CN106352657A - System and method for extracting helium gas from flashing steam - Google Patents
System and method for extracting helium gas from flashing steam Download PDFInfo
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- CN106352657A CN106352657A CN201610722780.XA CN201610722780A CN106352657A CN 106352657 A CN106352657 A CN 106352657A CN 201610722780 A CN201610722780 A CN 201610722780A CN 106352657 A CN106352657 A CN 106352657A
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- Prior art keywords
- helium
- product
- gas
- raw material
- nitrogen product
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- 239000001307 helium Substances 0.000 title claims abstract description 129
- 229910052734 helium Inorganic materials 0.000 title claims abstract description 129
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 title claims abstract description 129
- 239000007789 gas Substances 0.000 title claims abstract description 74
- 238000000034 method Methods 0.000 title claims abstract description 41
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 307
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 153
- 239000007788 liquid Substances 0.000 claims abstract description 63
- 239000002994 raw material Substances 0.000 claims abstract description 57
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 40
- 239000012071 phase Substances 0.000 claims abstract description 37
- 239000007791 liquid phase Substances 0.000 claims abstract description 33
- 230000018044 dehydration Effects 0.000 claims abstract description 17
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 17
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 17
- 238000000926 separation method Methods 0.000 claims abstract description 11
- 238000001816 cooling Methods 0.000 claims description 64
- 239000000284 extract Substances 0.000 claims description 48
- 238000009833 condensation Methods 0.000 claims description 45
- 230000005494 condensation Effects 0.000 claims description 45
- 239000006200 vaporizer Substances 0.000 claims description 38
- 238000010438 heat treatment Methods 0.000 claims description 35
- 239000001257 hydrogen Substances 0.000 claims description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 9
- 238000012545 processing Methods 0.000 claims description 8
- 150000002431 hydrogen Chemical class 0.000 claims description 3
- 238000009795 derivation Methods 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 238000000605 extraction Methods 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 230000008676 import Effects 0.000 description 9
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 8
- 230000008569 process Effects 0.000 description 6
- 238000004891 communication Methods 0.000 description 5
- 230000008859 change Effects 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000003345 natural gas Substances 0.000 description 4
- 239000003507 refrigerant Substances 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 238000005481 NMR spectroscopy Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000009471 action Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000000315 cryotherapy Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052756 noble gas Inorganic materials 0.000 description 1
- 150000002835 noble gases Chemical class 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/028—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of noble gases
- F25J3/029—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of noble gases of helium
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- 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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
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- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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- 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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
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- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
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- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
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- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
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- 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
- F25J2215/04—Recovery of liquid products
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- 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
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- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
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- F25J2270/00—Refrigeration techniques used
- F25J2270/12—External refrigeration with liquid vaporising loop
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- 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
- F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
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- F25J2270/00—Refrigeration techniques used
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
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- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/902—Details about the refrigeration cycle used, e.g. composition of refrigerant, arrangement of compressors or cascade, make up sources, use of reflux exchangers etc.
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- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
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Abstract
The embodiment of the invention provides a system and method for extracting helium gas from flashing steam and relates to the technical field of gas separation. The method includes the steps that a pressurized flashing steam raw material is cooled to obtain a liquid phase raw material and a gas phase raw material; the liquid phase raw material and the gas phase raw material are separated, the gas phase raw material is exported, and a crude helium gas product is obtained; the crude helium gas product is subjected to dehydrogenation, dehydration and denitrification, and a refined helium gas product is obtained; the liquid phase raw material is heated to obtain a liquefied natural gas raw material and a gas nitrogen raw material, the gas nitrogen raw material is cooled and separated, and an initial liquid nitrogen product and an initial gas nitrogen product are obtained; the obtained initial gas nitrogen product is heated to obtain a gas nitrogen product, and the initial liquid nitrogen product is exported to obtain a liquid nitrogen product. According to the system and method for extracting the helium gas from the flashing steam, the gas nitrogen product, the liquid nitrogen product, the liquefied natural gas product and other additional products can be extracted while the flashing steam is used for extracting the high-purity helium gas, the extraction process is simple and rapid, energy consumption is low, and good economic benefits are achieved.
Description
Technical field
The present invention relates to gas separation technique field, extract system and the side of helium in particular to a kind of flashed vapour
Method.
Background technology
Helium is one kind of noble gases, is important strategic materials, as a kind of protective gas and cryotherapy agent
There is in terms of space flight, national defence, semiconductor production, nuclear magnetic resonance, NMR and gas leak detection very important purposes.
Helium is primarily present in natural gas, extracts the key industry source that helium is current helium, at present from natural gas
The method extracting helium from natural gas mainly has the methods such as cryogenic separation, membrance separation and pressure-variable adsorption.But existing at present carry
Mostly there is extraction process complexity, power consumption height and extract the low problem of raw material availability in the method taking helium.
Content of the invention
In view of this, the purpose of the embodiment of the present invention is the system and method providing a kind of flashed vapour to extract helium to change
Kind extraction process flow process, lowers power consumption, improves resource utilization.
To achieve the above object, the flashed vapour that the present invention provides extracts the following institute of technical scheme of the system of helium
State:
A kind of flashed vapour extracts the system of helium, comprising: propose helium tower, main heat exchanger, the first condensation separator, the first condensation
Device and the first vaporizer, described first condenser be arranged at described in carry the top of helium tower, described first vaporizer is arranged at described
Carry the bottom of helium tower, described main heat exchanger is provided with the first cooling circuit and the second cooling circuit；
Described first cooling circuit, described first vaporizer, described second cooling circuit, described carry helium tower, described first
Condenser and described first condensation separator are sequentially communicated, and described first condensation separator is also connected with the described helium tower that carries；
Described first cooling circuit, described first vaporizer, described second cooling circuit and described first condenser are used for
Flashed vapour raw material after pressurization is carried out by cooling successively obtains liquid phase feed and phase feed, described phase feed include helium,
Nitrogen and hydrogen, described first condensation separator is used for described liquid phase feed and phase feed being carried out separate, and will separate
Described phase feed afterwards derives and obtains rough helium product.
Flashed vapour as above extracts the system of helium it is preferable that the system that flashed vapour extracts helium also includes denitrogenation
Tower, the second condensation separator, the second condenser and the second vaporizer, described second condenser is arranged at described second condensation separation
The top of device, described second vaporizer is arranged at the bottom of described second condensation separator, and described main heat exchanger is additionally provided with
Three cooling circuits and the first heating circuit；
The described bottom carrying helium tower, described second vaporizer, described 3rd cooling circuit, described denitrification column, described second
Condenser and described second condensation separator are sequentially communicated, described second condensation separator respectively with described first heating circuit and
Described denitrification column connection；
Described second vaporizer is gentle for the described liquid phase feed heating after separation is obtained liquefied natural gas (LNG) feed
Nitrogen raw material, described 3rd cooling circuit and described second condenser are used for described gas nitrogen raw material is cooled down successively, and described the
Two condensation separators are used for the gas nitrogen raw material after cooling is carried out separating, and obtain initial liquid nitrogen product and initial gas nitrogen product, institute
State initial liquid nitrogen product and include the first initial liquid nitrogen product and the second initial liquid nitrogen product, described first heating circuit is used for institute
State the heating of initial gas nitrogen product and obtain gas nitrogen product, described first initial liquid nitrogen product is imported into described denitrification column and thinks described taking off
Nitrogen tower provides cold, and described second initial liquid nitrogen product is exported to obtain liquid nitrogen product.
Flashed vapour as above extracts the system of helium it is preferable that the system that flashed vapour extracts helium also includes the 4th
Cooling circuit, described 4th cooling circuit is connected with the bottom of described denitrification column, for will be cold for the liquefied natural gas (LNG) feed obtaining
, and derive and obtain liquefied natural gas product but.
Flashed vapour as above extracts the system of helium it is preferable that the system that flashed vapour extracts helium also includes first
Compressor, the two ends of described first compressor respectively carry helium tower and described denitrification column connects with described, for for described
Carry helium tower and described denitrification column provides power.
Flashed vapour as above extracts the system of helium it is preferable that the system that flashed vapour extracts helium also includes dehydrogenation
Device, dehydration device and nitrogen rejection facility, described main heat exchanger is additionally provided with the second heating circuit, described second heating circuit and institute
State the first condensation separator connection, described second heating circuit, described dehydrogenation unit, described dehydration device and described denitrogenation dress
Put and be sequentially communicated, so that the rough helium product obtaining is carried out dehydrogenation, dehydration and denitrogenation processing, obtain purified nitrogen product.
Flashed vapour as above extracts the system of helium it is preferable that the system that flashed vapour extracts helium also includes second
Compressor, described second compressor is connected with described main heat exchanger, and described second compressor is used for mix refrigerant is pressed
Contracting is to provide cold to described main heat exchanger.
The technical scheme that the flashed vapour that the present invention provides extracts the method for helium is as described below:
A kind of method that flashed vapour extracts helium, methods described includes:
Cooling is carried out to the flashed vapour raw material after pressurization and obtains liquid phase feed and phase feed, described phase feed includes helium
Gas, nitrogen and hydrogen；
The liquid phase feed obtaining is separated with phase feed；
The phase feed isolated is derived and obtains rough helium product.
Flashed vapour as above extracts the method for helium it is preferable that methods described also includes:
The liquid phase feed obtaining heating is obtained liquefied natural gas (LNG) feed gentle nitrogen raw material；
The gas nitrogen raw material obtaining is cooled down；
Gas nitrogen raw material after cooling is carried out separating, obtains initial liquid nitrogen product and initial gas nitrogen product, described initial liquid
Nitrogen product includes the first initial liquid nitrogen product and the second initial liquid nitrogen product；
Obtain gas nitrogen product to obtaining the heating of initial gas nitrogen product；
First initial liquid nitrogen product is imported described denitrification column provides cold for described denitrification column, and described second initial liquid
Nitrogen product is derived and is obtained liquid nitrogen product.
Flashed vapour as above extracts the method for helium it is preferable that methods described also includes:
Derive after the liquefied natural gas (LNG) feed obtaining is cooled down, obtain liquefied natural gas product.
Flashed vapour as above extracts the method for helium it is preferable that methods described also includes:
The rough helium product obtaining is carried out dehydrogenation, dehydration and denitrogenation processing, obtains purified nitrogen product.
Compared with prior art, the system and method for the flashed vapour extraction helium of the present invention has the advantages that
The flashed vapour that the present invention provides extracts the system and method for helium, can be by entering to the flashed vapour in liquefied natural gas
Row recycles, and very easily extracts helium product, extraction process is simple and convenient, effectively reduces energy consumption, improves technique
Flow process.
Further, flashed vapour can be made full use of, while extracting helium using flashed vapour, also extractable
To gas nitrogen product, liquid nitrogen product and liquefied natural gas product etc., effectively increase the utilization rate of resource, reducing energy consumption, lifting
Economic benefit.
Further, dehydrogenation, dehydration and denitrogenation processing can be carried out to the helium product extracting and obtain highly purified refined nitrogen
Gas product.
For enabling the above objects, features and advantages of the present invention to become apparent, preferred embodiment cited below particularly, and coordinate
Appended accompanying drawing, is described in detail below.
Brief description
In order to be illustrated more clearly that the technical scheme of the embodiment of the present invention, below will be attached to use required in embodiment
Figure is briefly described it will be appreciated that the following drawings illustrate only certain embodiments of the present invention, and it is right to be therefore not construed as
The restriction of scope, for those of ordinary skill in the art, on the premise of not paying creative work, can also be according to this
A little accompanying drawings obtain other related accompanying drawings.
Fig. 1 extracts the structural representation of the system of helium for the flashed vapour that present pre-ferred embodiments provide.
Fig. 2 extracts the structural representation of the system of helium for the another flashed vapour that present pre-ferred embodiments provide.
The flow chart that Fig. 3 extracts the method for helium for the flashed vapour that present pre-ferred embodiments provide.
Main element symbol description
Carry helium tower 110, main heat exchanger 120, the first cooling circuit 121, the second cooling circuit 122, the 3rd cooling circuit
123, the first heating circuit 124, the 4th cooling circuit 125, the second heating circuit 126, the first condensation separator 130, first is cold
Condenser 140, the first vaporizer 150, denitrification column 160, the second condensation separator 170, the second condenser 180, the second vaporizer
190, the first compressor 200, the second compressor 210, dehydrogenation unit 220, dehydration device 230, nitrogen rejection facility 240.
Specific embodiment
Purpose, technical scheme and advantage for making the embodiment of the present invention are clearer, below in conjunction with the embodiment of the present invention
In accompanying drawing, the technical scheme in the embodiment of the present invention is clearly and completely described it is clear that described embodiment is
The a part of embodiment of the present invention, rather than whole embodiments.The present invention generally described and illustrated in accompanying drawing herein is implemented
The assembly of example can be arranged with various different configurations and design.
Therefore, below the detailed description of the embodiments of the invention providing in the accompanying drawings is not intended to limit claimed
The scope of the present invention, but be merely representative of the selected embodiment of the present invention.Based on the embodiment in the present invention, this area is common
The every other embodiment that technical staff is obtained under the premise of not making creative work, broadly falls into the model of present invention protection
Enclose.
It should also be noted that similar label and letter expression similar terms in following accompanying drawing, therefore, once a certain Xiang Yi
It is defined in individual accompanying drawing, then do not need it to be defined further and explains in subsequent accompanying drawing.
In describing the invention, it should be noted that term " " center ", " on ", D score, "left", "right", " vertical ",
The orientation of instruction such as " level ", " interior ", " outward " or position relationship are based on orientation shown in the drawings or position relationship, or should
Orientation or position relationship that invention product is usually put when using, are for only for ease of the description present invention and simplify description, and not
It is instruction or the hint device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore not
It is understood that as limitation of the present invention.Additionally, term " first ", " second ", " the 3rd " etc. are only used for distinguishing description, and can not manage
Solve as indicating or implying relative importance.
Additionally, the term such as term " level ", " vertical ", " pendency " is not offered as requiring part abswolute level or pendency, and
It is to be slightly tilted.As " level " only refers to for its direction relatively " vertical " more level, it is not this structure of expression
Must be fully horizontal, but can be slightly tilted.
In describing the invention in addition it is also necessary to explanation, unless otherwise clearly defined and limited, term " setting ",
" installation ", " being connected ", " connection " should be interpreted broadly, for example, it may be being fixedly connected or being detachably connected, or one
Body ground connects；Can be to be mechanically connected or electrically connect；Can be joined directly together it is also possible to by intermediary indirect
It is connected, can be the connection of two element internals.For the ordinary skill in the art, can be with concrete condition understanding
State term concrete meaning in the present invention.
Refer to Fig. 1, the flashed vapour that present pre-ferred embodiments provide extracts the structural representation of the system of helium, in figure
The direction of arrow represent the flow direction of medium.As shown in figure 1, flashed vapour extraction helium provided in an embodiment of the present invention is
System includes and carries helium tower 110, main heat exchanger 120, the first condensation separator 130, the first condenser 140 and the first vaporizer 150,
Main heat exchanger 120 is provided with the first cooling circuit 121 and the second cooling circuit 122.
First condenser 140 is arranged at the top carrying in helium tower 110, and the first vaporizer 150 is arranged at and carries in helium tower 110
Bottom.First cooling circuit 121 is used for the flashed vapour raw material after importing pressurization, the first cooling circuit 121, the first vaporizer 150,
Second cooling circuit 122, carry helium tower 110, the first condenser 140 and the first condensation separator 130 and be sequentially communicated.
Wherein, the first cooling circuit 121, the first vaporizer 150 and the second cooling circuit 122 are used for the flash distillation after pressurization
Gas raw material carries out cooling successively and obtains liquid phase feed and phase feed, described phase feed mainly include helium, part nitrogen with
And a small amount of hydrogen, the first condensation separator 130 is used for the liquid phase feed obtaining and phase feed are carried out separately, to incite somebody to action
The phase feed arriving derives from the outlet of the first condensation separator 130, draws the rough helium comprising part nitrogen and a small amount of hydrogen
Gas product.
Specifically, flashed vapour raw material can by compressor compresses to 5.2mpa about and import the first of main heat exchanger 120
Cooling circuit 121, and be cooled to import after -101 DEG C about in the first cooling circuit 121 of main heat exchanger 120 and carry helium tower 110
First vaporizer 150 of bottom is simultaneously continued cool to -120 DEG C about by the first vaporizer 150, and flashed vapour raw material is being steamed by first
Thermal source is provided for the first vaporizer 150 while sending out device 150 cooling.
Flashed vapour raw material is after being cooled to -120 DEG C about by the first vaporizer 150, then imports in main heat exchanger 120
Two cooling circuits 122 are simultaneously continuously cooled by and reach -140 DEG C about.Second cooling circuit 122 and carrying is provided between helium tower 110
One choke valve, be cooled to -140 DEG C about of flashed vapour raw material through this choke valve reducing pressure by regulating flow to 2.6mpa about after enter and carry
Helium tower 110 being enriched in the first condenser 140 of tower top, and condensed to -180 DEG C about by the first condenser 140, obtain liquid
Phase raw material and phase feed, liquid phase feed and phase feed are separated through the first condensation separator 130 again.Wherein,
Liquid phase feed mainly includes liquid nitrogen and liquefied natural gas, and phase feed is then main inclusion helium, part nitrogen and a small amount of hydrogen
The mixing gas of gas.Liquid phase feed is then back to, as backflow, the bottom carrying helium tower 110, and provides cold for carrying helium tower 110,
And phase feed then can be exported the rough helium product obtaining comprising part nitrogen and a small amount of hydrogen.
In the present embodiment, flashed vapour raw material first passes through compressor compresses to 5.2mpa, then again through choke valve
Reducing pressure by regulating flow to 2.6mpa about after enter carry helium tower 110, so can achieve throttling control.Certainly, flashed vapour raw material can also
Directly it is compressed to 2.6mpa when initial.To first pass through compressor compresses to 5.2mpa, then again through choke valve
Reducing pressure by regulating flow to 2.6mpa about mode be optimal.
Flashed vapour in liquefied natural gas can be recycled by the system that above-mentioned flashed vapour extracts helium, very
Easily extract helium product, extraction process is simple and convenient, effectively reduces energy consumption, improves technological process, however, extracting
Product is more single, will certainly cause the waste of resource.
In consideration of it, the system that flashed vapour provided in an embodiment of the present invention extracts helium is also entered in above-mentioned basic unit
The improvement of one step.Refer to Fig. 2, flashed vapour provided in an embodiment of the present invention extract helium system also include denitrification column 160,
Second condensation separator 170, the second condenser 180 and the second vaporizer 190, main heat exchanger 120 is additionally provided with the 3rd and cools back
Road 123, the first heating circuit 124 and the 4th cooling circuit 125.
Second condenser 180 is arranged at the top in denitrification column 160, and the second vaporizer 190 is arranged in denitrification column 160
Bottom.Carry the bottom of helium tower 110, the second vaporizer 190, the 3rd cooling circuit 123, denitrification column 160, the second condenser 180 and
Second condensation separator 170 is sequentially communicated, the second condensation separator 170 also respectively with the first heating circuit 124 and denitrification column 160
Connection, the 4th cooling circuit 125 is connected with the bottom of denitrification column 160.
Wherein, the second vaporizer 190 obtains liquefied natural gas (LNG) feed gentle nitrogen raw material for heating liquid phase feed, and the 3rd
Cooling circuit 123 and the second condenser 180 are used for the gas nitrogen raw material obtaining is cooled down successively, the second condensation separator 170
For carrying out separating to the gas nitrogen raw material after cooling, obtain initial liquid nitrogen product and initial gas nitrogen product, initial liquid nitrogen product bag
Include the first initial liquid nitrogen product and the second initial liquid nitrogen product, the first heating circuit 124 is used for adding to obtaining initial gas nitrogen product
Heat obtains gas nitrogen product, and the first initial liquid nitrogen product is used for importing denitrification column 160 for denitrification column 160 offer cold, and second is initial
Liquid nitrogen product obtains liquid nitrogen product for derivation.
Specifically, the liquid phase feed (mainly liquid nitrogen and liquefied natural gas) being back to the bottom carrying helium tower 110 can import
To the second vaporizer 190 in communication, and -140 DEG C about, in this course, liquid are heated to by the second vaporizer 190
Change natural gas and keep liquid, and liquid nitrogen is then mainly heated to form gaseous state (i.e. gas nitrogen raw material).Liquefied natural gas gentle nitrogen raw material warp
Cross after the 3rd cooling circuit 123 on main heat exchanger 120 is cooled to -151 DEG C about and enter denitrification column 160, liquefied natural gas
Then it is back to the bottom of denitrification column 160 and derives after entering the 4th cooling circuit 125 cooling, obtain liquefied natural gas product.And
Gas nitrogen raw material then enters the second condenser 180 and is cooled to -174 DEG C about, and now, gas nitrogen feedstock portions are cooled into liquid nitrogen,
Part keeps gaseous state.Then gas nitrogen raw material imports the second condensation separator 170 and carries out separating, and isolates initial liquid nitrogen product (liquid
Body nitrogen) and initial gas nitrogen product (gaseous nitrogen), initial gas nitrogen product is imported in communication by the second condensation separator 170 top
First heating circuit 124 simultaneously is heated to after room temperature deriving by the first heating circuit 124, that is, obtain the gas nitrogen product of room temperature.And just
The bottom through the second condensation separator 170 for the part in beginning liquid nitrogen product imports denitrification column 160 in communication, and is denitrogenation
Tower 160 provides cold, and another part is then derived from the second condensation separator 170, obtains liquid nitrogen product.
Using above-mentioned set-up mode, while extracting helium using flashed vapour, can also extract obtain gas nitrogen product,
Liquid nitrogen product and liquefied natural gas product etc., effectively increase the utilization rate of resource, reducing energy consumption, lift economic benefit.
Refer to Fig. 2, in the present embodiment, the system that flashed vapour extracts helium is provided with the first compressor 200 and the second pressure
Contracting machine 210.
Wherein, after the entrance of the first compressor 200 is connected with main heat exchanger 120 more respectively with put forward helium tower 110 and denitrification column
160 connection, the outlet of the first compressor 200 connect with main heat exchanger 120 after more respectively with carry helium tower 110 and denitrification column 160 company
Logical.First compressor 200 is used for compressed nitrogen, nitrogen is compressed to entrance main heat exchanger 120 liquefaction after 4mpa and is cooled to -162
DEG C effect, is then divided into two strands, one enters and carries the low-temperature receiver as the first condenser 140 for the top of helium tower 110, another burst of entrance
The top of denitrification column 160 is as the low-temperature receiver of the second condenser 180.Liquid nitrogen provides low-temperature receiver and converges entrance main heat exchanger after gasifying
120 re-heats enter the first compressor 200 and compress, thus completing entirely to circulate.In the process, the first compressor 200 is acceptable
There is provided power for denitrification column 160 with carrying helium tower 110.
The entrance and exit of the second compressor 210 is all connected with main heat exchanger 120, thus forming a circulation.Second pressure
Contracting machine 210 is used for mix refrigerant is compressed, and adopts three-level throttling refrigeration, and mix refrigerant is by the second compressor 210
Be compressed to 4mpa about after enter main heat exchanger 120, for main heat exchanger 120 provide cold, by a series of heat exchange and section
After stream, after low pressure mix refrigerant return main heat exchanger 120 re-heat going out main heat exchanger 120, it is again introduced into the second compressor 210
It is compressed, thus completing entirely to circulate.
Further, the system that the flashed vapour that the present invention provides extracts helium is additionally provided with dehydrogenation unit 220, dehydration device
230 and nitrogen rejection facility 240, main heat exchanger 120 is additionally provided with the second heating circuit 126.First condensation separator 130, second adds
Hot loop 126, dehydrogenation unit 220, dehydration device 230 and nitrogen rejection facility 240 are sequentially communicated.So, from the first condensation separation
The rough helium product that device 130 is derived can carry out dehydrogenation, dehydration and denitrogenation processing after the heating, obtains highly purified purified nitrogen
Product.
Please refer to Fig. 2 and 3, the embodiment of the present invention additionally provides a kind of method that flashed vapour extracts helium, this flash distillation
Air stripping takes the method for helium to be applied to the system that the flashed vapour shown in Fig. 2 extracts helium, below by the idiographic flow shown in Fig. 3
It is described in detail.
Step s301: cooling is carried out to the flashed vapour raw material after pressurization and obtains liquid phase feed and phase feed.
The method that the flashed vapour that the present embodiment provides extracts helium, is applied to the flashed vapour shown in above-mentioned Fig. 2 and extracts helium
System.When extracting helium, first flashed vapour raw material by compressor compresses to 5.2mpa, and can be imported main heat exchange
First cooling circuit 121 of device 120, imports after being cooled to -101 DEG C about and carry helium tower 110 bottom in the first cooling circuit 121
The first vaporizer 150 and continued cool to -120 DEG C about by the first vaporizer 150, flashed vapour raw material is by the first vaporizer
There is provided thermal source for the first vaporizer 150 during 150 cooling simultaneously.
Flashed vapour raw material is after being cooled to -120 DEG C about by the first vaporizer 150, then imports in main heat exchanger 120
Two cooling circuits 122 are simultaneously continuously cooled by and reach -140 DEG C about.Second cooling circuit 122 and carrying is provided between helium tower 110
One choke valve, be cooled to -140 DEG C about of flashed vapour raw material through this choke valve reducing pressure by regulating flow to 2.6mpa about after enter and carry
Helium tower 110 being enriched in the first condenser 140 of tower top, and condensed to -180 DEG C about by the first condenser 140, obtain liquid
Phase raw material and phase feed, wherein, phase feed can include helium, nitrogen and hydrogen.
Step s302: liquid phase feed is separated with phase feed, derives phase feed and obtain rough helium product.
After obtaining liquid phase feed and phase feed, liquid phase feed and phase feed are imported in the first condensation separator 130
And liquid phase feed and phase feed are separated.Wherein, liquid phase feed mainly includes liquid nitrogen and liquefied natural gas, phase feed
It is then the main mixing gas including helium, part nitrogen and a small amount of hydrogen.
Liquid phase feed is then back to, as backflow, the bottom carrying helium tower 110, and provides cold for carrying helium tower 110, and gas
Phase raw material then can be exported the rough helium product obtaining comprising part nitrogen and a small amount of hydrogen.
Step s303: dehydrogenation, dehydration and denitrogenation processing are carried out to rough helium product, obtains purified nitrogen product.
After the rough helium product obtaining is directed into the second heating circuit 126 and is heated by the second heating circuit, dehydrogenation fills
Put 220, dehydration device 230 and nitrogen rejection facility 240 carries out dehydrogenation, dehydration and denitrogenation processing respectively, remove rough helium product
In nitrogen, hydrogen and moisture etc., thus reaching highly purified purified nitrogen product.
Step s304: liquid phase feed heating is obtained liquefied natural gas (LNG) feed gentle nitrogen raw material, gas nitrogen raw material is carried out cold
But and separately, initial liquid nitrogen product and initial gas nitrogen product are obtained.
After liquid phase feed is back to the bottom carrying helium tower 110, it is imported into the second evaporation connecting with the bottom carrying helium tower 110
In device 190 and it is heated to -140 DEG C about by the second vaporizer 190, obtains liquefied natural gas (LNG) feed gentle nitrogen raw material, liquefy sky
So gas gentle nitrogen raw material enters denitrogenation after the 3rd cooling circuit 123 on main heat exchanger 120 is cooled to -151 DEG C about
Tower 160.
Wherein, liquefied natural gas is then back to the bottom of denitrification column 160 and leads after entering the 4th cooling circuit 125 cooling
Go out, obtain liquefied natural gas product.And gas nitrogen raw material then enters the second condenser 180 and is cooled to -174 DEG C about, now, gas
Nitrogen feedstock portions are cooled into liquid nitrogen, and part keeps gaseous state, are then directed to the second condensation separator 170 and carry out separating, separate
Go out initial liquid nitrogen product (liquid nitrogen) and initial gas nitrogen product (gaseous nitrogen).
Step s305: obtain gas nitrogen product to obtaining the heating of initial gas nitrogen product, initial liquid nitrogen product is derived and obtains liquid
Nitrogen product.
Initial gas nitrogen product is imported the first heating circuit 124 in communication and given by the second condensation separator 170 top
First heating circuit 124 is derived after being heated to room temperature, that is, obtain the gas nitrogen product of room temperature.And the part in initial liquid nitrogen product
Bottom through the second condensation separator 170 imports denitrification column 160 in communication, and provides cold, another portion for denitrification column 160
Dividing then derives from the second condensation separator 170, obtains liquid nitrogen product.
It should be noted that in the present embodiment, step s303 of Hydrolysis kinetics nitrogen product with extract liquid nitrogen product and gas
Step s305 of nitrogen product is to carry out in whole technological process simultaneously, and out-of-order limits.
In sum, the flashed vapour that the present invention provides extracts the system and method for helium, high-purity being extracted using flashed vapour
While the helium of degree, can also extract and obtain the addition products such as gas nitrogen product, liquid nitrogen product and liquefied natural gas product, have
Effect improves the utilization rate of resource, and whole extraction process flow process is simple and convenient, energy consumption greatly reduces and becomes with the production and operation
This, lift economic benefit further.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for the skill of this area
For art personnel, the present invention can have various modifications and variations.All within the spirit and principles in the present invention, made any repair
Change, equivalent, improvement etc., should be included within the scope of the present invention.It should also be noted that similar label and letter exist
Representing similar terms in figure below, therefore, once being defined in a certain Xiang Yi accompanying drawing, being then not required in subsequent accompanying drawing
It is defined further and to be explained.
The above, the only specific embodiment of the present invention, but protection scope of the present invention is not limited thereto, and any
Those familiar with the art the invention discloses technical scope in, change or replacement can be readily occurred in, all should contain
Cover within protection scope of the present invention.Therefore, protection scope of the present invention should described be defined by scope of the claims.
Claims (10)
1. a kind of flashed vapour extracts the system of helium it is characterised in that including: carry helium tower (110), main heat exchanger (120), first
Condensation separator (130), the first condenser (140) and the first vaporizer (150), described first condenser (140) is arranged at institute
State the top carrying helium tower (110), described first vaporizer (150) be arranged at described in carry the bottom of helium tower (110), described main heat exchange
Device (120) is provided with the first cooling circuit (121) and the second cooling circuit (122)；
Described first cooling circuit (121), described first vaporizer (150), described second cooling circuit (122), described carry helium
Tower (110), described first condenser (140) and described first condensation separator (130) are sequentially communicated, described first condensation separation
Device (130) is also connected with the described helium tower (110) that carries；
Described first cooling circuit (121), described first vaporizer (150), described second cooling circuit (122) and described first
Condenser (140) obtains liquid phase feed and phase feed, described gas for carrying out cooling successively to the flashed vapour raw material after pressurization
Phase raw material includes helium, nitrogen and hydrogen, and described first condensation separator (130) is used for former to described liquid phase feed and gas phase
Material carries out separating, and the described phase feed derivation after separation is obtained rough helium product.
2. flashed vapour according to claim 1 extract helium system it is characterised in that also include denitrification column (160), the
Two condensation separators (170), the second condenser (180) and the second vaporizer (190), described second condenser (180) is arranged at
The top of described second condensation separator (170), described second vaporizer (190) is arranged at described second condensation separator
(170) bottom, described main heat exchanger (120) is additionally provided with the 3rd cooling circuit (123) and the first heating circuit (124)；
The described bottom carrying helium tower (110), described second vaporizer (190), described 3rd cooling circuit (123), described denitrogenation
Tower (160), described second condenser (180) and described second condensation separator (170) are sequentially communicated, described second condensation separation
Device (170) is connected with described first heating circuit (124) and described denitrification column (160) respectively；
Described second vaporizer (190) is gentle for the described liquid phase feed heating after separation is obtained liquefied natural gas (LNG) feed
Nitrogen raw material, described 3rd cooling circuit (123) and described second condenser (180) are cold for carrying out successively to described gas nitrogen raw material
But, described second condensation separator (170) is used for the gas nitrogen raw material after cooling is carried out separating, and obtains initial liquid nitrogen product with just
Beginning gas nitrogen product, described initial liquid nitrogen product includes the first initial liquid nitrogen product and the second initial liquid nitrogen product, and described first adds
Hot loop (124) is used for obtaining gas nitrogen product to the heating of described initial gas nitrogen product, and described first initial liquid nitrogen product is imported into
Described denitrification column (160) thinks that described denitrification column (160) provides cold, and described second initial liquid nitrogen product is exported to obtain liquid
Nitrogen product.
3. flashed vapour according to claim 2 extracts the system of helium it is characterised in that also including the 4th cooling circuit
(125), described 4th cooling circuit (125) is connected with the bottom of described denitrification column (160), for by the liquefied natural gas obtaining
Raw material cools down, and derives and obtain liquefied natural gas product.
4. flashed vapour according to claim 1 extracts the system of helium it is characterised in that also including the first compressor
(200), the two ends of described first compressor (200) respectively carry helium tower (110) and described denitrification column (160) company with described
Logical, for carrying helium tower (110) and described denitrification column (160) offer power for described.
5. flashed vapour according to claim 1 extracts the system of helium it is characterised in that also including the second compressor
(210), described second compressor (210) is connected with described main heat exchanger (120), and described second compressor (210) is used for mixed
Close cold-producing medium to be compressed to provide cold to described main heat exchanger (120).
6. flashed vapour according to claim 1 extract helium system it is characterised in that also include dehydrogenation unit (220),
Dehydration device (230) and nitrogen rejection facility (240), described main heat exchanger (120) is additionally provided with the second heating circuit (126), described
Second heating circuit (126) is connected with described first condensation separator (130), described second heating circuit (126), described dehydrogenation
Device (220), described dehydration device (230) and described nitrogen rejection facility (240) are sequentially communicated, so that by the rough helium obtaining
Product carries out dehydrogenation, dehydration and denitrogenation processing, obtains purified nitrogen product.
7. a kind of flashed vapour extracts the method for helium it is characterised in that methods described includes:
Flashed vapour raw material after pressurization is carried out by cooling obtains liquid phase feed and phase feed, described phase feed include helium,
Nitrogen and hydrogen；
The liquid phase feed obtaining is separated with phase feed；
The phase feed isolated is derived and obtains rough helium product.
8. method according to claim 7 is it is characterised in that methods described also includes:
The liquid phase feed obtaining heating is obtained liquefied natural gas (LNG) feed gentle nitrogen raw material；
The gas nitrogen raw material obtaining is cooled down；
Gas nitrogen raw material after cooling is carried out separating, obtains initial liquid nitrogen product and initial gas nitrogen product, described initial liquid nitrogen produces
Product include the first initial liquid nitrogen product and the second initial liquid nitrogen product；
Obtain gas nitrogen product to obtaining the heating of initial gas nitrogen product；
It is that described denitrification column (160) provides cold that first initial liquid nitrogen product is imported described denitrification column (160), and described second
Initial liquid nitrogen product is derived and is obtained liquid nitrogen product.
9. method according to claim 8 is it is characterised in that methods described also includes:
Derive after the liquefied natural gas (LNG) feed obtaining is cooled down, obtain liquefied natural gas product.
10. method according to claim 7 is it is characterised in that methods described also includes: by the rough helium product obtaining
Carry out dehydrogenation, dehydration and denitrogenation processing, obtain purified nitrogen product.
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| CN201610722780.XA CN106352657B (en) | 2016-08-24 | 2016-08-24 | The system and method for flashed vapour extraction helium |
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| CN201610722780.XA CN106352657B (en) | 2016-08-24 | 2016-08-24 | The system and method for flashed vapour extraction helium |
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Cited By (5)
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| CN107228526A (en) * | 2017-07-03 | 2017-10-03 | 成都深冷液化设备股份有限公司 | A kind of LNG flashed vapours carry helium, denitrogenation and reliquefaction installation |
| CN113566493A (en) * | 2021-08-06 | 2021-10-29 | 安徽万瑞冷电科技有限公司 | Cryogenic separation system for helium recovery |
| CN113670002A (en) * | 2021-09-27 | 2021-11-19 | 西南石油大学 | Double-tower natural gas helium recovery method |
| CN113698971A (en) * | 2021-08-11 | 2021-11-26 | 宁夏天利丰能源利用有限公司 | Method for removing heavy hydrocarbon by using low-temperature rectification method |
| CN113865263A (en) * | 2021-09-15 | 2021-12-31 | 中国石油天然气股份有限公司西南油气田分公司成都天然气化工总厂 | Production system for extracting crude helium and co-producing liquefied natural gas by natural gas |
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| CN106352657B (en) | 2019-05-03 |
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