CN106461323A - Cryogenic purification with heat uptake - Google Patents
Cryogenic purification with heat uptake Download PDFInfo
- Publication number
- CN106461323A CN106461323A CN201580033220.7A CN201580033220A CN106461323A CN 106461323 A CN106461323 A CN 106461323A CN 201580033220 A CN201580033220 A CN 201580033220A CN 106461323 A CN106461323 A CN 106461323A
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- CN
- China
- Prior art keywords
- air
- temperature
- flow
- impurity
- interchanger
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000746 purification Methods 0.000 title claims 3
- 238000000034 method Methods 0.000 claims abstract description 24
- 238000007906 compression Methods 0.000 claims abstract description 20
- 230000006835 compression Effects 0.000 claims abstract description 18
- 230000008929 regeneration Effects 0.000 claims abstract description 14
- 238000011069 regeneration method Methods 0.000 claims abstract description 14
- 238000004821 distillation Methods 0.000 claims abstract description 10
- 238000001179 sorption measurement Methods 0.000 claims abstract description 7
- 239000012530 fluid Substances 0.000 claims abstract description 4
- 239000012535 impurity Substances 0.000 claims description 19
- 239000006096 absorbing agent Substances 0.000 claims description 14
- 238000010521 absorption reaction Methods 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 10
- 239000002808 molecular sieve Substances 0.000 claims description 4
- 230000001172 regenerating effect Effects 0.000 claims description 4
- 238000003303 reheating Methods 0.000 claims description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- FGUUSXIOTUKUDN-IBGZPJMESA-N C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 Chemical compound C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 FGUUSXIOTUKUDN-IBGZPJMESA-N 0.000 claims description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 claims description 2
- 239000000741 silica gel Substances 0.000 claims description 2
- 229910002027 silica gel Inorganic materials 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 238000010438 heat treatment Methods 0.000 description 8
- 239000003463 adsorbent Substances 0.000 description 7
- 238000007710 freezing Methods 0.000 description 7
- 230000008014 freezing Effects 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 7
- 239000007789 gas Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 150000002829 nitrogen Chemical class 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- VMXUWOKSQNHOCA-UKTHLTGXSA-N ranitidine Chemical compound [O-][N+](=O)\C=C(/NC)NCCSCC1=CC=C(CN(C)C)O1 VMXUWOKSQNHOCA-UKTHLTGXSA-N 0.000 description 2
- 239000001294 propane Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 230000009469 supplementation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- F25J3/02—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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
-
- 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
- F25J3/02—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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of 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
- 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
- F25J3/04—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 for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04242—Cold end purification of the feed air
-
- 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
- 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
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
- F25J2205/70—Heating the adsorption vessel
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation Of Gases By Adsorption (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Process for purifying a gaseous feed stream using an adsorption unit comprising at least two adsorbers, a cryogenic distillation unit, an exchanger and a compressor operating at a temperature less than or equal to -50 DEG C, in which the heat necessary for the regeneration of the adsorbers is derived, at least partly, from at least one portion of the heat generated by the compressor, during the compression of a fluid.
Description
The present invention relates to a kind of method for using absorbing unit and cryogenic distillation unit to purify feed stream.
Absorption is the phenomenon typically being promoted by low temperature.For example, for ASU (air separation equipment), CO2Over a molecular sieve
Stop at-100 DEG C at than at 20 DEG C big up to 5 times, and the stopping being compared to propane is big about about 3 times.
Regeneration requires supplementation with heat, and this additional heat has upset the freezing balance of equipment, if absorption occurs in negative temperature
Under words.Its energy cost may be even more big, because temperature is low.
In the method according to prior art, absorption is carried out at positive temperature, and for heat (many waste heats of regeneration
Amount) it is discharged in air, without affecting the freezing balance of this low isothermal segment.
From there, suffering from a problem that is offer cryogenic purincation, this cryogenic separation side in low temperature separating methods
Method already knows how to manage when it reaches freezing balance, at least equal to the thermal enhancement required for the regeneration of these absorbers.
One solution of the present invention is a kind of for using that runs at a temperature of less than or equal to-50 DEG C to comprise
The absorbing unit of at least 2 absorbers, cryogenic distillation unit, interchanger and compressor purify the method for feed stream, wherein,
Heat for regenerating needed for these absorbers is to be derived from least in part to be produced by this compressor in the compression process of fluid
At least a portion of heat.
Depending on the circumstances, it is one or more that the method according to the invention can have in following characteristics：
-described method includes the adsorption step implemented by this absorbing unit, and wherein this adsorption step enters under negative temperature
OK；
-described method includes, according to the first replacement scheme, following consecutive steps (Fig. 1)：
A) feed stream 1 is cooled in interchanger 2 less than-50 DEG C, is preferably shorter than the temperature of-100 DEG C；
B) delivering in absorbing unit 4 by the air-flow 3 of cooling, here at least one impurity X is adsorbed at least in part, with
Just the air-flow 5 of lean impurity X is reclaimed；
C) it is incorporated into the air-flow 5 of lean impurity X in interchanger 2 to be cool below-50 DEG C, preferably shorter than-150 DEG C
Temperature；
D) this lean impurity X and cooled air-flow 5 are delivered in cryogenic distillation unit 7, here this air-flow is separated
Become at least 2 streams 8 and 9；
E) be incorporated into a part for stream 9 in this interchanger so as to be heated to higher than-150 DEG C, preferably above-100 DEG C,
The temperature of more preferably higher than-50 DEG C, arrives the temperature close to the temperature of feed stream 1 at the end of step a) ideally,
It is compressed with the compression ratio more than 1.2 in compressor 10 afterwards；
F) compression stream 9 is delivered in absorbing unit 4, in order to one of regeneration the two absorber；
The wherein compression in step e) causes the temperature of at least 20 DEG C that flow 9 to rise, and thus provides and regenerate these
The required heat input of at least one in absorber；
-described method includes, according to the second replacement scheme, following consecutive steps (Fig. 2)：
A) feed stream 1 is cooled in interchanger 2 less than-50 DEG C, is preferably shorter than the temperature of-100 DEG C；
B) delivering in absorbing unit 4 by the air-flow 3 of cooling, here at least one impurity X is adsorbed at least in part, with
Just first-class the 5 of lean impurity X are reclaimed；
C) air-flow 5 of lean impurity X is compressed with the compression ratio more than 1.2 in compressor 10, afterwards at interchanger 2
In be cooled to less than-50 DEG C, the temperature of preferably shorter than-150 DEG C；
D) by this lean impurity X, compressed and cooled air-flow 5 is delivered in cryogenic distillation unit 7, here by this gas
Flow separation becomes at least 2 streams 8 and 9；
E) be incorporated into a part for stream 9 in this interchanger so as to be heated to higher than-150 DEG C, preferably above-100 DEG C,
The temperature of more preferably higher than-50 DEG C, arrives the temperature close to the temperature of feed stream 5 at the end of compression step c) ideally,
F) stream 9 of reheating is delivered in absorbing unit 4, in order at least one in regeneration the two absorber；
The wherein compression in step c) causes the temperature of at least 20 DEG C of the air-flow 5 of lean impurity X to rise, and thus
It is grounded and provide via interchanger 2 needed for the part reheating stream 9 and in step f), therefore regenerate the two absorber
In at least one required heat input；
-these absorbers include single, preferred molecular sieve；
-this feed stream is air, and this impurity X is selected from H2O、CO2、N2O、CnHm、NOx；
-this feed stream comprises water and described method includes, before step a), by the step of this feed stream prepurification
Suddenly, this prepurification step makes it possible to eliminate at least a portion of this water.
-this prepurification step is carried out by absorption at ambient temperature；
The absorption of-this prepurification step is to carry out on single of aluminum oxide, silica gel or molecular sieve type.
The present invention will illustrate on the ASU have cold compressor.This cold compressor will reheat the heat of compressed gas
Gain is incorporated in ice chest.The natural freezing balance of this equipment makes it possible to manage this thermal enhancement.A part for hot gas will
Directly or indirectly used so that the heating period regenerating via exchanging with another fluid thermal.This occurs without really
Energy loss because it does not disturbs the freezing balance of (or hardly interference) this equipment.
Fig. 1 represents the first replacement scheme according to the solution of the present invention.
Then pass through air 1 cooling (for example, as little as-120 DEG C) in exchange pipeline 2 under low temperature (-120 DEG C)
The bed of adsorbent 4, is then reintroduced back to (optionally slightly hot, due to absorption) and finally cools down in exchange pipeline 2, deliver to afterwards
In distillation fraction 7.
By a part about-120 DEG C of extractions from this exchange pipeline of remaining nitrogen 9, then compress in cold compressor 10,
It is here heated to the temperature of such as-80 DEG C, be then delivered in the adsorbent bed being reproduced.The heat structure being provided by compression
Become the heat input needed for the heating period of regeneration.This nitrogen is cooled down in the bed of adsorbent 4, then the temperature of about-120 DEG C
Exchange pipeline 2 is delivered to be additionally again heated to environment temperature under degree.
Adsorption temp i.e. can be determined by the method preferentially close to " naturally " inlet temperature in cold booster
Temperature, as have conventional environment temperature purify.
It can be seen that the heating period of this regeneration do not disturb the freezing balance of (or hardly interference) this equipment, this heating
Stage is to be carried out by the atural beat input being provided by cold compression.Therefore, in carrying out cryogenic purincation, there is not energy loss.
In cooling stage with regard to the regeneration of the method according to this first replacement scheme, by a part for remaining nitrogen from this
About-120 DEG C of extractions in exchange pipeline, then initially enter (cooling stage) in the bed being reproduced, are compressed afterwards, then send
To be additionally again heated to environment temperature in this exchange pipeline.
Observe that this heating and cooling stage are carried out at various pressures, it is desirable to make this adapt to the centre of correct pressure
Stage.
Fig. 2 represents the second replacement scheme according to the solution of the present invention.
Air 1 part is cooled to-120 DEG C, then passes through the bed of adsorbent 4, afterwards cold compression 10, here by this sky
Gas is heated to the temperature of-80 DEG C, is then returned to more heat exchange pipeline 2 and finally cools down, delivers to afterwards in distillation fraction 7.
A part for remaining nitrogen 9 is reheated in exchange pipeline 2, the up to temperature close to cold compression air themperature
Degree, such as-80 DEG C, thus indirectly reclaim the heat being introduced by the compression of air.The nitrogen being thus heated to-80 DEG C passes through
The heating period regenerating through the bed of adsorbent 4, in this adsorbent bed, this nitrogen is cooled to-120 DEG C, is then delivered to
To be additionally again heated to environment temperature in exchange pipeline 2.
Adsorption temp can be preferentially close to " naturally " inlet temperature in cold booster, the steaming of typically about oxygen
Send out the temperature of platform (plateau), for example, conventional single machine layout with cold booster (is pressurizeed under 40bar
Oxygen be about-120 DEG C).
It again it is seen that the heating period of this regeneration does not disturbs the freezing balance of (or interference hardly) this equipment, is somebody's turn to do
Heating period is to be carried out by the atural beat input being provided by cold compression (in this case indirectly).Therefore, carrying out
Cryogenic purincation does not exist energy loss.
With regard to the cooling stage of the regeneration of the method according to this second replacement scheme, by a part for remaining nitrogen close
This exchange pipeline is left, through adsorbent bed to be cooled to, so at the temperature (about-120 DEG C) of the entrance of cold compressor
After deliver in this exchange pipeline to be additionally again heated to environment temperature.In this case, heat with cooling stage in identical pressure
Carry out under power.
Claims (8)
1. one kind for use less than or equal to the absorbing unit comprising at least 2 absorbers running at a temperature of-50 DEG C,
Cryogenic distillation unit, interchanger and compressor purify the method for feed stream, wherein, for regenerating needed for these absorbers
Heat is at least a portion being derived from the heat being produced by this compressor in the compression process of fluid at least in part, and institute
The method of stating includes the adsorption step implemented by this absorbing unit, and wherein this adsorption step is carried out under negative temperature.
2. purification process as claimed in claim 1, it is characterised in that described method includes following consecutive steps：
A) this feed stream (1) is cooled in interchanger (2) temperature less than-50 DEG C；
B) delivering in this absorbing unit (4) by the air-flow (3) of this cooling, here at least one impurity X is inhaled at least in part
Attached, in order to reclaim the air-flow (5) of lean impurity X；
C) it is incorporated in this interchanger (2) air-flow (5) of this lean impurity X to be cool below the temperature of-50 DEG C；
D) this lean impurity X and cooled air-flow (5) are delivered to, in this cryogenic distillation unit (7), here divide this air-flow
From at least 2 streams (8) of one-tenth and (9)；
E) it is incorporated into the part of this stream (9) in this interchanger to be heated to the temperature higher than-150 DEG C, afterwards in pressure
Contracting machine is compressed with the compression ratio more than 1.2 in (10)；
F) this compression stream (9) is delivered in this absorbing unit (4), in order to one of regeneration the two absorber；
The wherein compression in step e) causes the temperature of at least 20 DEG C of this stream (9) to rise, and thus provides and regenerate these
The required heat input of at least one in absorber.
3. purification process as claimed in claim 1, it is characterised in that described method includes following consecutive steps：
A) this feed stream (1) is cooled in interchanger (2) temperature less than-50 DEG C；
B) delivering in this absorbing unit (4) by the air-flow (3) of this cooling, here at least one impurity X is inhaled at least in part
Attached, in order to reclaim first-class (5) of lean impurity X；
C) air-flow (5) of this lean impurity X is compressed with the compression ratio more than 1.2 in this compressor (10), afterwards at this
Interchanger (2) is cooled to the temperature less than-50 DEG C；
D) by this lean impurity X, compressed and cooled air-flow (5) is delivered to, in this cryogenic distillation unit (7), here should
Air-flow is separated at least 2 streams (8) and (9)；
E) it is incorporated into the part of this stream (9) in this interchanger to be heated to the temperature higher than-150 DEG C；
F) stream (9) of this reheating is delivered in this absorbing unit (4), in order at least one in regeneration the two absorber；
The wherein compression in step c) causes the temperature of 20 DEG C of the air-flow (5) of this lean compounds X to rise, and thus indirectly
Ground provides needed for the part reheating this stream 9 and therefore regeneration the two absorption in step f) via this interchanger 2
The required heat input of at least one in device.
4. the method as described in one of claims 1 to 3, it is characterised in that these absorbers include single, preferred molecular sieve.
5. the method as described in one of Claims 1-4, it is characterised in that this feed stream is air, and this impurity X choosing
From H2O、CO2、N2O、CnHm、NOX.
6. the method as described in one of claim 1 to 5, it is characterised in that this feed stream comprises water and described method bag
Including, before step a), by the step of this feed stream prepurification, this prepurification step makes it possible to eliminate this water at least
A part.
7. method as claimed in claim 6, it is characterised in that this prepurification step is to be carried out by absorption at ambient temperature
's.
8. method as claimed in claim 7, it is characterised in that the absorption of this prepurification step is at aluminum oxide, silica gel or to divide
Carry out on single of son sieve type.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR1455985A FR3022993A1 (en) | 2014-06-26 | 2014-06-26 | CRYOGENIC CLEANING WITH HEAT INPUT |
| FR1455985 | 2014-06-26 | ||
| PCT/FR2015/051567 WO2015197940A1 (en) | 2014-06-26 | 2015-06-12 | Cryogenic purification with heat uptake |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN106461323A true CN106461323A (en) | 2017-02-22 |
| CN106461323B CN106461323B (en) | 2019-08-06 |
Family
ID=51519043
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201580033220.7A Expired - Fee Related CN106461323B (en) | 2014-06-26 | 2015-06-12 | Cryogenic purincation method with heat absorption |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US20170138665A1 (en) |
| EP (1) | EP3161399B1 (en) |
| CN (1) | CN106461323B (en) |
| FR (1) | FR3022993A1 (en) |
| WO (1) | WO2015197940A1 (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4746332A (en) * | 1985-09-27 | 1988-05-24 | Hitachi, Ltd. | Process for producing high purity nitrogen |
| EP0894522A1 (en) * | 1997-07-31 | 1999-02-03 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for the production of ultra-pure inert gas |
| CN101198834A (en) * | 2005-06-23 | 2008-06-11 | 空气及水株式会社 | Nitrogen generating device and apparatus for use therefor |
| CN201265997Y (en) * | 2008-09-05 | 2009-07-01 | 苏州制氧机有限责任公司 | Liquid air separation plant |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1189094B (en) * | 1962-06-09 | 1965-03-18 | Linde Eismasch Ag | Process for removing carbon dioxide from gas mixtures |
| US3236059A (en) * | 1962-08-29 | 1966-02-22 | Air Prod & Chem | Separation of gaseous mixtures |
| US5551257A (en) * | 1992-10-01 | 1996-09-03 | The Boc Group, Inc. | Production of ultrahigh purity nitrogen |
| CN100363699C (en) * | 2005-04-25 | 2008-01-23 | 林福粦 | Air separation system for recycling cold energy of liquified natural gas |
-
2014
- 2014-06-26 FR FR1455985A patent/FR3022993A1/en not_active Ceased
-
2015
- 2015-06-12 US US15/318,801 patent/US20170138665A1/en not_active Abandoned
- 2015-06-12 CN CN201580033220.7A patent/CN106461323B/en not_active Expired - Fee Related
- 2015-06-12 EP EP15733826.0A patent/EP3161399B1/en active Active
- 2015-06-12 WO PCT/FR2015/051567 patent/WO2015197940A1/en active Application Filing
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4746332A (en) * | 1985-09-27 | 1988-05-24 | Hitachi, Ltd. | Process for producing high purity nitrogen |
| EP0894522A1 (en) * | 1997-07-31 | 1999-02-03 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for the production of ultra-pure inert gas |
| CN101198834A (en) * | 2005-06-23 | 2008-06-11 | 空气及水株式会社 | Nitrogen generating device and apparatus for use therefor |
| CN201265997Y (en) * | 2008-09-05 | 2009-07-01 | 苏州制氧机有限责任公司 | Liquid air separation plant |
Also Published As
| Publication number | Publication date |
|---|---|
| EP3161399B1 (en) | 2018-08-15 |
| CN106461323B (en) | 2019-08-06 |
| FR3022993A1 (en) | 2016-01-01 |
| EP3161399A1 (en) | 2017-05-03 |
| US20170138665A1 (en) | 2017-05-18 |
| WO2015197940A1 (en) | 2015-12-30 |
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