CN106052300A - Gas purification system - Google Patents
Gas purification system Download PDFInfo
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- CN106052300A CN106052300A CN201610369547.8A CN201610369547A CN106052300A CN 106052300 A CN106052300 A CN 106052300A CN 201610369547 A CN201610369547 A CN 201610369547A CN 106052300 A CN106052300 A CN 106052300A
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- gas
- heat sink
- purified
- purification system
- liquid
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- 238000000746 purification Methods 0.000 title claims abstract description 68
- 239000007788 liquid Substances 0.000 claims abstract description 98
- 238000009833 condensation Methods 0.000 claims abstract description 37
- 230000005494 condensation Effects 0.000 claims abstract description 35
- 238000000926 separation method Methods 0.000 claims abstract description 29
- 238000010521 absorption reaction Methods 0.000 claims abstract description 22
- 238000001816 cooling Methods 0.000 claims abstract description 17
- 239000000203 mixture Substances 0.000 claims abstract description 11
- 239000007789 gas Substances 0.000 claims description 123
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 88
- 239000012530 fluid Substances 0.000 claims description 52
- 229910052757 nitrogen Inorganic materials 0.000 claims description 44
- 238000011084 recovery Methods 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 238000001035 drying Methods 0.000 claims description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 6
- 230000036772 blood pressure Effects 0.000 claims description 6
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 5
- 230000007704 transition Effects 0.000 claims description 4
- 238000001179 sorption measurement Methods 0.000 claims description 3
- 230000003213 activating effect Effects 0.000 claims description 2
- 239000002775 capsule Substances 0.000 claims description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 2
- 239000001569 carbon dioxide Substances 0.000 claims description 2
- 230000015572 biosynthetic process Effects 0.000 claims 1
- 239000001307 helium Substances 0.000 description 45
- 229910052734 helium Inorganic materials 0.000 description 45
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 45
- 238000000034 method Methods 0.000 description 7
- 230000007246 mechanism Effects 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000002596 correlated effect Effects 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052756 noble gas Inorganic materials 0.000 description 1
- 239000013307 optical fiber Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000005204 segregation Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009967 tasteless effect Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0235—Heat exchange integration
- F25J1/0242—Waste heat recovery, e.g. from heat of compression
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/30—Helium
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a gas purification system which comprises a pre-cooling device, a condensation cooling device, a gas-liquid separation device and a low-temperature absorption device. Gas to be purified flows into the condensation cooling device after being pre-cooled by the pre-cooling device so as to be liquefied to form a gas-liquid mixture. The gas-liquid separation device is used for conducting gas-liquid separation on the gas-liquid mixture to form primary purified gas and condensation liquid. The low-temperature absorption device is used for conducting secondary purification on the primary purified gas to form purified gas, and the purified gas and the condensation liquid together provide a cooling source for the pre-cooling device.
Description
Technical field
The present invention relates to gas recovery techniques, particularly to a kind of gas purification system.
Background technology
Helium is a kind of colourless, tasteless noble gas, and chemical property is extremely stable, the most not with any element
Close.Helium has the lowest critical temperature, is the gas being most difficult to liquefaction in nature；In all of gas, the boiling point of helium is minimum,
The normal boiling point of 4He is only 4.224K.Meanwhile, helium (only also has the thermophysical propertys such as higher specific heat, thermal conductivity and low-density
Inferior to hydrogen).Because of the hot physical property of its uniqueness, helium is widely used in low temperature, superconduction (NMR, MRI etc.), pressurized displacement, welding guarantor
Protect atmosphere, hunt leak, breathe the aspects such as gaseous mixture, the close phase of industrial expansion such as it and space technology, quasiconductor, superconduction, optical fiber
Close.
Helium application is so extensive, but helium is a kind of rare non-renewable resources, in atmosphere content be only 4～
5.6ppm, and its extraction process is extremely difficult, therefore mainly extracts the helium of trace from natural gas.China is a lean helium
Country, most helium derives from external import, continuous progressive along with cryogenic technique, and China is to the demand of helium day by day
Increasing, once the outlet of helium is tightened up by the U.S., when the time comes can be because causing, without helium supply, scientific research and the medical item that existing many is relevant
Cannot implement, affect the most serious.Therefore, in order to save helium resource, it is necessary to carry out helium resource reclaiming purification.
In actual application, in addition to helium, the gas resource such as hydrogen is also in the urgent need to reclaiming purification devices.
In consideration of it, the present invention needs the above-mentioned technical problem of solution badly.
Summary of the invention
The technical problem that present invention mainly solves is to provide and a kind of can re-use reclaiming after waste gas is purified
Gas purification system.
For solving above-mentioned technical problem, the technical scheme that the present invention uses is: provide a kind of gas purification system, its
Including: pre-heat sink, condensation heat sink, gas-liquid separation device and cryogenic absorption device, gas to be purified is through dress of lowering the temperature in advance
Condensation heat sink is flowed into gas partial liquefaction to be purified to be formed gas-liquid mixture, gas-liquid separation device use after putting pre-cooling
Forming preliminary purification gas and condensed fluid in gas-liquid mixture carries out gas-liquid separation, cryogenic absorption device is for preliminary purification
Gas carries out secondary purification and forms purified gases, and purified gases provides cooling low-temperature receiver for pre-heat sink together with condensed fluid.
Wherein, gas purification system farther includes choke valve, and choke valve is arranged at gas-liquid separator and pre-heat sink
Between the flowing through on path for reducing the pressure flowing through the condensed fluid after choke valve and then reducing the phase transformation of condensed fluid of condensed fluid
Temperature.
Wherein, pre-heat sink is three stream heat exchanger, is used for treating purified gases, purified gases and condensed fluid three kinds stream
Body carries out heat exchange, and gas to be purified flows into condensation heat sink after pre-heat sink is lowered the temperature in advance and is cooled to partial liquefaction, through gas
Liquid separating apparatus condensate after gas-liquid separation discharges after flowing through pre-heat sink, and preliminary purification gas is through cryogenic absorption device secondary
The purified gases formed after purification is collected by bundle pipes after further flowing through pre-heat sink.
Wherein, the pressure of gas to be purified is more than 15bara.
Wherein, after choke valve blood pressure lowering, the pressure of condensed fluid is 0～5bara.
Wherein, after choke valve blood pressure lowering, the pressure of condensed fluid is 0～1.5bara.
Wherein, gas purification system farther includes liquid nitrogen cool-bag, condensation heat sink, gas-liquid separation device and low
Temperature adsorbent equipment is soaked in liquid nitrogen cool-bag, and gas to be purified is treated pure after being cooled to dew point temperature in condensation heat sink
The liquefaction of activating QI body portion forms gas-liquid mixture.
Wherein, cryogenic absorption device is absorbent charcoal adsorber.
Wherein, gas purification system farther includes to reclaim air bag, compressor, oily-water seperating equipment and drying device, returns
Getter capsule is used for storing gas recovery, after gas recovery is gone oil removing to divide by oily-water seperating equipment and compressed again after compressor compresses
The moisture produced, is then gone moisture removal and carbon dioxide to form gas to be purified further by drying device.
The invention has the beneficial effects as follows: compared with prior art, gas purification system of the present invention utilizes two-stage heat sink
Treating purified gases to lower the temperature, first order heat sink is pre-heat sink, and its utilization carries after purification in colder environment
Take the condensed fluid generated in the purified gases of generation and purge process to treat purified gases as cooling low-temperature receiver and carry out pre-cooling, no
Only existing waste liquid has been carried out the recycling of energy, and compared with the purification system without pre-heat sink or with only have
Purified gases is compared as the purification system of pre-heat sink low-temperature receiver and is greatly reduced second level heat sink-condensation heat sink
Low-temperature receiver loss.To sum up, the present invention provide not only a kind of gas purification system reclaiming waste gas, and compared to traditional gas
Purification system is greatly saved the loss of low-temperature receiver, has high economic worth.
Accompanying drawing explanation
Fig. 1 is the structural representation of gas purification system one of the present invention preferred embodiment；
Fig. 2 be only using purified gases as pre-heat sink low-temperature receiver with pressure condition as 150bara, He-N2The dirt of component
Relation curve as a example by helium, to the consumption of liquid nitrogen during helium condensation purification with helium entrance purity；
Fig. 3 be identical with Fig. 2 under conditions of to purify the entrance purity of helium during helium bent with the relation of condensing liquid quantity
Line；
Fig. 4 be by purified gases and condensed fluid collectively as pre-heat sink low-temperature receiver with pressure condition as 150bara, He-
N2Relation curve as a example by the dirty helium of component, to condensed fluid backheat pressure during helium condensation purification with liquid nitrogen consumption.
Detailed description of the invention
Refer to Fig. 1, gas purification system 100 of the present invention includes gas recovery pretreatment mechanism, pre-heat sink 10, cold
Solidifying heat sink 20, gas-liquid separation device 30, cryogenic absorption device 40, bundle pipes 50, choke valve 60, liquid nitrogen cool-bag 70.
Gas recovery pretreatment mechanism is room temperature processing mechanism, specifically includes recovery air bag 81, compressor 82, oil-water separation
Device 83 and drying device 84.Reclaim air bag 81 to be used for storing gas recovery.Reclaim between air bag 81 and compressor 82 by pipe
Road C1 connects, and is connected by pipeline C2, oily-water seperating equipment 83 and drying device between compressor 82 and oily-water seperating equipment 83
Connected by pipeline C3 between 84.Valve S1 is installed on pipeline C1, when valve S1 opens, reclaims the recovery of storage in air bag 81
Gas is delivered to compressor 82 through piping C1, and compressor 82 is for gas recovery supercharging, and one of purpose of supercharging is for rear
Continuous purification provides high-pressure air source, another object is that and is liquefied by portion gas, a part of miscellaneous to be removed by oily-water seperating equipment 83
Matter.The moisture that oily-water seperating equipment 83 produces after gas recovery is gone oil removing to divide and compressed, drying device 84 goes further
Moisture removal and carbon dioxide form gas to be purified.
Pre-heat sink 10, condensation heat sink 20, gas-liquid separation device 30, cryogenic absorption device 40, bundle pipes 50, joint
Stream valve 60 and liquid nitrogen cool-bag 70 collectively form the low temperature purification processes mechanism of gas purification system 100.In the present embodiment,
Pre-heat sink 10 carries out heat exchange for gas to be purified with purified gases and condensed fluid, hereinafter will be further detailed.Liquid nitrogen is protected
Holding abundant liquid nitrogen in temperature container 70, condensation heat sink 20, gas-liquid separation device 30 and cryogenic absorption device 40 soak
In liquid nitrogen cool-bag 70, purify for low temperature and low-temperature receiver is provided.Liquid nitrogen cool-bag 70 can be entered by vacuum-packed form
Liquid nitrogen can also be incubated by the way of at liquid nitrogen cool-bag outer wrapping adiabator by the insulation of row liquid nitrogen.
In other examples, the setting of liquid nitrogen cool-bag can also be omitted, and will condensation heat sink 20, gas-liquid
Segregation apparatus 30 and cryogenic absorption device 40 are disposed as the device carrying low-temperature receiver to guarantee being smoothed out of gas condensation purification.
Forming gas to be purified after the just processing means preliminary treatment of the recovered gas of gas recovery, gas to be purified is through pre-fall
Condensation heat sink 20 is flowed into so that gas partial liquefaction to be purified is formed gas-liquid mixture, gas-liquid separation after temperature device 10 cooling
Device 30 forms preliminary purification gas and condensed fluid for gas-liquid mixture carries out gas-liquid separation, and cryogenic absorption device 40 is used for
Preliminary purification gas carrying out secondary purification and forms purified gases, purified gases provides fall for pre-heat sink together with condensed fluid
Temperature low-temperature receiver.
Specifically, in the present embodiment, pre-heat sink is three stream heat exchanger, is used for treating purified gases, purified gases
Heat exchange is carried out with three kinds of fluids of condensed fluid；Pre-heat sink 10 connects drying device 84 by pipeline C9, is connected by pipeline C8
One end of condensation heat sink 20, by the bottom of pipeline C6 connection gas-liquid separation device 30, is inhaled by pipeline C7 connection low temperature
One end of adsorption device 40；The other end of condensation heat sink 20 connects gas-liquid separation device 30 by pipeline C4；Gas-liquid separation fills
Put the top of 30 other end by pipeline C5 connection cryogenic absorption device 40.
The gas to be purified of self-desiccation device 84 output arrives pre-heat sink 10 after pipeline C9 and lowers the temperature in advance, further
Flow into after pipeline C8 after condensation heat sink 20 is cooled to dew point temperature and portion gas therein is liquefied, mixed in gas-liquid afterwards
The gas to be purified of conjunction state is in pipeline C4 input gas-liquid separation device 30.Wherein it is preferred to, the pressure of gas to be purified is
15～150bara.Gas-liquid separation device 30 passes through pipeline C5 by preliminary purification gas after gas-liquid mixture carries out gas-liquid separation
Inputting to cryogenic absorption device 40 and exported by condensed fluid by pipeline C6, condensed fluid arrives pre-cooling after flowing through pipeline C6
Device 10 provides low-temperature receiver for pre-heat sink 10, then flows out pre-heat sink 10 and is discharged.Cryogenic absorption device 40 is filled out
Filling activated carbon, for absorbent charcoal adsorber, activated carbon adsorbs remaining impurity in preliminary purification gas under high pressure low temperature to be completed
Treating the secondary purification of purified gases, generate purified gases after secondary purification, purified gases flows into pre-heat sink through pipeline C7
10 provide low-temperature receiver for pre-heat sink 10, and purified gases preserves purified gases by bundle pipes 50 after flowing out pre-heat sink 10.
All generating in the environment of colder due to condensed fluid and purified gases, their temperature is less than by drying device
The temperature of gases to be purified of 84 outputs, the two provides low-temperature receiver for pre-heat sink 10 jointly, compares without low-temperature receiver or only purification
Gas all will be substantially reduced, as the situation of low-temperature receiver, the temperature flowing out the gas to be purified after pre-heat sink, and then reduces cold
Low-temperature receiver loss required for lowering the temperature further in solidifying heat sink 20.
Leaking in the case of heat not considering, the method mainly has two parts for the consumption of liquid nitrogen: condensation purification consumption and
Cryogenic absorption consumes.Wherein helium condensation is owing to condensation heat exchange device 2 is soaked in liquid nitrogen to the consumption of liquid nitrogen, needs to consume liquid
Gas to be purified is cooled further to dew point temperature by nitrogen latent heat；The consumption of cryogenic absorption is mainly used in absorbing heat of adsorption, by
In cryogenic absorption device portal impurity content less than 1%V, therefore this part liquid nitrogen consumes seldom.
Gas to be purified generally uses the gas after compression in the flow process that condensation purifies, and has bigger pressure, therefore
In gas-liquid separation step, the pressure of produced condensed fluid is inevitable relatively big, and its pressure is also between 15～150bara.Work as condensed fluid
Pressure the biggest, its gas-liquid phase transition temperature is the highest, is more unfavorable for that condensed fluid releases energy towards the outside.By arranging choke valve 60
Mode improves releasing energy of condensed fluid.Choke valve 60 is arranged between gas-liquid separation device 30 and pre-heat sink 10 condensation
Liquid flow through on path i.e. pipeline C6, choke valve 60 is for reducing the pressure after condensed fluid flows through choke valve 60 and then reducing condensation
The phase transition temperature of liquid.It is gradually lowered along with the pressure of condensed fluid is gradually reduced the gas-liquid phase transition temperature of condensed fluid, is conducive to condensation
Liquid releases energy towards the outside.The results show, when the pressure of condensed fluid is less than 5bara, the gas to be purified of different purity
Low-temperature receiver waste needed for purification at least can save 30% when being more than 15bara compared to the pressure of condensed fluid, it is therefore preferable that
Ground, after described choke valve blood pressure lowering, the pressure of described condensed fluid is 0～5bara.When the pressure of condensed fluid is less than 1.5bara,
Low-temperature receiver waste needed for the gas purification to be purified of different purity at least can when being more than 15bara compared to the pressure of condensed fluid
Saving 80%, therefore it is more preferable to ground, after described choke valve blood pressure lowering, the pressure of described condensed fluid is 0～1.5bara.
Below, will contrast condensed fluid as a example by purifying using dirty helium recovery as liquid nitrogen before and after the low-temperature receiver of pre-heat sink 10
The change of consumption.As a example by the dirty helium of the pressure He-N2 component as 150Bara, when condensed fluid not being lowered the temperature as pre-
When the low-temperature receiver of device 10 utilizes, to amount of liquid nitrogen such as figure required during helium condensation purification amount 100Nm3/h (pure amount of helium about 5g/s)
Shown in 2, it can be seen that along with the reduction of dirty helium entrance purity, the amount of liquid nitrogen of condensing heat exchanger consumption increases sharply, 95%V
Need under purity operating mode consume amount of liquid nitrogen be need under 15.6L/h, 90%V purity operating mode consume amount of liquid nitrogen be 35L/h,
Needing the amount of liquid nitrogen consumed under 80%V purity operating mode is 80L/h, and needs the amount of liquid nitrogen consumed to reach under 70%V purity operating mode
About 135L/h.Now, as it is shown on figure 3, while liquid nitrogen consumption increases, substantial amounts of impurity condensed fluid cold does not obtain profit
With.The condensed fluid having nearly 15g/s (about 66L/h) when helium purity is 70% is wasted, and has near when helium purity is 80%
The condensed fluid of 8.5g/s is wasted, and has the condensed fluid of nearly 4g/s to be wasted when helium purity is 90%, when helium purity is
The condensed fluid having nearly 2g/s when 95% is wasted.
Using condensed fluid as pre-heat sink low-temperature receiver utilize after, as seen from Figure 4, when backheat pressure is 150bara
Time, the dirty helium liquid nitrogen consumption of entrance purity 95%V is 6L/h, and the dirty helium liquid nitrogen consumption of entrance purity 90%V is
13L/h, the dirty helium liquid nitrogen consumption of entrance purity 80%V is 25L/h, the dirty helium liquid nitrogen consumption of entrance purity 70%V
For 38L/h.In sum, by condensed fluid and purified gases collectively as the low-temperature receiver of pre-heat sink, even if the backheat of condensed fluid
Pressure does not adjusts, relative to only being exceeded by the consumption that purified gases can also reduce liquid nitrogen as the low-temperature receiver of pre-heat sink
50%.
Condensed fluid backheat pressure has the biggest impact for liquid nitrogen consumption, can adjust condensation by adjusting choke valve
The backheat pressure of liquid.When backheat pressure is 5bara, the dirty helium liquid nitrogen consumption of entrance purity 95%V is 4.5L/h, entrance
The dirty helium liquid nitrogen consumption of purity 90%V is 4.5L/h, and the dirty helium liquid nitrogen consumption of entrance purity 80%V is 5L/h, enters
The dirty helium liquid nitrogen consumption of mouth purity 70%V is 6L/h.To sum up, when backheat pressure drops to 5bara, the entrance of dirty helium
Purity is the lowest, and it is the most obvious that the consumption of liquid nitrogen reduces degree.
When backheat pressure is 1.5bara, the dirty helium liquid nitrogen consumption of entrance purity 95%V is 2.4L/h, relative to
Only using purified gases as pre-heat sink low-temperature receiver reduce liquid nitrogen consume 98%；And for the dirty helium of entrance purity 70%V
Liquid nitrogen consumption is 1.5L/h, relative to only purified gases being reached as the low-temperature receiver minimizing liquid nitrogen consumption of pre-heat sink
98.9%.
Above, only listing the embodiment of dirty helium purification, in actual application, purification system of the present invention can also be used to carry
Pure dirty hydrogen etc..
Being different from prior art, gas purification system 100 of the present invention utilizes two-stage heat sink to treat purified gases to carry out
Cooling, first order heat sink is pre-heat sink 10, and it utilizes the purified gas extracting generation after purification in colder environment
The condensed fluid generated in body and purge process is treated purified gases as cooling low-temperature receiver and is carried out pre-cooling, not only by existing waste liquid
Carry out the recycling of energy, and as in advance compared with the purification system without pre-heat sink or with only purified gases
The purification system of heat sink low-temperature receiver compares the low-temperature receiver loss greatly reducing second level heat sink-condensation heat sink.Combine
On, the present invention provide not only a kind of gas purification system reclaiming waste gas, and compared to traditional gas purification system significantly
Save the loss of low-temperature receiver, there is high economic worth.
The foregoing is only embodiments of the present invention, not thereby limit the scope of the claims of the present invention, every utilization is originally
Equivalent structure or equivalence flow process that description of the invention and accompanying drawing content are made convert, or are directly or indirectly used in what other were correlated with
Technical field, is the most in like manner included in the scope of patent protection of the present invention.
Claims (9)
1. a gas purification system, it is characterised in that described gas purification system includes: pre-heat sink, condensation cooling dress
Put, gas-liquid separation device and cryogenic absorption device, gas to be purified flows into described condensation after described pre-heat sink is lowered the temperature in advance
Heat sink is to form gas-liquid mixture by described gas partial liquefaction to be purified, and described gas-liquid separation device is for by described gas
Liquid mixture carries out gas-liquid separation and forms preliminary purification gas and condensed fluid, and described cryogenic absorption device is for described the purest
Activating QI body carries out secondary purification and forms purified gases, and described purified gases carries for described pre-heat sink together with described condensed fluid
For cooling low-temperature receiver.
Gas purification system the most according to claim 1, it is characterised in that described gas purification system farther includes joint
Stream valve, described choke valve is arranged at flowing through of condensed fluid between described gas-liquid separation device and described pre-heat sink and uses on path
In the pressure of the described condensed fluid reduced after flowing through described choke valve and then reduce the phase transition temperature of described condensed fluid.
Gas purification system the most according to claim 1, it is characterised in that described pre-heat sink is three plume heat exchange
Device, is used for treating purified gases, purified gases and three kinds of fluids of condensed fluid and carries out heat exchange, and described gas to be purified is through described pre-fall
Temperature device flows into described condensation heat sink after lowering the temperature in advance and is cooled to partial liquefaction, after described gas-liquid separation device gas-liquid separation
Described condensed fluid discharges after flowing through described pre-heat sink, and described preliminary purification gas is through described cryogenic absorption device secondary purification
The purified gases of rear formation is collected by bundle pipes after further flowing through described pre-heat sink.
Gas purification system the most according to claim 1, it is characterised in that the pressure of described gas to be purified is more than
15bara。
Gas purification system the most according to claim 4, it is characterised in that after described choke valve blood pressure lowering, described condensation
The pressure of liquid is 0～5bara.
Gas purification system the most according to claim 5, it is characterised in that after described choke valve blood pressure lowering, described condensation
The pressure of liquid is 0～1.5bara.
Gas purification system the most according to claim 1, it is characterised in that described gas purification system farther includes liquid
Nitrogen cool-bag, described condensation heat sink, gas-liquid separation device and cryogenic absorption device are soaked in described liquid nitrogen cool-bag
In, described gas to be purified is described gas partial liquefaction shape to be purified after being cooled to dew point temperature in described condensation heat sink
Become gas-liquid mixture.
Gas purification system the most according to claim 1, it is characterised in that described cryogenic absorption device is activated carbon adsorption
Device.
Gas purification system the most according to claim 1, it is characterised in that described gas purification system farther includes back
Getter capsule, compressor, oily-water seperating equipment and drying device, described recovery air bag is used for storing gas recovery, described recovery gas
The moisture that body produces after being gone oil removing to divide by oily-water seperating equipment and compressed again after described compressor compresses, is then dried by described
Device goes moisture removal and carbon dioxide to form described gas to be purified further.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114111219A (en) * | 2021-11-02 | 2022-03-01 | 深圳供电局有限公司 | Gas purification device based on low-temperature refrigerator |
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