CN106052300B - Gas purification system - Google Patents
Gas purification system Download PDFInfo
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- CN106052300B CN106052300B CN201610369547.8A CN201610369547A CN106052300B CN 106052300 B CN106052300 B CN 106052300B CN 201610369547 A CN201610369547 A CN 201610369547A CN 106052300 B CN106052300 B CN 106052300B
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- 238000000746 purification Methods 0.000 title claims abstract description 65
- 239000007788 liquid Substances 0.000 claims abstract description 147
- 239000007789 gas Substances 0.000 claims abstract description 133
- 238000001816 cooling Methods 0.000 claims abstract description 89
- 238000000926 separation method Methods 0.000 claims abstract description 28
- 238000009833 condensation Methods 0.000 claims abstract description 27
- 230000005494 condensation Effects 0.000 claims abstract description 25
- 238000010521 absorption reaction Methods 0.000 claims abstract description 22
- 239000000203 mixture Substances 0.000 claims abstract description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 87
- 229910052757 nitrogen Inorganic materials 0.000 claims description 43
- 238000011084 recovery Methods 0.000 claims description 13
- 238000004064 recycling Methods 0.000 claims description 12
- 238000001035 drying Methods 0.000 claims description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 5
- 238000001179 sorption measurement Methods 0.000 claims description 5
- 230000006837 decompression Effects 0.000 claims description 4
- 230000007704 transition Effects 0.000 claims description 4
- 230000015572 biosynthetic process 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
- 230000008859 change Effects 0.000 claims description 2
- 239000012530 fluid Substances 0.000 claims description 2
- 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 6
- 230000007246 mechanism 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
- 239000007791 liquid phase Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000004321 preservation Methods 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000011810 insulating material Substances 0.000 description 1
- 239000003345 natural gas Substances 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
- 238000011160 research Methods 0.000 description 1
- 230000029058 respiratory gaseous exchange Effects 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- -1 superconduction 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
- 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
-
- 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
Abstract
The invention discloses a kind of gas purification systems, comprising: pre- cooling device, condensation cooling device, gas-liquid separation device and cryogenic absorption device, gas to be purified flows into condensation cooling device after pre- cooling device cools down in advance gas partial liquefaction to be purified is formed gas-liquid mixture, gas-liquid separation device is used to gas-liquid mixture carrying out gas-liquid separation to form preliminary purification gas and condensate liquid, cryogenic absorption device is used to carry out secondary purification to preliminary purification gas to form purified gases, and purified gases and condensate liquid provide cooling cold source together for pre- cooling device.
Description
Technical field
The present invention relates to gas recovery techniques, in particular to a kind of gas purification system.
Background technique
Helium is a kind of colourless, tasteless inert gas, and chemical property is extremely stable, under normal circumstances not with any element
It closes.Helium has very low critical-temperature, is that liquefied gas is most difficult in nature；In all gas, the boiling point of helium is minimum,
The normal boiling point of 4He is only 4.224K.Meanwhile the thermophysical properties such as helium specific heat, thermal conductivity and low-density also with higher are (only
Inferior to hydrogen).Because of its unique hot physical property, helium is widely used in low temperature, superconduction (NMR, MRI etc.), pressurized displacement, welding guarantor
Protect atmosphere, leak detection, breathing gaseous mixture etc., the close phase of the industrial expansions such as it and space technology, semiconductor, superconduction, optical fiber
It closes.
Helium application is so extensive, but helium is a kind of rare non-renewable resources, in air content be only 4~
5.6ppm, and its extraction process is extremely difficult, therefore micro helium is mainly extracted from natural gas.China is a poor helium
Country, most helium derive from external import, with being constantly progressive for cryogenic technique, China to the demand of helium increasingly
Increase, once the outlet of U.S.'s tightening helium, can supply because of no helium leads to existing many relevant scientific researches and medical item at that time
It can not implement, influence very serious.Therefore, in order to save helium resource, it is necessary to carry out recovery purifying to helium resource.
In practical application, in addition to helium, also there is an urgent need to recovery purifying devices for the gases such as hydrogen resource.
In consideration of it, urgent need to resolve above-mentioned technical problem of the present invention.
Summary of the invention
Recycling exhaust gas after purification can re-use the invention mainly solves the technical problem of providing a kind of
Gas purification system.
In order to solve the above technical problems, one technical scheme adopted by the invention is that: a kind of gas purification system is provided,
It include: pre- cooling device, condensation cooling device, gas-liquid separation device and cryogenic absorption device, gas to be purified is through pre- cooling dress
Condensation cooling device is flowed into so that gas partial liquefaction to be purified is formed gas-liquid mixture after setting pre- cooling, and gas-liquid separation device is used
Preliminary purification gas and condensate liquid are formed in gas-liquid mixture is carried out gas-liquid separation, cryogenic absorption device is used for preliminary purification
Gas carries out secondary purification and forms purified gases, and purified gases and condensate liquid provide cooling cold source together for pre- cooling device.
Wherein, gas purification system further comprises throttle valve, and throttle valve is set to gas-liquid separator and pre- cooling device
Between condensate liquid flow through on path for reducing flow through the condensate liquid after throttle valve pressure so that reduce condensate liquid phase transformation
Temperature.
Wherein, pre- cooling device is three stream heat exchangers, for treating purified gases, purified gases and three kinds of condensate liquid streams
Body exchanges heat, and gas to be purified flows into condensation cooling device after pre- cooling device cools down in advance and is cooled to partial liquefaction, through gas
Liquid separating apparatus condensate after gas-liquid separation discharges after flowing through pre- cooling device, and preliminary purification gas is secondary through cryogenic absorption device
The purified gases formed after purification are collected after further flowing through pre- cooling device by bundle pipes.
Wherein, the pressure of gas to be purified is greater than 15bara.
Wherein, after throttle valve is depressured, the pressure of condensate liquid is 0~5bara.
Wherein, after throttle valve is depressured, the pressure of condensate liquid is 0~1.5bara.
Wherein, gas purification system further comprises liquid nitrogen cool-bag, condensation cooling device, gas-liquid separation device and low
Warm adsorbent equipment is soaked in liquid nitrogen cool-bag, gas to be purified condensation cooling device in be cooled to dew-point temperature after to pure
Change gas partial liquefaction and forms gas-liquid mixture.
Wherein, cryogenic absorption device is activated carbon adsorption device.
Wherein, gas purification system further comprises recycling air bag, compressor, oily-water seperating equipment and drying device, is returned
Getter capsule is for storing gas recovery, and gas recovery is after compressor compresses again by oily-water seperating equipment removal oil and after compressing
Then the moisture of generation further goes moisture removal and carbon dioxide to form gas to be purified by drying device.
The beneficial effects of the present invention are: compared with prior art, gas purification system of the present invention utilizes two-stage cooling device
It treats purified gases to cool down, first order cooling device is pre- cooling device, utilizes and mentions in colder environment after purification
It takes the condensate liquid generated in the purified gases and purification process of generation to treat purified gases as cooling cold source to be cooled down in advance, no
Existing waste liquid has only been subjected to the recycling of energy, and compared with the purification system without pre- cooling device or with only
Purified gases are compared as the purification system of pre- cooling device cold source and greatly reduce second level cooling device-condensation cooling device
Cold source loss.To sum up, the present invention provides not only a kind of gas purification system for recycling exhaust gas, and compared to traditional gas
The loss of cold source is greatly saved in purification system, has high economic value.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of one preferred embodiment of gas purification system of the present invention；
Fig. 2 be only using purified gases as pre- cooling device cold source with pressure condition for 150bara, He-N2The dirt of component
For helium, the consumption of liquid nitrogen and the relation curve of helium entrance purity when purifying are condensed to helium；
Fig. 3 is that the relationship of the entrance purity and condensing liquid quantity of helium during purifying helium under the same conditions with Fig. 2 is bent
Line；
Fig. 4 be by purified gases and condensate liquid collectively as pre- cooling device cold source with pressure condition for 150bara, He-
N2For the dirty helium of component, the relation curve of condensate liquid backheat pressure and liquid nitrogen consumption when purifying is condensed to helium.
Specific embodiment
Please refer to Fig. 1, gas purification system 100 of the present invention includes gas recovery pretreatment mechanism, pre- cooling device 10, cold
Solidifying cooling device 20, gas-liquid separation device 30, cryogenic absorption device 40, bundle pipes 50, throttle valve 60, liquid nitrogen cool-bag 70.
It is room temperature processing mechanism that gas recovery, which pre-processes mechanism, specifically includes recycling air bag 81, compressor 82, water-oil separating
Device 83 and drying device 84.Recycling air bag 81 is for storing gas recovery.Pass through pipe between recycling air bag 81 and compressor 82
Road C1 connection, is connected between compressor 82 and oily-water seperating equipment 83 by pipeline C2, oily-water seperating equipment 83 and drying device
It is connected between 84 by pipeline C3.Valve S1 is installed on pipeline C1, when valve S1 is opened, recycles the recycling stored in air bag 81
Gas is delivered to compressor 82 through piping C1, and compressor 82 is used to be pressurized gas recovery, the first purpose of pressurization be rear
Continuous purification provides high-pressure air source, another object is that portion gas is liquefied, it is a part of miscellaneous to be removed by oily-water seperating equipment 83
Matter.Oily-water seperating equipment 83 is used for the moisture generated after gas recovery removal oil and compression, and drying device 84 is further gone
Moisture removal and carbon dioxide form gas to be purified.
Pre- cooling device 10, condensation cooling device 20, gas-liquid separation device 30, cryogenic absorption device 40, bundle pipes 50, section
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- cooling device 10 carries out heat exchange for gas to be purified and purified gases and condensate liquid, will be further detailed hereinafter.Liquid nitrogen is protected
Enough liquid nitrogen are held in warm container 70, condensation cooling device 20, gas-liquid separation device 30 and cryogenic absorption device 40 are impregnated
In liquid nitrogen cool-bag 70, cold source is provided for low temperature.Liquid nitrogen cool-bag 70 can by vacuum-packed form into
The heat preservation of row liquid nitrogen can also keep the temperature liquid nitrogen by way of wrapping up heat-insulating material outside liquid nitrogen cool-bag.
In other examples, the setting of liquid nitrogen cool-bag can also be omitted, and cooling device 20, gas-liquid will be condensed
Separator 30 and cryogenic absorption device 40 are disposed as the device of included cold source to ensure going on smoothly for gas condensation purifying.
Gas to be purified is formed after the just processing unit preliminary treatment of the recovered gas of gas recovery, gas to be purified is dropped in advance
Warm device 10 flows into condensation cooling device 20 so that gas partial liquefaction to be purified is formed gas-liquid mixture, gas-liquid separation after cooling down
Device 30 is used to gas-liquid mixture carrying out gas-liquid separation formation preliminary purification gas and condensate liquid, cryogenic absorption device 40 are used for
Secondary purification is carried out to preliminary purification gas and forms purified gases, purified gases and condensate liquid provide drop together for pre- cooling device
Warm cold source.
Specifically, in the present embodiment, pre- cooling device is three stream heat exchangers, for treating purified gases, purified gases
It exchanges heat with three kinds of fluids of condensate liquid；Pre- cooling device 10 is connected to drying device 84 by pipeline C9, is connected to by pipeline C8
The one end for condensing cooling device 20 is connected to the bottom end of gas-liquid separation device 30 by pipeline C6, is connected to low temperature by pipeline C7 and inhales
One end of adsorption device 40；The other end for condensing cooling device 20 is connected to gas-liquid separation device 30 by pipeline C4；Gas-liquid separation dress
Set the other end that 30 top passes through pipeline C5 connection cryogenic absorption device 40.
The gas to be purified that self-desiccation device 84 exports reaches the pre- cooling in advance of cooling device 10 after pipeline C9, further
It is flowed into after pipeline C8 after condensation cooling device 20 is cooled to dew-point temperature and portion gas therein liquefies, it is mixed in gas-liquid later
The gas to be purified of conjunction state is through in pipeline C4 input gas-liquid separation device 30.Wherein it is preferred to which the pressure of gas to be purified is
15~150bara.Gas-liquid separation device 30 passes through pipeline C5 for preliminary purification gas after gas-liquid mixture is carried out gas-liquid separation
It is input in cryogenic absorption device 40 and is exported condensate liquid by pipeline C6, condensate liquid reaches pre- cooling after flowing through pipeline C6
Device 10 is that pre- cooling device 10 provides cold source, then flows out pre- cooling device 10 and is discharged.It is filled out in cryogenic absorption device 40
Active carbon is filled, is activated carbon adsorption device, active carbon adsorbs remaining impurity in preliminary purification gas under high pressure low temperature to be completed
The secondary purification of purified gases is treated, purified gases are generated after secondary purification, purified gases flow into pre- cooling device through pipeline C7
10 provide cold source for pre- cooling device 10, and purified gases pass through the preservation purified gases of bundle pipes 50 after flowing out pre- cooling device 10.
Since condensate liquid and purified gases are generated under colder environment, their temperature is less than by drying device
The temperature of the gas to be purified of 84 outputs, the two is that pre- cooling device 10 provides cold source jointly, compared to no cold source or only purifying
Gas will all substantially reduce the temperature of the gas to be purified after flowing out pre- cooling device as the situation of cold source, and then reduce cold
Cold source loss required for further cooling down in solidifying cooling device 20.
In the case where not considering leakage heat, this method mainly has two parts for the consumption of liquid nitrogen: condensation purifying consumption and
Cryogenic absorption consumption.Wherein helium condensation is to need to consume liquid since condensation heat exchange device 2 is soaked in liquid nitrogen to the consumption of liquid nitrogen
Gas to be purified is cooled further to dew-point temperature by nitrogen latent heat；The consumption of cryogenic absorption is mainly used for absorbing heat of adsorption, by
It is lower than 1%V in cryogenic absorption device entrance impurity content, therefore the consumption of this part liquid nitrogen is seldom.
Gas to be purified generallys use compressed gas in the process of condensation purification, has biggish pressure, therefore
The pressure of generated condensate liquid is necessarily larger in gas-liquid separation step, and pressure is also between 15~150bara.Work as condensate liquid
Pressure it is bigger, gas-liquid phase transition temperature is higher, is more unfavorable for condensate liquid and releases energy towards the outside.Pass through setting throttle valve 60
Mode improves releasing energy for condensate liquid.Throttle valve 60 is set between gas-liquid separation device 30 and pre- cooling device 10 and condenses
Liquid flows through on path i.e. pipeline C6, and throttle valve 60 flows through the pressure after throttle valve 60 for reducing condensate liquid and then reduces condensation
The phase transition temperature of liquid.As the gas-liquid phase transition temperature that the pressure of condensate liquid is gradually reduced condensate liquid gradually decreases, be conducive to condense
Liquid releases energy towards the outside.The results show, when the pressure of condensate liquid is less than 5bara, the gas to be purified of different purity
Cold source waste needed for purification can at least save 30% when being greater than 15bara compared to the pressure of condensate liquid, it is therefore preferable that
Ground, after throttle valve decompression, the pressure of the condensate liquid is 0~5bara.When the pressure of condensate liquid is less than 1.5bara,
Cold source waste needed for the gas purification to be purified of different purity at least can when being greater than 15bara compared to the pressure of condensate liquid
80% is saved, therefore it is more preferable to ground, after throttle valve decompression, the pressure of the condensate liquid is 0~1.5bara.
In the following, the cold source front and back liquid nitrogen by condensate liquid as pre- cooling device 10 will be compared by taking the purification of dirty helium recovery as an example
The variation of consumption.By taking pressure is the dirty helium of the He-N2 component of 150Bara as an example, when not using condensate liquid as pre- cooling
When the cold source of device 10 utilizes, required amount of liquid nitrogen is such as schemed when condensing purifying amount 100Nm3/h (pure amount of helium about 5g/s) to helium
Shown in 2, it can be seen that with the reduction of dirty helium entrance purity, the amount of liquid nitrogen of condensing heat exchanger consumption increases sharply, 95%V
The amount of liquid nitrogen for needing to consume under purity operating condition is 15.6L/h, and the amount of liquid nitrogen for needing to consume under 90%V purity operating condition is 35L/h,
The amount of liquid nitrogen for needing to consume under 80%V purity operating condition is 80L/h, and the amount of liquid nitrogen for needing to consume under 70%V purity operating condition reaches
About 135L/h.At this point, as shown in figure 3, a large amount of impurity condensate liquid cooling capacity does not obtain benefit while liquid nitrogen consumption increases
With.There is the condensate liquid of nearly 15g/s (about 66L/h) to be wasted when helium purity is 70%, has when helium purity is 80% close
The condensate liquid of 8.5g/s is wasted, and has the condensate liquid of nearly 4g/s to be wasted when helium purity is 90%, when helium purity is
There is the condensate liquid of nearly 2g/s to be wasted when 95%.
After condensate liquid is utilized as the cold source of pre- cooling device, as seen from Figure 4, when backheat pressure is 150bara
When, 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
The dirty helium liquid nitrogen consumption of 13L/h, entrance purity 80%V are 25L/h, the dirty helium liquid nitrogen consumption of entrance purity 70%V
For 38L/h.In conclusion by condensate liquid and purified gases collectively as the cold source of pre- cooling device, even if the backheat of condensate liquid
Pressure does not adjust, relative to being only more than using the consumption that purified gases can also reduce liquid nitrogen as the cold source of pre- cooling device
50%.
Condensate liquid backheat pressure has very big influence for liquid nitrogen consumption, by adjusting the adjustable condensation of throttle 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, is entered
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 lower, and the consumption of liquid nitrogen reduces degree and is more obvious.
When backheat pressure is 1.5bara, the dirty helium liquid nitrogen consumption of entrance purity 95%V is 2.4L/h, relative to
Only liquid nitrogen consumption 98% is reduced using purified gases as the cold source of pre- cooling device；And for the dirty helium of entrance purity 70%V
Liquid nitrogen consumption is 1.5L/h, is reached relative to purified gases are only reduced liquid nitrogen consumption as the cold source of pre- cooling device
98.9%.
More than, only list the embodiment of dirty helium purifying, in practical application, purification system of the present invention can also be used to mention
Pure dirt hydrogen etc..
It is different from the prior art, gas purification system 100 of the present invention is treated purified gases using two-stage cooling device and carried out
Cooling, first order cooling device are pre- cooling device 10, utilize the purified gas for extracting generation in colder environment after purification
The condensate liquid generated in body and purification process treats purified gases as cooling cold source and is cooled down in advance, not only by existing waste liquid
The recycling of energy is carried out, and as pre- compared with the purification system without pre- cooling device or with only purified gases
The purification system of cooling device cold source is lost compared to second level cooling device-condensation cooling device cold source is greatly reduced.It is comprehensive
On, the present invention provides not only a kind of gas purification system for recycling exhaust gas, and significantly compared to traditional gas purification system
The loss of cold source is saved, there is high economic value.
Mode the above is only the implementation of the present invention is not intended to limit the scope of the invention, all to utilize this
Equivalent structure or equivalent flow shift made by description of the invention and accompanying drawing content, it is relevant to be applied directly or indirectly in other
Technical field is included within the scope of the present invention.
Claims (8)
1. a kind of gas purification system, which is characterized in that the gas purification system includes: pre- cooling device, condensation cooling dress
It sets, gas-liquid separation device and cryogenic absorption device, gas to be purified flow into the condensation after the pre- cooling device cools down in advance
The gas partial liquefaction to be purified is formed gas-liquid mixture, the gas-liquid separation device is used for the gas cooling device
Liquid mixture carries out gas-liquid separation and forms preliminary purification gas and condensate liquid, and the cryogenic absorption device is used for described preliminary pure
Change gas and carry out secondary purification formation purified gases, the purified gases and the condensate liquid are that the pre- cooling device mentions together
For the cold source that cools down；The gas purification system further comprises throttle valve, and the throttle valve is set to the gas-liquid separation device
Condensate liquid flows through on path for reducing flowing through the condensate liquid after the throttle valve between the pre- cooling device
Pressure reduces the phase transition temperature of the condensate liquid in turn.
2. gas purification system according to claim 1, which is characterized in that the pre- cooling device is the heat exchange of three plumes
Device, for treating purified gases, three kinds of fluids of purified gases and condensate liquid exchange heat, and the gas to be purified is through the pre- drop
Warm device flows into the condensation cooling device and is cooled to partial liquefaction after cooling down in advance, after the gas-liquid separation device gas-liquid separation
The condensate liquid discharges after flowing through the pre- cooling device, and the preliminary purification gas is through the cryogenic absorption device secondary purification
The purified gases formed afterwards are collected after further flowing through the pre- cooling device by bundle pipes.
3. gas purification system according to claim 1, which is characterized in that the pressure of the gas to be purified is greater than
15bara。
4. gas purification system according to claim 3, which is characterized in that after throttle valve decompression, the condensation
The pressure of liquid is 0~5bara.
5. gas purification system according to claim 4, which is characterized in that after throttle valve decompression, the condensation
The pressure of liquid is 0~1.5bara.
6. gas purification system according to claim 1, which is characterized in that the gas purification system further comprises liquid
Nitrogen cool-bag, the condensation cooling device, gas-liquid separation device and cryogenic absorption device are soaked in the liquid nitrogen cool-bag
In, the gas to be purified is cooled to the gas partial liquefaction shape to be purified after dew-point temperature in the condensation cooling device
At gas-liquid mixture.
7. gas purification system according to claim 1, which is characterized in that the cryogenic absorption device is activated carbon adsorption
Device.
8. gas purification system according to claim 1, which is characterized in that the gas purification system further comprises back
Getter capsule, compressor, oily-water seperating equipment and drying device, the recycling air bag is for storing gas recovery, the recycling gas
The moisture that body is generated by oily-water seperating equipment removal oil and after compressing again after the compressor compresses, then by the drying
Device further goes moisture removal and carbon dioxide to form the gas to be purified.
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