Methods 0.000 claims description 29
- 230000008569 process Effects 0.000 claims description 23
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 11
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 7
- 125000003827 glycol group Chemical group 0.000 claims description 3
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims description 2
- 238000001816 cooling Methods 0.000 abstract description 22
- 238000002309 gasification Methods 0.000 abstract description 22
- 239000012530 fluid Substances 0.000 description 7
- 239000006200 vaporizer Substances 0.000 description 6
- 238000004064 recycling Methods 0.000 description 5
- 238000005057 refrigeration Methods 0.000 description 5
- 235000011089 carbon dioxide Nutrition 0.000 description 4
- 238000010276 construction Methods 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 230000008676 import Effects 0.000 description 4
- 238000007710 freezing Methods 0.000 description 3
- 230000008014 freezing Effects 0.000 description 3
- 230000008023 solidification Effects 0.000 description 3
- 238000007711 solidification Methods 0.000 description 3
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- KPAMAAOTLJSEAR-UHFFFAOYSA-N [N].O=C=O Chemical compound [N].O=C=O KPAMAAOTLJSEAR-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/32—Hydrogen storage
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- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
The utility model relates to a cold volume recovery system in tandem type liquid hydrogen hydrogenation station, cold volume recovery system in tandem type liquid hydrogen hydrogenation station includes that the equipartition is arranged in a plurality of tee bend structures and a plurality of heat exchangers in the closed cold box, still includes hydrogen flow path and a plurality of working medium flow path, the utility model discloses select nitrogen, carbon dioxide, ethylene glycol solution, water etc. to retrieve and cold-storage working medium as the cold energy, realize the recovery of cold energy among the liquid hydrogen gasification according to temperature gradient cascade type ground to can carry out effective cold energy and recycle, avoid the problem of liquid hydrogen in air cooling, water-cooling gasification, improve the economic nature in liquid hydrogen hydrogenation station.
Description
Technical Field
The utility model relates to a cold volume recovery technical field of liquid hydrogen especially relates to a cold volume recovery system of tandem type liquid hydrogen hydrogenation station.
Background
The high hydrogen storage density of liquid hydrogen is one of the development trends of hydrogen stations to store hydrogen in the form of liquid hydrogen. Meanwhile, the hydrogen energy source vehicle will also be developed toward two routes of a high-pressure hydrogen vehicle carrying a high-pressure hydrogen cylinder and a liquid hydrogen vehicle carrying a liquid hydrogen cylinder. The liquid hydrogen in the hydrogen filling station can be directly filled into liquid hydrogen vehicles, and can also be heated, gasified and compressed for high-pressure hydrogen vehicles. In the process of temperature rise and gasification, liquid hydrogen has a large amount of cold energy release at deep low temperature (20K). On one hand, the liquid hydrogen temperature is lower than the boiling point and the freezing point of most fluids, and the conventional cooling method, such as a vaporizer using air and water as working media, needs larger working medium flow and vaporizer area, and needs continuous economic cost investment to avoid the surface of the vaporizer from frosting. On the other hand, the cold energy is reasonably recycled, and the economical efficiency of the liquid hydrogen refueling station is inevitably improved. Taking 2.5Mpa as an example, the cooling capacity of liquid hydrogen for heating from 25K to 300K is as high as: 4296kj/kg. However, the design of the existing vaporizer is difficult and consumes additional energy, and at present, no system or method capable of effectively recycling and utilizing the cold energy in the liquid hydrogen gasification process of the liquid hydrogen refueling station exists, so that the cold energy in the liquid hydrogen gasification process of the liquid hydrogen refueling station is seriously wasted.
SUMMERY OF THE UTILITY MODEL
Based on this, the utility model aims at providing a cold volume recovery system of tandem type liquid hydrogen hydrogenation station chooses for use nitrogen, carbon dioxide, ethylene glycol, water etc. to retrieve and the cold-storage working medium for cold energy, realizes the recovery and the recycle of cold energy among the liquid hydrogen gasification, has avoided the problem in air cooling, water-cooling gasification, improves liquid hydrogen hydrogenation station economic nature.
The utility model provides a cold energy recovery system of a cascade liquid hydrogen hydrogenation station, which comprises a plurality of tee structures and a plurality of heat exchangers which are uniformly arranged in a closed cold box, wherein the cold energy recovery system of the cascade liquid hydrogen hydrogenation station comprises a hydrogen flow path and a plurality of working medium flow paths, the hydrogen flow path is connected with the tee structures and the heat exchangers and is used for supplying liquid hydrogen to carry out a multi-stage heat exchange process; the flow direction of the working medium flow path is opposite to that of the hydrogen flow path, and the working medium flow path is connected with one or more heat exchangers and used for realizing the heat exchange process of the working medium by utilizing the cold energy released by the liquid hydrogen in the multistage heat exchange process, so that a corresponding working medium product is obtained.
In an embodiment of the present invention, the cooling capacity recycling system of the cascade type liquid hydrogen hydrogenation station includes a first tee structure, a second tee structure, a first heat exchanger, a second heat exchanger, a third heat exchanger, a throttle valve, a liquid hydrogen interface, a first working medium interface, a second working medium interface, a third working medium interface, a first interface, a second interface, and a third interface; the plurality of working medium flow paths comprise a first working medium flow path, a second working medium flow path and a third working medium flow path;
the hydrogen flow path is sequentially connected with a liquid hydrogen interface, the first three-way structure, the first heat exchanger, the second three-way structure, the second heat exchanger, the third heat exchanger and a hydrogen interface, wherein liquid hydrogen enters the hydrogen flow path to form hydrogen after a multi-stage heat exchange process is carried out, and the hydrogen is recycled through the hydrogen interface;
the first working medium flow path is sequentially connected with a first working medium interface, the third heat exchanger, the second heat exchanger, the first heat exchanger, a throttle valve and a first interface, wherein a first working medium product is obtained after the first working medium enters the first working medium flow path for heat exchange, and the first working medium product is recycled through the first interface;
the second working medium flow path is sequentially connected with the second working medium interface, the third heat exchanger, the second heat exchanger and the second interface, wherein a second working medium product is obtained after the second working medium enters the second working medium flow path for heat exchange, and the second working medium product is recycled through the second interface;
the third working medium flow path is sequentially connected with the third working medium interface, the third heat exchanger and the third interface, wherein a third working medium product is obtained after the third working medium enters the third working medium flow path for a heat exchange process, and the third working medium product is recycled through the third interface.
The utility model discloses an in the embodiment, first three-way valve has first import, second import and first export, the second three-way valve has third import, second export and third export, wherein cascade-type liquid hydrogen hydrogenation station cold volume recovery system still includes the hydrogen flow path that flows backwards, the hydrogen flow path that flows backwards connects gradually the second export of second three-way valve with the first import of first three-way valve for to the hydrogen flow path lets in partial hydrogen that flows backwards, improves hydrogen temperature in the hydrogen flow path avoids leading to working medium solidification to block up the heat exchanger runner because the liquid hydrogen temperature is less than the working medium freezing point.
The utility model discloses an in the embodiment, first heat exchanger be two strand flows the heat exchanger the second heat exchanger be three strand flows the heat exchanger the third heat exchanger is four strand flows the heat exchanger.
In an embodiment of the present invention, the first working medium is nitrogen, the first working medium interface is connected to the nitrogen gas cylinder group, and the first interface is connected to the liquid nitrogen storage tank; the second working medium is carbon dioxide, the second working medium interface is connected to the carbon dioxide gas cylinder group, and the second interface is connected to the liquid carbon dioxide storage tank or the ice making machine; the third working medium is glycol or water, the third working medium interface is connected to the high-temperature solution tank, and the third interface is connected to the low-temperature solution tank.
The utility model discloses an in the embodiment, the pressure of the first working medium of first working medium flow path is greater than or equal to 2bara, the pressure of the second working medium of second working medium flow path is greater than or equal to 6bara, the pressure of the third working medium of third working medium flow path > 1bara.
The utility model discloses on the other hand still provides a cold volume recovery method of tandem type liquid hydrogen hydrogenation station, including the step:
s1, introducing liquid hydrogen into a hydrogen flow path, wherein the liquid hydrogen flows through a first three-way structure, is mixed with hydrogen flowing back into the first three-way structure and then sequentially flows through a first heat exchanger, a second three-way structure, a second heat exchanger and a third heat exchanger to form hydrogen, and the hydrogen is discharged through a hydrogen interface;
s2, introducing a first working medium into a first working medium flow path, wherein the first working medium flows through a third heat exchanger, a second heat exchanger, a first heat exchanger and a throttle valve in sequence to obtain a first working medium product, and the first working medium product is discharged through a first interface;
s3, introducing a second working medium into a second working medium flow path, wherein the second working medium flows through a third heat exchanger and a second heat exchanger in sequence to obtain a second working medium product, and the second working medium product is discharged through a second interface;
and S4, introducing a third working medium into a third working medium flow path, wherein a third working medium product is obtained after the third working medium flows through a third heat exchanger, and the third working medium product is discharged through a third interface.
The utility model discloses an in the embodiment, first heat exchanger be two strand flows the heat exchanger the second heat exchanger be three strand flows the heat exchanger the third heat exchanger is four strand flows the heat exchanger.
The utility model discloses an in the embodiment, in step S2, will first working medium interface connection is in nitrogen gas cylinder group to organize via nitrogen gas cylinder to first working medium flow path lets in nitrogen gas, and will first interface connection is in the liquid nitrogen storage tank, in order to retrieve the liquid nitrogen.
In an embodiment of the present invention, in step S3, the second working medium interface is connected to the carbon dioxide gas cylinder set, so that the carbon dioxide gas cylinder set feeds carbon dioxide into the second working medium flow path, and the second interface is connected to the liquid carbon dioxide storage tank or the ice maker to recover the liquid carbon dioxide.
In an embodiment of the present invention, in step S4, the third working medium interface is connected to the high temperature solution tank, so that the third working medium flow path is connected to the ethylene glycol or water via the high temperature solution tank, and the third interface is connected to the low temperature solution tank to recover the ethylene glycol solution or water.
In an embodiment of the present invention, in step S2, the pressure of the first working medium introduced into the first working medium flow path is greater than or equal to 2bara; in the step S3, the pressure of the second working medium introduced into the second working medium flow path is more than or equal to 6bara; in step S4, the pressure of the third working medium introduced into the third working medium flow path is more than 1bara.
The utility model discloses cold energy is extravagant in the gasification process to liquid hydrogen, the degree of difficulty exists in the vaporizer design, and the problem of extra power consumption, multiple application scene according to liquid hydrogen cold energy, the gradient utilization of hydrogen cold energy, the construction cost, many-sided such as cold energy recovery is recycled, a cascade type liquid hydrogen hydrogenation station cold volume recovery system is proposed, choose for use nitrogen, carbon dioxide, ethylene glycol solution, water etc. are cold energy recovery and cold-storage working medium, realize the recovery of liquid hydrogen gasification liquid hydrogen cold energy, and can carry out effective cold energy and recycle, avoided at the air cooling, the problem in the water-cooling gasification process, the economic nature at liquid hydrogen hydrogenation station has been improved.
The utility model discloses a cold volume recovery system in cascade-type liquid hydrogen hydrogenation station can retrieve produced cold energy in the liquid hydrogen gasification process in liquid hydrogen hydrogenation station according to temperature gradient cascade-type ground, need not the input of nitrogen gas, carbon dioxide compressor and corresponding place and electric energy moreover, and overall structure is simple, with low costs, cold volume recovery efficiency is high, has extensive application prospect.
Further objects and advantages of the invention will be fully apparent from the ensuing description and drawings.
Drawings
Fig. 1 is a schematic structural diagram of a refrigeration recovery system of a cascade-type liquid hydrogen hydrogenation station according to a preferred embodiment of the present invention, wherein the direction of the arrow is a fluid flow direction.
The reference numbers illustrate: a cascade liquid hydrogen hydrogenation station cold energy recovery system 100; closing the cold box 10; a first three-way structure 21; a first inlet 211; a second inlet 212; a first outlet 213; a second tee structure 22; a third inlet 221; a second outlet 222; a third outlet 223; a first heat exchanger 31; a second heat exchanger 32; a third heat exchanger 33; a throttle valve 34; a liquid hydrogen interface 41; a hydrogen gas interface 42; a first working medium interface 43; second working medium interface 44; a third working medium interface 45; a first interface 46; a second interface 47; a third interface 48; a first working medium flow path 51; second working fluid flow path 52; third working fluid flow path 53; a return hydrogen gas flow path 54; a hydrogen flow path 55.
Detailed Description
The following description is presented to disclose the invention so as to enable any person skilled in the art to practice the invention. The preferred embodiments in the following description are given by way of example only, and other obvious variations will occur to those skilled in the art. The basic principles of the invention, as defined in the following description, may be applied to other embodiments, variations, modifications, equivalents and other technical solutions without departing from the spirit and scope of the invention.
It will be understood by those skilled in the art that in the present disclosure, the terms "vertical," "horizontal," "up," "down," "front," "back," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in the orientation or positional relationship indicated in the drawings for ease of description and simplicity of description, and do not indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and thus, are not to be considered limiting.
It is understood that the terms "a" and "an" should be interpreted as meaning "at least one" or "one or more," i.e., that a quantity of one element may be one in one embodiment, while a quantity of another element may be plural in other embodiments, and the terms "a" and "an" should not be interpreted as limiting the quantity.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; may be mechanically connected, may be electrically connected or may be in communication with each other; either directly or indirectly through intervening media, either internally or in any other relationship. The specific meaning of the above terms in the present invention can be understood according to specific situations by those of ordinary skill in the art.
As shown in fig. 1, a specific structure of a refrigeration recovery system 100 of a cascade liquid hydrogen refueling station provided by the present invention is illustrated. Specifically, the refrigeration capacity recovery system 100 of the cascade liquid hydrogen station comprises a plurality of three-way structures and a plurality of heat exchangers which are uniformly distributed in the closed cold box 10, and the refrigeration capacity recovery system 100 of the cascade liquid hydrogen station comprises a hydrogen flow path 55 and a plurality of working medium flow paths, wherein the hydrogen flow path 55 is connected to the plurality of three-way structures and the plurality of heat exchangers and is used for supplying liquid hydrogen to perform a multi-stage heat exchange process; the flow direction of the working medium flow path is opposite to that of the hydrogen flow path 55, and the working medium flow path is connected with one or more heat exchangers and used for realizing the heat exchange process of the working medium by utilizing the cold energy released by the liquid hydrogen in the multistage heat exchange process, so that a corresponding working medium product is obtained.
More specifically, the cascade type liquid hydrogen hydrogenation station cold energy recovery system 100 adopts two tee structures, three heat exchangers and a throttle valve 34, the whole structure is uniformly distributed in the closed cold box 10 (vacuum container), and the inlets and outlets of four working mediums pass through the closed cold box 10 to be connected with the outside.
The cascade type liquid hydrogen hydrogenation station cold energy recovery system 100 comprises a first tee joint structure 21, a second tee joint structure 22, a first heat exchanger 31, a second heat exchanger 32, a third heat exchanger 33, a throttle valve 34, a liquid hydrogen interface 41, a hydrogen interface 42, a first working medium interface 43, a second working medium interface 44, a third working medium interface 45, a first interface 46, a second interface 47 and a third interface 48; the working medium flow paths comprise a first working medium flow path 51, a second working medium flow path 52 and a third working medium flow path 53;
the hydrogen flow path 55 is sequentially connected to a liquid hydrogen interface 41, the first three-way structure 21, the first heat exchanger 31, the second three-way structure 22, the second heat exchanger 32, the third heat exchanger 33 and a hydrogen interface 42, wherein liquid hydrogen enters the hydrogen flow path 55 to perform a multi-stage heat exchange process to form hydrogen gas, and the hydrogen gas is recycled through the hydrogen interface 42;
the first working medium flow path 51 is sequentially connected with a first working medium interface 43, the third heat exchanger 33, the second heat exchanger 32, the first heat exchanger 31, the throttle valve 34 and the first interface 46, wherein a first working medium product is obtained after the first working medium enters the first working medium flow path 51 for a heat exchange process, and the first working medium product is recycled through the first interface 46;
the second working medium flow path 52 is sequentially connected with the second working medium interface 44, the third heat exchanger 33, the second heat exchanger 32 and the second interface 47, wherein a second working medium product is obtained after the second working medium enters the second working medium flow path 52 for a heat exchange process, and the second working medium product is recycled through the second interface 47;
the third working medium flow path 53 is sequentially connected with the third working medium interface 45, the third heat exchanger 33 and the third interface 48, wherein a third working medium product is obtained after the third working medium enters the third working medium flow path 53 for a heat exchange process, and the third working medium product is recycled through the third interface 48.
In particular, the first three-way valve has a first inlet 211, a second inlet 212 and a first outlet 213, the second three-way valve has a third inlet 221, a second outlet 222 and a third outlet 223, wherein the cascade liquid hydrogen station cold recovery system 100 further includes a backflow hydrogen flow path 54, and the backflow hydrogen flow path 54 is sequentially connected with the second outlet 222 of the second three-way valve and the first inlet 211 of the first three-way valve, and is used for introducing partial backflow hydrogen into the hydrogen flow path 55, increasing the hydrogen temperature in the hydrogen flow path 55, and avoiding the blockage of the heat exchanger flow path due to the solidification of the working medium caused by the temperature in the hydrogen flow path 55 being lower than the freezing point of the working medium.
That is to say, because the liquid hydrogen temperature is less than liquid nitrogen solidification temperature, in order to avoid nitrogen to solidify and block the heat exchanger runner, the utility model designs a hydrogen flow path 54 backflows for partial hydrogen backflows and liquid hydrogen mixes, improves hydrogen stream temperature, thereby avoids nitrogen to solidify and block the heat exchanger runner.
It can be understood that the utility model discloses a two tee bend structures to set up two tee bend structures respectively the mode of first heat exchanger 31 both sides has realized adopting comparatively simple structure to have constructed hydrogen flow path 55 with backflow hydrogen flow path 54 is favorable to simplifying the structure of cascade type liquid hydrogen hydrogenation station cold volume recovery system 100 reduces holistic volume.
It can be understood that, because the liquid hydrogen temperature is only about 20K, a proper working medium needs to be selected for heat exchange with hydrogen, and the selected working medium should satisfy the following conditions: 1. is non-toxic and harmless; 2. the melting point is low enough, the specific heat capacity is large, and the material is not solidified; 3. because the area of the hydrogenation station is limited, the required supporting facilities have low construction cost and small occupied area; 4. it is easy to exchange heat with other working media.
Based on this, the utility model discloses a nitrogen gas, carbon dioxide, ethylene glycol or water are retrieved and cold-storage working medium as the cold energy of liquid hydrogen, and these working mediums can both satisfy aforementioned several requirements betterly, can realize the recovery of liquid hydrogen gasification liquid hydrogen cold energy to can carry out effective cold energy and recycle.
Specifically, the first working medium selected by the utility model is nitrogen, the first working medium interface 43 is connected to the nitrogen gas cylinder group, and the first interface 46 is connected to the liquid nitrogen storage tank; the second working medium is carbon dioxide, the second working medium interface 44 is connected to the carbon dioxide gas cylinder group, and the second interface 47 is connected to a liquid carbon dioxide storage tank or an ice making machine; the third working medium is glycol or water, the third working medium interface 45 is connected to the high-temperature solution tank, and the third interface 48 is connected to the low-temperature solution tank.
It will be appreciated that the four fluid flow directions follow the directions of the arrows shown in fig. 1:
liquid hydrogen: liquid hydrogen passes through first tee bend structure 21, mixes with the hydrogen that flows back that gets into first tee bend structure 21 and gets into for hydrogen A gets into first heat exchanger 31 becomes hydrogen B, and hydrogen B gets into in the second tee bend structure 22, and a share divides into the hydrogen that flows back and gets into in the first tee bend structure 21, another share is called hydrogen C and flows into behind second heat exchanger 32, becomes hydrogen D, and hydrogen D flows through become the hydrogen E that is close normal atmospheric temperature behind the third heat exchanger 33, and hydrogen E via hydrogen interface 42 gets into hydrogen storage tank or hydrogen compressor and carries out recycle.
Nitrogen gas: the nitrogen sequentially passes through the third heat exchanger 33, the second heat exchanger 32, the first heat exchanger 31 and the throttle valve 34, the name of the nitrogen is sequentially changed from nitrogen A to nitrogen B, nitrogen C, liquid nitrogen A and liquid nitrogen B, and the liquid nitrogen B enters the liquid nitrogen storage tank through the first interface 46 to be recovered.
Carbon dioxide: the carbon dioxide sequentially passes through the third heat exchanger 33 and the second heat exchanger 32, the name of the carbon dioxide is sequentially changed from carbon dioxide A to carbon dioxide B and carbon dioxide C, and the carbon dioxide C enters a liquid carbon dioxide storage tank or an ice making machine through the second interface 47 for recycling.
Solution: the solution a passes through the third heat exchanger 33 and then outputs a solution B with a lower temperature, and the solution B enters the low-temperature solution tank through the third interface 48 for recycling, wherein the solution is ethylene glycol or water.
Nitrogen pressure: in order to reduce the investment of the compressor and the liquid hydrogen amount of the hydrogenation station is not large (generally 500-2000 kg), the gasification process is carried out intermittently, which means that the use efficiency of the compressor is low. Therefore, the nitrogen is supplied by a high-purity gas cylinder group, the pressure after decompression can be set to be more than or equal to 2bara, and the gas utilization rate in the gas cylinder group is improved as much as possible. After throttling of the liquid nitrogen, the pressure is atmospheric pressure.
Carbon dioxide pressure: the carbon dioxide is supplied by a high-purity gas cylinder group. In order to avoid the triple point of carbon dioxide and avoid the carbon dioxide from being solidified in the flow channel of the heat exchanger, the pressure after pressure reduction can be determined to be more than or equal to 6bara.
Solution pressure: > 1bara, to ensure that the solution can be driven to flow.
Pressure of hydrogen: compared with the process of compressing gaseous hydrogen by a compressor after gasification, the liquid hydrogen pump is utilized to pressurize the liquid hydrogen, and the energy consumption of the liquid hydrogen pump is far lower than that of the compressor. Therefore, the pressure of the liquid hydrogen is high during vaporization.
Example of calculation:
the quantities of liquid nitrogen, dry ice and glycol solution (50%) that can be obtained are calculated according to the liquid hydrogen station with a 1 ton/day hydrogenation capacity:
conditions are as follows: hydrogen pressure 25bara, nitrogen pressure 6bara, carbon dioxide pressure 6bara, solution pressure 2bara, each stream temperature was set according to the following table:
the flow rate of each stream is calculated as:
| stream of oil | Liquid hydrogen | Back flow of hydrogen | Solution(s) | Carbon dioxide | Nitrogen is present in |
| Mass kg | 1000 | 624 | 6070 | 3010 | 3902 |
It can be seen, adopt the utility model discloses a cascade-type liquid hydrogen hydrogenation station cold volume recovery system 100 and method, 1 ton liquid hydrogen can obtain 3.9 tons of liquid nitrogen, 3 tons of dry ice and 9 tons of refrigerated ethylene glycol solution, it is visible the utility model discloses a cascade-type liquid hydrogen hydrogenation station cold volume recovery system 100 and method can realize the recovery of liquid hydrogen gasification liquid hydrogen cold energy effectively to can carry out effective cold energy and recycle.
In addition, the cold energy in the process of recycling liquid hydrogen gasification also needs reasonable heat exchange structure arrangement to ensure that the cold energy can be utilized in a gradient way. Therefore, the utility model discloses according to the working medium type and the quantity that adopt, chooseed for use three heat exchanger, specifically, in this embodiment, first heat exchanger 31 be two strand flows heat exchanger second heat exchanger 32 be three strand flows heat exchanger third heat exchanger 33 is four strand flows heat exchanger.
It should be understood that, in some embodiments of the present invention, the cascade-type liquid hydrogen station cold recovery system 100 may further include four or more heat exchangers according to actual use conditions, and the types of the heat exchangers and the types and the number of the working mediums may be selected according to actual needs, which is not limited by the present invention.
Particularly, except that the hydrogenation station also has the demand to cold volume, like the precooling before the high pressure hydrogenation, the utility model discloses still consider following liquid hydrogen application scene, let the cold volume of retrieving obtain abundant utilization.
Scene 1: the temperature of the liquid hydrogen bottle of the liquid hydrogen vehicle is reduced as close as possible to the temperature of the liquid hydrogen
Liquid hydrogen vehicle liquid hydrogen bottle can need the cooling after first use or long-term not using. If liquid hydrogen is directly adopted for cooling, a large amount of liquid hydrogen volatilizes. If cold energy recovery when gasifying liquid hydrogen is stored for the precooling cooling of liquid hydrogen bottle of liquid hydrogen vehicle, the cold energy that liquid hydrogen vehicle liquid hydrogen bottle cooling needs will certainly be reduced, the quantity of liquid hydrogen when reducing the temperature.
Scene 2: the cold accumulation working medium is directly used, about 50 DEG C
For a conventional refrigerator car, cold storage working media such as carbon dioxide working media and glycol solution can be adopted for refrigeration. If the cold energy in the liquid hydrogen gasification process is used for preparing dry ice from carbon dioxide and cooling glycol solution, the hydrogenation station can be changed into a small dry ice and low-temperature glycol solution supply station.
Scene 3: cooling the compressor of the hydrogenation station and high-temperature hydrogen at the temperature of more than 0 DEG C
When the compressor works, a motor of the compressor needs to be cooled, the temperature of compressed hydrogen also needs to be cooled to room temperature, and water cooling is a conventional cooling method. The hydrogen cold energy is provided to water, and can be used for cooling a compressor motor and high-temperature hydrogen.
The utility model discloses utilize, construction cost, cold energy recovery recycle according to the gradient of above application scene, hydrogen cold energy, proposed cascade type liquid hydrogen hydrogenation station cold volume recovery system 100 and method choose for use nitrogen, carbon dioxide, ethylene glycol solution, water etc. to retrieve and cold-storage working medium for the cold energy, realize the recovery of liquid hydrogen gasification liquid hydrogen cold energy to can carry out effective cold energy and recycle, avoid the problem in air cooling, water-cooling gasification, improve the hydrogenation station economic nature.
The utility model discloses on the other hand still provides a cascade type liquid hydrogen station cold volume recovery method, including the step:
s1, introducing liquid hydrogen into a hydrogen flow path 55, wherein the liquid hydrogen flows through a first three-way structure 21, is mixed with hydrogen flowing back into the first three-way structure 21 and then sequentially flows through a first heat exchanger 31, a second three-way structure 22, a second heat exchanger 32 and a third heat exchanger 33 to form hydrogen, and the hydrogen is discharged through a hydrogen interface 42;
s2, introducing a first working medium into a first working medium flow path 51, wherein the first working medium flows through a third heat exchanger 33, a second heat exchanger 32, a first heat exchanger 31 and a throttle valve 34 in sequence to obtain a first working medium product, and the first working medium product is discharged through a first interface 46;
s3, introducing a second working medium into a second working medium flow path 52, wherein the second working medium flows through the third heat exchanger 33 and the second heat exchanger 32 in sequence to obtain a second working medium product, and the second working medium product is discharged through a second interface 47;
and S4, introducing a third working medium into a third working medium flow path 53, wherein a third working medium product is obtained after the third working medium flows through the third heat exchanger 33, and the third working medium product is discharged through a third interface 48.
Specifically, the utility model discloses a first working medium is nitrogen gas, the second working medium is carbon dioxide, the third working medium is ethylene glycol or water.
Correspondingly, in step S2, the first working medium interface 43 is connected to the nitrogen gas cylinder set to introduce nitrogen gas into the first working medium flow path 51 through the nitrogen gas cylinder set, and the first interface 46 is connected to a liquid nitrogen storage tank to recover liquid nitrogen.
Correspondingly, in step S3, the second working medium interface 44 is connected to the carbon dioxide gas cylinder set, so as to introduce carbon dioxide into the second working medium flow path 52 through the carbon dioxide gas cylinder set, and the second interface 47 is connected to a liquid carbon dioxide storage tank or an ice drying machine, so as to recover liquid carbon dioxide.
Correspondingly, in step S4, the third working medium interface 45 is connected to the high-temperature solution tank, so as to introduce ethylene glycol or water into the third working medium flow path 53 through the high-temperature solution tank, and the third interface 48 is connected to the low-temperature solution tank, so as to recover the ethylene glycol solution or water.
Particularly, in step S2, the pressure of the first working medium introduced into the first working medium flow path 51 is greater than or equal to 2bara; in step S3, the pressure of the second working medium introduced into the second working medium flow path 52 is more than or equal to 6bara; in step S4, the pressure of the third working fluid introduced into said third working fluid flow path 53 is > 1bara.
In general, the utility model discloses cold energy is extravagant among the gasification to liquid hydrogen, the degree of difficulty exists in the vaporizer design, and the problem of extra power consumption, multiple application scene according to liquid hydrogen cold energy, hydrogen cold energy gradient utilizes, construction cost, many-sided such as cold energy recovery is recycled, a cascade type liquid hydrogen hydrogenation station cold volume recovery system has been proposed, choose for use nitrogen, carbon dioxide, ethylene glycol solution, water etc. are cold energy recovery and cold-storage working medium, realize the recovery of liquid hydrogen gasification liquid hydrogen cold energy, and can carry out effective cold energy and recycle, avoided at the air cooling, the problem among the water-cooling gasification, the economic nature at liquid hydrogen hydrogenation station has been improved.
The technical features of the above embodiments can be arbitrarily combined, and for the sake of brevity, all possible combinations of the technical features in the above embodiments are not described, but should be considered as the scope of the present specification as long as there is no contradiction between the combinations of the technical features.
The above examples only represent preferred embodiments of the present invention, which are described in more detail and detail, but are not to be construed as limiting the scope of the invention. It should be noted that, for those skilled in the art, without departing from the concept of the present invention, several variations and modifications can be made, which all fall within the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the appended claims.
Claims (6)
1. The cascade type liquid hydrogen hydrogenation station cold energy recovery system is characterized by comprising a plurality of tee joint structures and a plurality of heat exchangers which are uniformly distributed in a closed cold box, wherein the cascade type liquid hydrogen hydrogenation station cold energy recovery system comprises a hydrogen flow path and a plurality of working medium flow paths, and the hydrogen flow path is connected with the tee joint structures and the heat exchangers and is used for supplying liquid hydrogen to perform a multi-stage heat exchange process; the flow direction of the working medium flow path is opposite to that of the hydrogen flow path, and the working medium flow path is connected with one or more heat exchangers.
2. The cascade liquid hydrogen hydrogenation station cold energy recovery system of claim 1, wherein the cascade liquid hydrogen hydrogenation station cold energy recovery system comprises a first tee structure, a second tee structure, a first heat exchanger, a second heat exchanger, a third heat exchanger, a throttle valve, a liquid hydrogen interface, a first working medium interface, a second working medium interface, a third working medium interface, a first interface, a second interface and a third interface; the plurality of working medium flow paths comprise a first working medium flow path, a second working medium flow path and a third working medium flow path;
the hydrogen flow path is sequentially connected with a liquid hydrogen interface, the first tee structure, the first heat exchanger, the second tee structure, the second heat exchanger, the third heat exchanger and a hydrogen interface;
the first working medium flow path is sequentially connected with a first working medium interface, the third heat exchanger, the second heat exchanger, the first heat exchanger, a throttle valve and a first interface;
the second working medium flow path is sequentially connected with the second working medium interface, the third heat exchanger, the second heat exchanger and the second interface;
the third working medium flow path is sequentially connected with the third working medium interface, the third heat exchanger and the third interface.
3. The cascade type liquid hydrogen hydrogenation station cold energy recovery system of claim 2, wherein the first three-way valve has a first inlet, a second inlet and a first outlet, and the second three-way valve has a third inlet, a second outlet and a third outlet, and wherein the cascade type liquid hydrogen hydrogenation station cold energy recovery system further comprises a backflow hydrogen gas flow path, and the backflow hydrogen gas flow path is sequentially connected with the second outlet of the second three-way valve and the first inlet of the first three-way valve, and is used for introducing partial backflow hydrogen gas into the hydrogen flow path to increase the hydrogen temperature in the hydrogen flow path.
4. The cascade liquid hydrogen hydrogenation station cold energy recovery system of claim 3, wherein the first heat exchanger is a two-stream heat exchanger, the second heat exchanger is a three-stream heat exchanger, and the third heat exchanger is a four-stream heat exchanger.
5. The cascade liquid hydrogen hydrogenation station cold energy recovery system of claim 4, wherein the first working medium is nitrogen, the first working medium interface is connected to a nitrogen gas cylinder group, and the first interface is connected to a liquid nitrogen storage tank; the second working medium is carbon dioxide, the second working medium interface is connected to the carbon dioxide gas cylinder group, and the second interface is connected to the liquid carbon dioxide storage tank or the ice making machine; the third working medium is glycol or water, the third working medium interface is connected to the high-temperature solution tank, and the third interface is connected to the low-temperature solution tank.
6. The cascade type liquid hydrogen station cold energy recovery system according to claim 5, wherein the pressure of the first working medium flow path is more than or equal to 2bara, the pressure of the second working medium flow path is more than or equal to 6bara, and the pressure of the third working medium flow path is more than 1bara.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115789511A (en) * | 2022-12-12 | 2023-03-14 | 中山先进低温技术研究院 | Liquid hydrogen cold energy gradient utilization system and method |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115789511A (en) * | 2022-12-12 | 2023-03-14 | 中山先进低温技术研究院 | Liquid hydrogen cold energy gradient utilization system and method |
| CN115789511B (en) * | 2022-12-12 | 2023-10-17 | 中山先进低温技术研究院 | Liquid hydrogen cold energy cascade utilization system and method |
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