CN207635720U - Gas liquefaction system - Google Patents
Gas liquefaction system Download PDFInfo
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- CN207635720U CN207635720U CN201721648442.2U CN201721648442U CN207635720U CN 207635720 U CN207635720 U CN 207635720U CN 201721648442 U CN201721648442 U CN 201721648442U CN 207635720 U CN207635720 U CN 207635720U
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- 239000007789 gas Substances 0.000 claims abstract description 86
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 74
- 239000001257 hydrogen Substances 0.000 claims abstract description 68
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 68
- 238000005057 refrigeration Methods 0.000 claims abstract description 62
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 238000001816 cooling Methods 0.000 claims description 27
- 150000002431 hydrogen Chemical class 0.000 claims description 7
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- 230000001131 transforming effect Effects 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 20
- 239000001307 helium Substances 0.000 abstract description 17
- 229910052734 helium Inorganic materials 0.000 abstract description 17
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 abstract description 17
- 230000008569 process Effects 0.000 abstract description 17
- 239000007791 liquid phase Substances 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 3
- 230000009286 beneficial effect Effects 0.000 abstract 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- 238000006243 chemical reaction Methods 0.000 description 8
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- 238000004781 supercooling Methods 0.000 description 4
- 238000004364 calculation method Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000002360 explosive Substances 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- 238000005482 strain hardening Methods 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000010835 comparative analysis Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 230000005283 ground state Effects 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004451 qualitative analysis Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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- Separation By Low-Temperature Treatments (AREA)
Abstract
A gas liquefaction system comprises a compressor unit, a precooling heat exchanger, a multi-stage intermediate turbine precooling unit, a first heat exchanger, a final stage turboexpander, a second heat exchanger, a throttling valve and a low-temperature liquid storage tank. The second heat exchanger is arranged between the throttling valve and the low-temperature liquid storage tank. The gas liquefaction system comprises a gas circuit to be liquefied, a refrigeration working medium circulation process and a precooling working medium circulation loop. Compared with the traditional helium refrigeration hydrogen liquefaction system, the gas liquefaction system has the advantages that the dryness of the liquefied gas can be further reduced to 0 by additionally arranging the first-stage second heat exchanger after the throttling of the throttling valve, the outlet pipeline of the second heat exchanger is ensured to be operated in a full liquid phase, safety is realized, and the equipment cost is saved; the lowest temperature of the whole gas liquefaction system is increased, thereby being beneficial to improving the system efficiency and saving energy.
Description
Technical field
The utility model is related to liquefaction technology field more particularly to a kind of gas liquefaction systems.
Background technology
Since the fossil fuel for meeting our times energy demand is almost exhausted, and its combustion product can cause environment
Pollution, therefore seek the key subjects that new energy is attracted attention as the world.Hydrogen it is resourceful, source is various, as a kind of secondary
The energy, it has many advantages, such as combustion heat value height, clean environment firendly, can store, is renewable.And Hydrogen Energy can meet resource, ring simultaneously
The requirement in border and sustainable development, so the energy referred to as human future.
Hydrogen is typically the equilibrium mixture of ortho-hydrogen and parahydrogen.The equilibrium concentration of hydrogen has significantly with the difference of temperature
Variation.When the temperature decreases, the ortho-hydrogen with high-energy ground state is spontaneously converted to the parahydrogen of lower state, until that cannot convert,
As balance hydrogen at this temperature.Under room temperature thermal equilbrium state, hydrogen is about made of 75% ortho-hydrogen and 25% parahydrogen, referred to herein as just
Chang Qing.The n- parastate conversion of Gaseous Hydrogen could occur in the presence of a catalyst, and liquified hydrogen is then in not catalyst
In the case of n- secondary conversion also can spontaneously occur.But conversion rate is slower.The just secondary conversion of hydrogen is an exothermic reaction, in liquid
In hydrogen storing process, in order to avoid converting the vaporization of thermally-induced liquid hydrogen product, re-liquefied energy consumption is reduced, for large-scale liquefaction of hydrogen
Device, parahydrogen content should be more than 95% in product.
Liquid hydrogen is as one of currently the most important ones storage and transportation mode, and in long-distance transportation, storage etc. has huge warp
Ji property, plays an important role in hydrogen utilization.The process (including just secondary critical heat) of liquefaction of hydrogen takes around consuming
Therefore 17kWh/kgLH2 improves overall efficiency, save energy consumption, contribute to large-scale use and the popularization of liquid hydrogen.
It is traditional using helium as refrigerant, the Process flow for carrying out liquefaction of hydrogen is as shown in Figure 1.It includes mainly one
Cover closed helium refrigeration, Liquid nitrogen precooler and hydrogen road.Specifically, including helium compressor 20, helium turboexpander 30, hydrogen
Compressor 40, four heat exchangers 50,60,70,80,100m3Liquid hydrogen tank 90, hydrogen source 22, pipeline 24 and pipeline 26.Liquid nitrogen from
Pipeline 24 enters, and after heat exchange, liquid nitrogen becomes nitrogen and flowed out from pipeline 26.Hydrogen road after low-temperature helium cools down, by throttle valve into
Enter liquid hydrogen storage tank.If the degree of supercooling before throttle valve is sufficiently large, all liquid hydrogen after throttling；If degree of supercooling is inadequate, save
There is flashed vapour after stream, is then recycled by hydrogen compressor.
For the traditional process, a kind of method is that the fluid of gas-liquid two-phase after throttling is directly entered wet tank, by gas
Increase pressure through hydrogen compressor after backheat, recycling uses, this technological process is complicated, and hydrogen is flammable explosive gas, exist safety,
A series of problems, such as cost；Second method then can ensure its certain supercooling by way of temperature before reducing throttle valve
Degree so that the gas after throttling is still within the state of full liquid phase, can cause the decline of system effectiveness in this case.
Utility model content
In consideration of it, it is necessary to provide a kind of safety, refrigerating efficiency, energy saving gas liquefaction system can be improved.
Turbine pre-cooling unit, first are changed among a kind of gas liquefaction system, including compressor set, precool heat exchanger device, multistage
Hot device, final stage turbo-expander, the second heat exchanger, throttle valve and cryogenic liquid storage tank；
The outlet of the compressor set is connected to the high-pressure side refrigeration working medium entrance of the precool heat exchanger device, and the precooling is changed
The high-pressure side refrigeration working medium outlet of hot device is connected to the high-pressure side refrigeration working medium entrance of the multistage intermediate turbine pre-cooling unit, institute
The high-pressure side refrigeration working medium of the high-pressure side refrigeration working medium outlet and the First Heat Exchanger of stating turbine pre-cooling unit among multistage enters
The high-pressure side refrigeration working medium outlet of mouth connection, the First Heat Exchanger is connected to the entrance of the final stage turbo-expander, described
The outlet of final stage turbo-expander is connected to the refrigeration working medium entrance of second heat exchanger, the refrigeration work of second heat exchanger
Matter outlet is connected to the low-pressure side refrigeration working medium entrance of the First Heat Exchanger, the low-pressure side refrigeration working medium of the First Heat Exchanger
It exports and is connected to the low-pressure side refrigeration working medium entrance of the multistage intermediate turbine pre-cooling unit, the multistage intermediate turbine precooling is single
The low-pressure side refrigeration working medium outlet of member is connected to the low-pressure side refrigeration working medium entrance of the precool heat exchanger device, the precool heat exchanger device
Low-pressure side refrigeration working medium outlet be connected to the entrance of the compressor set；
The precool heat exchanger device further includes gas access to be liquefied and gas vent to be liquefied, and the precool heat exchanger device waits for
Liquid gas is exported to be connected to the gas access to be liquefied of the multistage intermediate turbine pre-cooling unit, and the multistage intermediate turbine is pre-
The gas vent to be liquefied of cold unit is connected to the gas access to be liquefied of the First Heat Exchanger, and the First Heat Exchanger waits for
Liquid gas outlet is connected to the entrance of the throttle valve, the outlet of the throttle valve and the gas to be liquefied of second heat exchanger
Body entrance is connected to, and the gas vent to be liquefied of second heat exchanger is connected to the cryogenic liquid storage tank；
The precool heat exchanger device further includes precooling working medium entrances and precooling sender property outlet.
In one embodiment, further include precooling working medium unit, the outlet and the precooling of the precooling working medium unit are changed
The precooling working medium entrances of hot device are connected to, and the entrance of the precooling sender property outlet of the precool heat exchanger device and the precooling working medium unit connects
It is logical.
In one embodiment, the multistage intermediate turbine pre-cooling unit is the combination of heat exchanger and turbo-expander.
In one embodiment, the multistage intermediate turbine pre-cooling unit is based on Cloud's refrigeration cycle or Collins's system
The combination of the heat exchanger and turbo-expander of SAPMAC method.
In one embodiment, the gas to be liquefied is hydrogen, and the gas access to be liquefied of the precool heat exchanger device is also
Equipped with hydrogen filter device and hydrogen purification devices.
In one embodiment, the gas to be liquefied is hydrogen, and the precool heat exchanger device, the multistage intermediate turbine are pre-
It is filled with positive parahydrogen transforming agent in the hydrogen paths in heat exchanger and the First Heat Exchanger in cold unit.
In one embodiment, the gas vent to be liquefied of the First Heat Exchanger, parahydrogen concentration are more than or equal to 95%.
Above-mentioned gas liquefaction system, under same system wasted work, by the liquefaction flow path form for changing low-temperature end so that
Final stage turbo-expander expands at high temperature, obtains more High cooling power, compared with traditional helium refrigeration liquefaction of hydrogen system, in throttle valve
The second heat exchanger of level-one is further added by after throttling to be further reduced to 0 by the mass dryness fraction of the gas after liquefaction, ensure the second heat exchange
The export pipeline of device runs for full liquid phase, compares scheme one, and safety can save equipment cost；Compared to scheme two, entire gas
The minimum temperature of liquefaction system improves, and helps to improve system effectiveness, energy saving.
Description of the drawings
Fig. 1 is the structural schematic diagram of traditional helium refrigeration liquefaction of hydrogen system；
Fig. 2 is the structural schematic diagram of the gas liquefaction system of an embodiment；
Fig. 3 is structural schematic diagram of the end flow using the gas liquefaction system of conventional flowage structure.
Specific implementation mode
It is with reference to the accompanying drawings and embodiments, right in order to make the purpose of this utility model, technical solution and advantage be more clear
The utility model is further elaborated.It should be appreciated that specific embodiment described herein is only used to explain this reality
With novel, it is not used to limit the utility model.
As shown in Fig. 2, in the gas liquefaction system 10 of an embodiment, including compressor set 1, precool heat exchanger device 8, multistage
Between turbine pre-cooling unit 3, First Heat Exchanger 4, final stage turbo-expander 5, the second heat exchanger 9, throttle valve 6 and cryogenic liquid storage tank
7。
The outlet of compressor set 1 is connected to the high-pressure side refrigeration working medium entrance of precool heat exchanger device 8, the height of precool heat exchanger device 8
The outlet of pressure side refrigeration working medium is connected to the high-pressure side refrigeration working medium entrance of multistage intermediate turbine pre-cooling unit 3, multistage intermediate turbine
The high-pressure side refrigeration working medium outlet of pre-cooling unit 3 is connected to the high-pressure side refrigeration working medium entrance of First Heat Exchanger 4, First Heat Exchanger
4 high-pressure side refrigeration working medium outlet is connected to the entrance of final stage turbo-expander 5, the outlet of final stage turbo-expander 5 and second
The refrigeration working medium entrance of heat exchanger 9 is connected to, and the refrigeration working medium outlet of the second heat exchanger 9 and the low-pressure side of First Heat Exchanger 4 are freezed
Working medium entrances are connected to, the low-pressure side system of the low-pressure side refrigeration working medium outlet of First Heat Exchanger 4 and multistage intermediate turbine pre-cooling unit 3
Cold working medium entrances connection, the low-pressure side of low-pressure side the refrigeration working medium outlet and precool heat exchanger device 8 of multistage intermediate turbine pre-cooling unit 3
Refrigeration working medium entrance is connected to, and the low-pressure side refrigeration working medium outlet of precool heat exchanger device 8 is connected to the entrance of compressor set 1.
Precool heat exchanger device 8 further includes gas access to be liquefied and gas vent to be liquefied, the gas to be liquefied of precool heat exchanger device 8
Body is exported to be connected to the gas access to be liquefied of multistage intermediate turbine pre-cooling unit 3, and multistage intermediate turbine pre-cooling unit 3 waits for liquid
Change gas vent to be connected to the gas access to be liquefied of First Heat Exchanger 4, the gas vent to be liquefied of First Heat Exchanger 4 and throttling
The entrance of valve 6 is connected to, and the outlet of throttle valve 6 is connected to the gas access to be liquefied of the second heat exchanger 9, and the second heat exchanger 9 waits for
Liquid gas outlet is connected to cryogenic liquid storage tank 7.
Precool heat exchanger device 8 further includes precooling working medium entrances and precooling sender property outlet.
Gas liquefaction system 10 further includes precooling working medium unit, the outlet of precooling working medium unit 2 and precool heat exchanger device 8 it is pre-
The precooling sender property outlet of cold working medium entrances connection, precool heat exchanger device 8 is connected to the entrance of precooling working medium unit 2.Working medium is pre-chilled can
Think liquid nitrogen.It is appreciated that precooling working medium is not limited to liquid nitrogen.
Multistage intermediate turbine pre-cooling unit 3 is the combination of heat exchanger and turbo-expander.Further, multistage intermediate turbine
Pre-cooling unit 3 is the combination of heat exchanger and turbo-expander based on Cloud's refrigeration cycle or Collins's refrigeration cycle.Heat exchange
The quantity and spread pattern of device and turbo-expander can be configured according to actual needs.
In one embodiment, gas to be liquefied is hydrogen, and the gas access to be liquefied of precool heat exchanger device 8 is additionally provided with hydrogen mistake
Filter device (not shown) and hydrogen purification devices (not shown).Gas to be liquefied is not limited to hydrogen.
In one embodiment, gas to be liquefied is hydrogen, and positive parahydrogen is filled in the hydrogen paths of precool heat exchanger device 8 and is turned
Agent.The gas vent to be liquefied of precool heat exchanger device 8, parahydrogen concentration are about 45%.It is equipped in the hydrogen paths of First Heat Exchanger 4
Positive parahydrogen transforming agent.The gas vent to be liquefied of First Heat Exchanger 4, parahydrogen concentration are more than or equal to 95%.Multistage intermediate turbine is pre-
Also positive parahydrogen transforming agent is filled in the hydrogen paths of heat exchanger in cold unit 3.
In one embodiment, refrigeration working medium is helium, it will be understood that refrigeration working medium is not limited to helium.
In above-mentioned gas liquefaction system 10, gas road 100 to be liquefied is one-way passage, and entrance is generally high pressure gas.
This sentences gas to be liquefied and is illustrated for hydrogen.Consider from secure context, to prevent impurity in hydrogen from especially consolidating oxygen deposition,
Explosive accident, 99.999% rank that source hydrogen purity need to meet national regulations is caused to be needed if being unsatisfactory for requiring
It is filtered, purifies.It after meeting index request, enters back into ice chest, is cooled down by precool heat exchanger device 8, while in precool heat exchanger
Positive parahydrogen transforming agent is filled in device 8, after conversion, parahydrogen concentration is about 45%, subsequently into turbine among multistage
After heat exchanger and First Heat Exchanger 4 in chilldown system 3 temperature reduce and further across multistage just secondary conversion after, it is secondary
Hydrogen concentration about reaches 98%, is depressured by throttle valve 6, and outlet is gas-liquid two-phase fluid, after the second heat exchanger 9, quilt
Refrigeration working medium less than its boiling temperature cools down, and enters in cryogenic liquid storage tank 7 after being fully liquefied, and parahydrogen concentration is made and is more than
95% liquid hydrogen product.
Refrigeration working medium circulation loop 200 is as follows：Refrigeration working medium gas pressure after the compression of compressor set 1 first increases,
After the precooling of pre-cooled heat exchanger 8 and multistage intermediate turbine pre-cooling unit 3 are pre-chilled, temperature reduces, and into First Heat Exchanger 4, passes through
After crossing 5 decrease temperature and pressure of final stage turbo-expander, pass through the second heat exchanger successively at a temperature below being liquefied after gas hydrogen boiling point
9, the heat exchanger rewarming in First Heat Exchanger 4 and multiple expansion engine chilldown system 3, is arrived into 8 rewarming of Liquid nitrogen precooler heat exchanger
Room temperature enters back into compressor set 1, re-starts compression, forms complete refrigeration working medium closed cycle.
It is as follows that working medium circulation circuit 300 is pre-chilled：The precooling working medium flowed out from precooling working medium unit 2 enters precool heat exchanger device 8,
After precooling working medium transfers heat to refrigeration working medium and gas to be liquefied, precooling working medium unit 2 is flowed back to from precool heat exchanger device 8,
Form a cycle.
Gas liquefaction system 10 is illustrated so that helium freezes liquefaction of hydrogen as an example, equally applicable for other gas liquefactions；In advance
Cold form includes but are not limited to liquid nitrogen.
Emulation shows 10 practicability and effectiveness of gas liquefaction system.Below by the specific calculation specifications gas liquefaction system
The validity of 10 Process flow.For convenience of the validity of the gas liquefaction system 10 is proved, least significant end flow is only calculated, it is conventional
Helium refrigeration liquefaction of hydrogen system simplification Process flow it is as shown in phantom in Figure 3, wherein 201 in Fig. 3,202,203,204,
301,302,303 corresponding connecting line is corresponded to.In the Process flow such as Fig. 2 of the simplification of the gas liquefaction system 10 of the application
Shown in dotted line frame, wherein in Fig. 2 201,202 ', 203 ', 204,205,301,302 ', 303 ', 303 it is corresponding in it is corresponding
Connecting line.
In order to ensure to have same primary condition, boundary temperature, pressure and the refrigerant gas of fixed First Heat Exchanger 4
Flow, to calculate the liquefaction amount of the maximum accessible gas that is liquefied.For commonly calculating temperature range, two are carried out
The performance of kind Process flow compares,
Calculation of boundary conditions is as shown in table 1 below：
The Process flow boundary condition of the traditional helium refrigeration liquefaction of hydrogen system of table 1
| (T201,P201) | P204 | (T301, P301) | P303 | |
| Unit | (K, bar) | bar | (K, bar) | bar |
| Numerical value | (45,12) | 1.5 | (45,20) | 1.05 |
The Process flow assumed condition of the traditional helium refrigeration liquefaction of hydrogen system of table 2
As shown in figure 3, in order to ensure that the liquid after throttling by throttle valve 8 is full liquid phase, then T302 must assure that centainly
Degree of supercooling, in this example, the temperature of T302 is determined as 19K, then the temperature 20.95K after throttling can be protected in the pressure of 1.5bar
Card is full liquid phase.4 pressure drop of First Heat Exchanger in remaining flow, flow, efficiency of turbine etc. are assumed that parameter is rule of thumb arranged and are seen
Shown in table 2.
In addition, in First Heat Exchanger 4, hydrogen carries out just secondary conversion, and critical heat is taken away by low-temperature helium cold.Assuming that first
Heat exchanger 4 processes the requirement for the minimum temperature difference 0.2K that can reach capacity, and therefore, T203 is set as 0.2K with the T302 temperature difference, i.e.,
T203 is 18.8K.By assumed above, in workflow management, each equipment can provide a conservation equation, and each logistics has
3 variables and there are the conservation of mass for same logistics.By above assumed condition, can obtain current known variables is
T202, T204, m301, T303.Wherein a total of 3 equipment (First Heat Exchanger 4, final stage turbo-expander 5 and throttle valve 6), 3
A conservation equation, 3 equations in total, equation can whether there is or not array solution, adjust m301 make T204 less than inlet temperature T201 >=
0.2K.Under above-mentioned assumed condition, acquisition liquefaction of hydrogen amount m301 maximum liquefaction amounts are 21.02g/s.
Step according to the above analysis calculates the process parameter in dotted line frame shown in Fig. 2.To ensure the inlet and outlet of two kinds of flows
Condition is consistent, and in this time analyzing, liquid hydrogen outlet temperature T303 is fixed as the flow one of traditional helium refrigeration liquefaction of hydrogen system
The temperature of sample is 20.95K.Calculation of boundary conditions is as shown in table 3 below.
The boundary condition of 3 modified flow form of table
| (T201,P201) | P204 | (T301, P301) | P303 | T303 | |
| Unit | (K, bar) | bar | (K, bar) | bar | K |
| Numerical value | (45,12) | 1.5 | (45,20) | 1.05 | 20.95 |
The assumed condition of 4 modified flow form of table
In Process flow shown in Fig. 2, Fig. 3 is compared, increases by the second heat exchanger 9, analyzes its whole flow process meter below
Calculate the condition that equation group is closed.When 22K, the equilibrium concentration of the parahydrogen in hydrogen has arrived at 98%, therefore, assumes in this example
The temperature of T302 ' is 22K.Equally, T203 ' requires to be set as 20.75K according to heat exchanger processing, then by after assumed above, not
Know that variable is as follows：T303 ', T205, T202 ', T204, m301.The similar above analysis, 5 unknown numbers just have 4 equipment
(First Heat Exchanger 4, final stage turbo-expander 5, throttle valve 6 and the second heat exchanger 9) forms 4 equations, and equation number is less than unknown
Several numbers, the countless solutions of equation.According to above-mentioned condition, the flow of m301 is adjusted so that T204 goes out equal to what former workflow management obtained
Mouth temperature 44.8K, the maximum liquefaction amount for obtaining hydrogen are：22.78g/s.
Pass through above comparative analysis, under similarly inlet and outlet boundary condition, the improved Process flow (Fig. 2 of the application
It is shown) turboexpander inlet temperature T202 ' be 36.28K, former flow (Fig. 3) T202 be 33.22K, due to final stage turbine expansion
Machine 5 expands at high temperature, and the cold brought is more, and in this example, modified flow turbo-expander cold is 16.26kW, former
There is flow turbo-expander cold 14.99kW, compared to former flow, liquefaction amount increases to 22.78g/s by 21.02g/s.And from original
It is said in reason, this scheme form does not influence the qualitative analysis because of the setting of assumed condition.
Above-mentioned gas liquefaction system 10, by changing the liquefaction flow path form of low-temperature end, makes under same system wasted work
It obtains final stage turbo-expander 5 to expand at high temperature, obtains more High cooling power, compared with traditional helium refrigeration liquefaction of hydrogen system, saving
Be further added by the second heat exchanger of level-one 9 after the stream throttling of valve 6 further can be reduced to 0 by the mass dryness fraction of the gas after liquefaction, ensure the
The export pipeline of two heat exchangers 9 runs for full liquid phase, compares scheme one, and safety can save equipment cost；Compared to scheme two,
The minimum temperature of entire gas liquefaction system 10 improves, and helps to improve system effectiveness, energy saving.
The above is only the preferred embodiment of the utility model, it is noted that for the common skill of the art
Art personnel can also make several improvements and modifications without departing from the principle of this utility model, these improvements and modifications
Also it should be regarded as the scope of protection of the utility model.
Claims (7)
1. a kind of gas liquefaction system, which is characterized in that single including compressor set, precool heat exchanger device, multistage intermediate turbine precooling
Member, First Heat Exchanger, final stage turbo-expander, the second heat exchanger, throttle valve and cryogenic liquid storage tank；
The outlet of the compressor set is connected to the high-pressure side refrigeration working medium entrance of the precool heat exchanger device, the precool heat exchanger device
The outlet of high-pressure side refrigeration working medium and the high-pressure side refrigeration working medium entrance of the multistage centre turbine pre-cooling unit be connected to, it is described more
The high-pressure side refrigeration working medium outlet of the intermediate turbine pre-cooling unit of grade and the high-pressure side refrigeration working medium entrance of the First Heat Exchanger connect
Logical, the high-pressure side refrigeration working medium outlet of the First Heat Exchanger is connected to the entrance of the final stage turbo-expander, the final stage
The outlet of turbo-expander is connected to the refrigeration working medium entrance of second heat exchanger, and the refrigeration working medium of second heat exchanger goes out
Mouth is connected to the low-pressure side refrigeration working medium entrance of the First Heat Exchanger, the low-pressure side refrigeration working medium outlet of the First Heat Exchanger
It is connected to the low-pressure side refrigeration working medium entrance of the multistage intermediate turbine pre-cooling unit, the multistage intermediate turbine pre-cooling unit
Low-pressure side refrigeration working medium outlet be connected to the low-pressure side refrigeration working medium entrance of the precool heat exchanger device, the precool heat exchanger device it is low
The outlet of pressure side refrigeration working medium is connected to the entrance of the compressor set；
The precool heat exchanger device further includes gas access to be liquefied and gas vent to be liquefied, the precool heat exchanger device it is to be liquefied
Gas vent is connected to the gas access to be liquefied of the multistage intermediate turbine pre-cooling unit, and the multistage intermediate turbine precooling is single
Member gas vent to be liquefied be connected to the gas access to be liquefied of the First Heat Exchanger, the First Heat Exchanger it is to be liquefied
Gas vent is connected to the entrance of the throttle valve, and the outlet of the throttle valve and the gas to be liquefied of second heat exchanger enter
Mouth connection, the gas vent to be liquefied of second heat exchanger are connected to the cryogenic liquid storage tank；
The precool heat exchanger device further includes precooling working medium entrances and precooling sender property outlet.
2. gas liquefaction system as described in claim 1, which is characterized in that further include precooling working medium unit, the precooling work
The outlet of matter unit is connected to the precooling working medium entrances of the precool heat exchanger device, the precooling sender property outlet of the precool heat exchanger device and
The entrance connection of the precooling working medium unit.
3. gas liquefaction system as described in claim 1, which is characterized in that the multistage intermediate turbine pre-cooling unit is heat exchange
The combination of device and turbo-expander.
4. gas liquefaction system as claimed in claim 3, which is characterized in that the multistage intermediate turbine pre-cooling unit be based on
The combination of the heat exchanger and turbo-expander of Cloud's refrigeration cycle or Collins's refrigeration cycle.
5. gas liquefaction system as described in claim 1, which is characterized in that the gas to be liquefied is hydrogen, the precooling
The gas access to be liquefied of heat exchanger is additionally provided with hydrogen filter device and hydrogen purification devices.
6. gas liquefaction system as described in claim 1, which is characterized in that the gas to be liquefied is hydrogen, the precooling
It is filled in the hydrogen paths in heat exchanger and the First Heat Exchanger in heat exchanger, the multistage intermediate turbine pre-cooling unit
There is positive parahydrogen transforming agent.
7. gas liquefaction system as claimed in claim 6, which is characterized in that the gas to be liquefied of the First Heat Exchanger goes out
Mouthful, parahydrogen concentration is more than or equal to 95%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721648442.2U CN207635720U (en) | 2017-11-30 | 2017-11-30 | Gas liquefaction system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201721648442.2U CN207635720U (en) | 2017-11-30 | 2017-11-30 | Gas liquefaction system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207635720U true CN207635720U (en) | 2018-07-20 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107940895A (en) * | 2017-11-30 | 2018-04-20 | 中国科学院理化技术研究所 | Gas liquefaction system |
| CN109764637A (en) * | 2018-12-28 | 2019-05-17 | 中国科学院理化技术研究所 | A kind of novel helium liquefier flow path device |
| CN115420062A (en) * | 2022-08-26 | 2022-12-02 | 中国舰船研究设计中心 | Marine nitrogen liquefaction system and method |
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2017
- 2017-11-30 CN CN201721648442.2U patent/CN207635720U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107940895A (en) * | 2017-11-30 | 2018-04-20 | 中国科学院理化技术研究所 | Gas liquefaction system |
| CN109764637A (en) * | 2018-12-28 | 2019-05-17 | 中国科学院理化技术研究所 | A kind of novel helium liquefier flow path device |
| CN109764637B (en) * | 2018-12-28 | 2020-09-25 | 中国科学院理化技术研究所 | Helium liquefier flow device |
| CN115420062A (en) * | 2022-08-26 | 2022-12-02 | 中国舰船研究设计中心 | Marine nitrogen liquefaction system and method |
| CN115420062B (en) * | 2022-08-26 | 2024-03-22 | 中国舰船研究设计中心 | Marine nitrogen liquefaction system and method |
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Effective date of registration: 20210805 Address after: 1407, 14th floor, building 51, 63 Zhichun Road, Haidian District, Beijing 100083 Patentee after: Beijing Zhongke Fu Hai Low Temperature Technology Co.,Ltd. Address before: No. 29 East Zhongguancun Road, Haidian District, Beijing 100190 Patentee before: Technical Institute of Physics and Chemistry Chinese Academy of Sciences |