CN106461323B - Cryogenic purincation method with heat absorption - Google Patents
Cryogenic purincation method with heat absorption Download PDFInfo
- Publication number
- CN106461323B CN106461323B CN201580033220.7A CN201580033220A CN106461323B CN 106461323 B CN106461323 B CN 106461323B CN 201580033220 A CN201580033220 A CN 201580033220A CN 106461323 B CN106461323 B CN 106461323B
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- Prior art keywords
- air
- temperature
- flow
- exchanger
- impurity
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- Expired - Fee Related
Links
- 238000000034 method Methods 0.000 title claims abstract description 30
- 238000010521 absorption reaction Methods 0.000 title claims description 7
- 238000007906 compression Methods 0.000 claims abstract description 19
- 239000006096 absorbing agent Substances 0.000 claims abstract description 18
- 238000004821 distillation Methods 0.000 claims abstract description 10
- 239000012530 fluid Substances 0.000 claims abstract description 4
- 230000001172 regenerating effect Effects 0.000 claims abstract description 3
- 239000012535 impurity Substances 0.000 claims description 20
- 230000006835 compression Effects 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 11
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 6
- 238000001179 sorption measurement Methods 0.000 claims description 6
- 239000002808 molecular sieve Substances 0.000 claims description 4
- 230000008929 regeneration Effects 0.000 claims description 4
- 238000011069 regeneration method 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
- 238000003303 reheating Methods 0.000 claims description 3
- 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
- 239000000741 silica gel Substances 0.000 claims description 2
- 229910002027 silica gel Inorganic materials 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 14
- 238000010438 heat treatment Methods 0.000 description 9
- 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
- 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
- 230000002452 interceptive effect Effects 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000000926 separation method Methods 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
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
- F25J3/04151—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
- 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
- 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
A method of carrying out purified gases feeding flow in the at a temperature of absorbing unit for containing at least two absorber, cryogenic distillation unit, exchanger and the compressor that run less than or equal to -50 DEG C for using, wherein being at least part for being at least partly originated from the heat generated in the compression process of fluid by the compressor for heat needed for regenerating these absorbers.
Description
Technical field
The present invention relates to a kind of methods for purifying feed stream using absorbing unit and cryogenic distillation unit.
Background technique
Absorption is the phenomenon that generally promotion by low temperature.For example, for ASU (air separation equipment), CO2In molecular sieve
On stop at it is up to 5 times bigger than at 20 DEG C and about 3 times or so bigger than the stopping for propane at -100 DEG C.
Regeneration requires supplementation with heat, which has upset the freezing balance of equipment, if absorption occurs in negative temperature
Under talking about.Its energy cost may be even more big, because temperature is low.
It in method according to prior art, is adsorbed at positive temperature and carries out, and be used for regenerated heat (extra heat
Amount) it is discharged into atmosphere, the freezing without will affect the low temperature part balances.
From there, suffering from a problem that is that cryogenic purincation is provided in low temperature separating methods, the cryogenic separation side
Method already knows how to manage the thermal enhancement required for the regeneration at least equal to these absorbers when it reaches freezing balance.
Summary of the invention
A solution of the invention be it is a kind of for use less than or equal to -50 DEG C at a temperature of run include
Absorbing unit, cryogenic distillation unit, exchanger and the compressor of at least two absorber are come the method that purifies feed stream, wherein
It is at least partly to be originated to be generated in the compression process of fluid by the compressor for heat needed for regenerating these absorbers
Heat at least part.
It depends on the circumstances, can have according to the method for the present invention one or more in following characteristics:
The adsorption step that the method includes being implemented by the absorbing unit, wherein the adsorption step under negative temperature into
Row；
The method includes, according to the first alternative solution, following consecutive steps (Fig. 1):
A) feed stream 1 is cooled to the temperature lower than -50 DEG C, preferably shorter than -100 DEG C in exchanger 2；
B) cooling air-flow 3 being sent in absorbing unit 4, at least one impurity X is at least partly adsorbed herein, with
Just the air-flow 5 of poor impurity X is recycled；
C) air-flow 5 of poor impurity X is introduced into exchanger 2 to be cool below -50 DEG C, preferably shorter than -150 DEG C
Temperature；
D) by the poor impurity X and cooled air-flow 5 is sent in cryogenic distillation unit 7, the air-flow is separated herein
At at least two stream 8 and 9；
E) a part for flowing 9 is introduced into the exchanger so as to be heated to be higher than -150 DEG C, preferably higher than -100 DEG C,
More preferably higher than -50 DEG C of temperature ideally arrives the temperature close to the temperature of feed stream 1 at the end of step a),
It is compressed later in compressor 10 with the compression ratio greater than 1.2；
F) compression stream 9 is sent in absorbing unit 4, to regenerate one of the two absorbers；
Wherein the compression in step e) causes at least 20 DEG C of temperature of stream 9 to rise, and regenerates these to provide
Heat input needed at least one of absorber；
The method includes, according to the second alternative solution, following consecutive steps (Fig. 2):
A) feed stream 1 is cooled to the temperature lower than -50 DEG C, preferably shorter than -100 DEG C in exchanger 2；
B) cooling air-flow 3 being sent in absorbing unit 4, at least one impurity X is at least partly adsorbed herein, with
Just first-class the 5 of poor impurity X are recycled；
C) air-flow 5 of poor impurity X is compressed in compressor 10 with the compression ratio greater than 1.2, later in exchanger 2
In be cooled to lower than -50 DEG C, preferably shorter than -150 DEG C of temperature；
D) by the poor impurity X, compressed and cooled air-flow 5 is sent in cryogenic distillation unit 7, herein should
Air-flow is separated at least two stream 8 and 9；
E) a part for flowing 9 is introduced into the exchanger so as to be heated to be higher than -150 DEG C, preferably higher than -100 DEG C,
More preferably higher than -50 DEG C of temperature ideally arrives the temperature close to the temperature of feed stream 5 at the end of compression step c),
F) stream of reheating 9 is sent in absorbing unit 4, to regenerate at least one of the two absorbers；
Wherein the compression in step c) causes at least 20 DEG C of temperature of the air-flow 5 of poor impurity X to rise, and between
Ground connection provides a part of required of reheating stream 9 via exchanger 2 and therefore regenerates the two absorbers in step f)
At least one of needed for heat input；
These absorbers include single, preferred molecular sieve；
The feed stream is air, and impurity X is selected from H2O、CO2、N2O、CnHm, NOx；
The feed stream includes water and the method includes before step a), by the step of the feed stream prepurification
Suddenly, which makes it possible to eliminate at least part of the water.
The prepurification step is by adsorbing progress at ambient temperature；
The absorption of the prepurification step is the single upper progress in aluminium oxide, silica gel or molecular sieve type.
The present invention will be illustrated on the ASU with cold compressor.The cold compressor will reheat the heat of compressed gas
Gain is introduced into ice chest.The natural freezing balance of the equipment makes it possible to manage the thermal enhancement.A part of hot gas will
Via with another fluid heat exchange and by direct or indirect use to carry out the regenerated heating period.This is occurred without really
Energy loss because it does not interfere the freezing balance of (or the hardly interfere) equipment.
Detailed description of the invention
Fig. 1 shows the first alternative solution according to the solution of the present invention.
Fig. 2 shows the second alternative solutions according to the solution of the present invention.
Specific embodiment
Fig. 1 shows the first alternative solutions according to the solution of the present invention.
By air 1 in exchange pipeline 2 cooling (for example, down to -120 DEG C), then pass through under low temperature (- 120 DEG C)
Then the bed of adsorbent 4 is reintroduced back to (optionally slightly hot, due to absorption) and is finally cooled down into exchange pipeline 2, is sent to later
In distillation fraction 7.
By a part of remaining nitrogen 9, about -120 DEG C of extractions from the exchange pipeline, then compress in cold compressor 10,
It is heated to such as -80 DEG C of temperature herein, is then delivered in the adsorbent bed being reproduced.The heat structure provided by compression
At heat input needed for the regenerated heating period.The nitrogen is cooling in the bed of adsorbent 4, then in about -120 DEG C of temperature
It is sent under degree to exchange pipeline 2 to be additionally again heated to environment temperature.
Adsorption temp can be determined preferentially close to " natural " inlet temperature in cold booster by this method
Temperature, as have conventional environment temperature purifying.
As can be seen that the regenerated heating period does not interfere the freezing balance of (or the hardly interfering) equipment, the heating
Stage is carried out by the natural heat input provided by cold compression.Therefore, energy loss is not present in carrying out cryogenic purincation.
About in the regenerated cooling stage according to the method for first alternative solution, by a part of remaining nitrogen from this
About -120 DEG C of extractions in pipeline are exchanged, (cooling stage) is then initially entered in the bed being reproduced, is compressed later, then sent
Into the exchange pipeline to be additionally again heated to environment temperature.
Observe that the heating and cooling stage carry out at various pressures, it is desirable that this bed is made to adapt to the centre of correct pressure
Stage.
Fig. 2 indicates the second alternative solution according to the solution of the present invention.
1 part of air is cooled to -120 DEG C, then passes through the bed of adsorbent 4, later cold compression 10, herein by the sky
Gas is heated to -80 DEG C of temperature, is then returned to more heat exchange pipeline 2 and is finally cooled down, is sent in distillation fraction 7 later.
A part of remaining nitrogen 9 is reheated in exchange pipeline 2, up to the temperature close to cold compression air themperature
Degree, such as -80 DEG C, to recycle the heat introduced by the compression of air indirectly.Thus -80 DEG C of nitrogen is heated to pass through
Bed across adsorbent 4 carries out the regenerated heating period, and the nitrogen is cooled to -120 DEG C in the adsorbent bed, is then delivered to
It exchanges in pipeline 2 to be additionally again heated to environment temperature.
Adsorption temp can be preferentially close to " natural " inlet temperature in cold booster, the typically about steaming of oxygen
The temperature of platform (plateau) is sent out, such as conventional single machine layout with cold booster (for pressurizeing at 40bar
Oxygen be about -120 DEG C).
Again it is seen that the regenerated heating period does not interfere the freezing balance of (or the hardly interfering) equipment, it should
Heating period is carried out by the natural heat input provided by cold compression (in this case indirectly).Therefore, it is carrying out
Energy loss is not present in cryogenic purincation.
About the regenerated cooling stage according to the method for second alternative solution, by a part of remaining nitrogen close
The exchange pipeline is left at the temperature (about -120 DEG C) of the entrance of cold compressor, across adsorbent bed to be cooled to, so
After be sent in the exchange pipeline to be additionally again heated to environment temperature.In this case, heating and cooling stage are in identical pressure
It is carried out under power.
Claims (9)
1. it is a kind of for use less than or equal to -50 DEG C at a temperature of run the absorbing unit comprising at least two absorber,
Cryogenic distillation unit, exchanger and compressor are come the method that purifies feed stream, wherein for regenerating needed for these absorbers
Heat is at least partly to be originated from at least part of heat generated in the compression process of fluid by the compressor, and institute
The method of stating includes the adsorption step implemented by the absorbing unit, and wherein the adsorption step carries out under negative temperature.
2. the method as described in claim 1, which is characterized in that the method includes following consecutive steps:
The feed stream (1) a) is cooled to the temperature lower than -50 DEG C in exchanger (2)；
B) air-flow of the cooling (3) is sent in the absorbing unit (4), at least one impurity X is at least partly inhaled herein
It is attached, to recycle the air-flow (5) of poor impurity X；
C) air-flow (5) of the poor impurity X is introduced into and is cool below -50 DEG C of temperature in the exchanger (2)；
D) by the poor impurity X and cooled air-flow (5) is sent in the cryogenic distillation unit (7), herein by the air-flow point
From at least first-class (8) and second (9)；
E) a part of the second (9) is introduced into be heated to the temperature for being higher than -150 DEG C in the exchanger, later
It is compressed in compressor (10) with the compression ratio greater than 1.2；
F) compressed second (9) is sent in the absorbing unit (4), to regenerate one of the two absorbers；
Wherein the compression in step e) causes at least 20 DEG C of temperature of the second (9) to rise, and to provide regeneration
Heat input needed at least one of these absorbers.
3. the method as described in claim 1, which is characterized in that the method includes following consecutive steps:
The feed stream (1) a) is cooled to the temperature lower than -50 DEG C in exchanger (2)；
B) air-flow of the cooling (3) is sent in the absorbing unit (4), at least one impurity X is at least partly inhaled herein
It is attached, to recycle the air-flow (5) of poor impurity X；
C) air-flow (5) of the poor impurity X is compressed in the compressor (10) with the compression ratio greater than 1.2, later at this
The temperature lower than -50 DEG C is cooled in exchanger (2)；
D) by the poor impurity X, compressed and cooled air-flow (5) is sent in the cryogenic distillation unit (7), herein should
Air-flow is separated at least first-class (8) and second (9)；
E) a part of the second (9) is introduced into the exchanger to be heated to the temperature for being higher than -150 DEG C；
F) second of the reheating (9) is sent in the absorbing unit (4), to regenerate at least one in the two absorbers
It is a；
Wherein the compression in step c) causes 20 DEG C of temperature of the air-flow (5) of the poor impurity X to rise, and to indirectly
There is provided via the exchanger (2) reheat the second (9) a part of required and therefore in step f) regeneration this two
Heat input needed at least one of a absorber.
4. the method as described in one of claims 1 to 3, which is characterized in that these absorbers include single.
5. method as claimed in claim 4, which is characterized in that these absorbers include molecular sieve.
6. method as claimed in claim 2 or claim 3, which is characterized in that the feed stream is air, and impurity X is selected from H2O、
CO2、N2O、CnHm、NOx。
7. method as claimed in claim 2 or claim 3, which is characterized in that the feed stream include water and the method includes,
Before step a), the step of by the feed stream prepurification, which makes it possible to eliminate at least one of the water
Point.
8. the method for claim 7, which is characterized in that the prepurification step is carried out by adsorbing at ambient temperature
's.
9. method according to claim 8, which is characterized in that the absorption of the prepurification step is in aluminium oxide, silica gel or to divide
Single upper progress 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 CN106461323A (en) | 2017-02-22 |
| CN106461323B true 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 |
| CN106461323A (en) | 2017-02-22 |
| FR3022993A1 (en) | 2016-01-01 |
| EP3161399A1 (en) | 2017-05-03 |
| US20170138665A1 (en) | 2017-05-18 |
| WO2015197940A1 (en) | 2015-12-30 |
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