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
  • F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B23/00—Noble gases; Compounds thereof
  • C01B23/001—Purification or separation processes of noble gases
  • C01B23/0036—Physical processing only
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2210/00—Purification or separation of specific gases
  • C01B2210/0029—Obtaining noble gases
  • C01B2210/0031—Helium
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2210/00—Purification or separation of specific gases
  • C01B2210/0043—Impurity removed
  • C01B2210/0045—Oxygen
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2210/00—Purification or separation of specific gases
  • C01B2210/0043—Impurity removed
  • C01B2210/0046—Nitrogen
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2210/00—Purification or separation of specific gases
  • C01B2210/0043—Impurity removed
  • C01B2210/0053—Hydrogen
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2210/00—Purification or separation of specific gases
  • C01B2210/0043—Impurity removed
  • C01B2210/0078—Noble gases
  • C01B2210/0081—Neon
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2205/00—Processes or apparatus using other separation and/or other processing means
  • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2205/00—Processes or apparatus using other separation and/or other processing means
  • F25J2205/20—Processes or apparatus using other separation and/or other processing means using solidification of components
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2205/00—Processes or apparatus using other separation and/or other processing means
  • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2205/00—Processes or apparatus using other separation and/or other processing means
  • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2215/00—Processes characterised by the type or other details of the product stream
  • F25J2215/30—Helium
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
  • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
• • 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
  • F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
  • F25J2260/20—Integration in an installation for liquefying or solidifying a fluid stream
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
  • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
  • F25J2270/00—Refrigeration techniques used
  • F25J2270/30—Quasi-closed internal or closed external helium refrigeration cycle
• • 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
  • F25J2280/00—Control of the process or apparatus
  • F25J2280/02—Control in general, load changes, different modes ("runs"), measurements

Definitions

• the invention relates to a method and a device for separating undesired components from a helium stream.
• Nitrogen, oxygen and argon A generic method is disclosed in DE-A 102008053846, for example.
• Condenser supplied.
• the helium stream to be purified is turned against a suitable cooling medium, e.g. a helium or helium-rich stream up to a temperature that is a maximum of 8 K above the freezing point of the undesired component or, in the case of several undesirable components, up to one temperature , which is a maximum of 8 K above the highest freezing point of these undesirable components.
• a suitable cooling medium e.g. a helium or helium-rich stream up to a temperature that is a maximum of 8 K above the freezing point of the undesired component or, in the case of several undesirable components, up to one temperature , which is a maximum of 8 K above the highest freezing point of these undesirable components.
• a suitable cooling medium e.g. a helium or helium-rich stream up to a temperature that is a maximum of 8 K above the freezing point of the undesired component or, in the case of several undesirable components, up to one temperature , which is a maximum of 8
• the condensate collected in it can be discarded and / or used to cool the helium liquefaction process.
• a second cooling step the so-called freeze-out, the precooled helium stream to be cleaned is then cooled down to such an extent that the remaining undesired components freeze out.
• the components that freeze out clog the freezer over time. It is therefore necessary to warm up the heat exchanger from time to time, whereby the frozen components melt off.
• the heat exchanger Before the process can then go back into operation, the heat exchanger has to cool down again Operating temperature required.
• the helium stream purified in this way is then fed to its further use, such as, for example, a liquefaction.
• the cooling medium required for the two cooling steps described above is fed in countercurrent to the helium stream to be cooled.
• the amount and / or composition of the refrigerant or refrigerants used for the 1st and / or 2nd cooling step can be controlled or regulated so that they are adapted to the current conditions, such as the composition of the helium -Current, temperature, pressure, etc., can be adjusted. This enables individual regulation of the two cooling steps.
• the amount and / or composition of the cooling medium or cooling media used for the first and / or second cooling step can thus be optimally adjusted.
• the purified helium flow is used as a further cooling medium in countercurrent for the second cooling step and is then used for the first cooling step.
• DE 10 2013 012656 A1 discloses, in the context of such a method, an adsorber which, after the second cooling step, separates hydrogen and / or neon from the helium flow. cares.
• the air components condense in a first heat exchanger in a first cooling step and freeze out in a second heat exchanger in a second cooling step If the air components condense in the same heat exchanger in which they also freeze out, the liquid cannot be separated cleanly, but remains in the cold heat exchanger. The liquid continues to cool, freeze and block the flow channels of the heat exchanger.
• the amount of cooling medium used for the first cooling step can be controlled or regulated so that more cooling medium can be fed to the first heat exchanger via a feed valve, so that the temperature can be corrected downwards for high levels of soiling.
• the temperature between the two cooling steps may be lower than 62 K due to the counterflow of the purified helium despite the closed feed valve for the cooling medium supplied to the first heat exchanger.
• the first heat exchanger clogs and the function of the helium cleaning device is impaired.
• Such an undesirable temperature decrease can also occur with continuous operation of the helium cleaning device, in particular with continuous operation over, for example, 4 weeks or more. Due to the continuous operation, the entire device is continuously cooled.
• the object of the present invention is accordingly to avoid the problems outlined above.
• a method for separating undesired components, such as nitrogen, oxygen, hydrogen and / or neon, from a helium stream to be purified containing undesired components, this initially being exposed to a first cooling medium in a first cooling step a temperature that is above freezing point or, in the case of several undesirable components, is cooled down to a temperature that is above the highest freezing point of the undesired components, in such a way that one or more undesired component (s) condense or condense and thereby condensing undesired component (s) is or are separated from the helium stream to be purified, and wherein the helium stream is then further cooled in a second cooling step against a second cooling medium, so that the undesired (n ) Freeze component (s), and wherein the amount and / or composition of the or the cooling medium or cooling media used for the first and second cooling step can be controlled or regulated, the purified helium stream initially being used as
• a branch shortly before the first heat exchanger creates a simple possibility of specifically removing cooling power from the first cooling step without impairing the second cooling step.
• the temperature of the first heat exchanger can be increased in a targeted manner by the controllable branching off of part of the purified helium flow and / or the supply of warmer helium and / or warmer refrigerant. In this way it is possible to prevent the helium stream to be purified from being cooled to below 62 K in the first cooling step and thus to prevent it from freezing out in the first cooling step.
• the helium stream is subjected to an adsorption process serving to separate off hydrogen and / or neon.
• the temperature of the helium flow to be purified fed to the adsorption process is between 10 and 35 K.
• the adsorption process used to separate hydrogen and / or neon now makes it possible to safely separate the unwanted components neon and hydrogen, with the achievable temperature stability unwanted desorption of these components can be avoided.
• the hydrogen and neon components retained by the adsorption process are specifically desorbed at the beginning of the regeneration and, preferably blown out to the atmosphere. In this way an accumulation of these components in the recovery system is avoided.
• the hydrogen and neon components removed from the system can be fed to a treatment process.
• helium and / or a helium-rich fraction is used as the first and / or second cooling medium for the first and / or second cooling step. This is advantageous because the required low temperatures can be achieved in an effective way with helium as the refrigerant.
• the first refrigerant and the second refrigerant are expediently the same, preferably in such a way that the second refrigerant, after being used for the second cooling step, is used as the first refrigerant for the first cooling step.
• colder refrigerant is necessary than for the first cooling step. Therefore, after being used for the second cooling step, the refrigerant is still suitable for use for the first cooling step.
• the helium stream to be purified is preferably cooled in the first cooling step to a temperature which is a maximum of 8 K above the freezing point or, in the case of several undesirable components, a maximum of 8 K above the highest freezing point of the undesired components. Because the temperature is only slightly above the highest freezing point of the unwanted components, the maximum amount of unwanted components can condense without freezing out.
• a device for carrying out the method according to the first aspect is proposed, with a first heat exchanger and a second heat exchanger, which is set up to countercurrently flow a helium flow to be cleaned against itself and against a first and second cooling medium to cool, wherein the first heat exchanger is set up to carry out the first cooling step and the second heat exchanger is set up to carry out the second cooling step, the countercurrent of the purified helium from an outlet for the countercurrent of the second heat exchanger to an inlet for the countercurrent of the first heat exchanger a guide is guided, which can for example be a line or a line with a heat exchanger, and this guide has a branch and // or wherein the countercurrent of the purified helium from an outlet for the countercurrent of the second heat exchanger to an inlet for the countercurrent flow of the first heat exchanger is guided and this guide has a feed device, so that after it has been used as a cooling medium for the second cooling step, warmer helium can be
• the device preferably has an adsorber which is set up to subject the helium stream to be cleaned, after the second cooling step, to an adsorption process serving to separate off hydrogen and / or neon. In this way, the adsorption process step can be achieved.
• the countercurrent expediently has a branch (19) before it enters the second heat exchanger, so that helium during a regeneration of the device Can be branched off in a controllable or regulatable manner. This is advantageous to ensure problem-free regeneration.
• FIG. 1 shows a preferred embodiment of a device according to the invention in a schematic view
• FIG. 2 shows an alternative preferred embodiment of a device according to the invention in a schematic view.
• FIG. 1 a first preferred embodiment of a device according to the invention is shown in a schematic view and denoted as a whole by 100.
• the device 100 has a first heat exchanger 10, which can also be referred to as a condenser, which is composed here of two partial heat exchangers. It also has a second heat exchanger 11, which is also referred to as a freezer. It is set up to flow a helium stream 1A to be cleaned in countercurrent against itself and against a first and second To cool the cooling medium.
• the helium stream 1A to be cleaned is supplied by a helium supply device or via a line 1.
• the first heat exchanger 10 is set up to carry out a first cooling step.
• the helium stream 1A to be purified is first cooled to a temperature which is above the highest freezing point of undesired components in the helium stream 1A.
• this temperature is only slightly, for example 8 K, above the highest freezing point.
• the condensed components can now be transported to the second heat exchanger either via a line for the helium stream 1A to be cleaned or via a separate line as a liquid stream 1C.
• the temperature of the helium stream 1A to be cleaned in the first heat exchanger 10 should not fall below the highest freezing point of the undesired components, since otherwise clogging of the lines cannot be ruled out. It is also advantageous if the final temperature of the helium stream 1A to be purified after passing through the first heat exchanger is not higher than 8 K, preferably 2-7 K, above the highest freezing point of the undesired components. In this way, it is ensured that freezing out in the first heat exchanger 10 is prevented and, nevertheless, the largest possible amount of the undesired components condenses, so that the amount of unwanted components to be frozen out is reduced in the second heat exchanger 11.
• This temperature should therefore be regulated, especially if the proportion of impurities in the helium stream 1A to be cleaned fluctuates.
• a pressure at this point can in particular be regulated to 25 bar.
• the second heat exchanger 11 is set up to carry out a second cooling step. In the second cooling step, the unwanted components freeze out. Nitrogen in particular freezes out at this point. The frozen nitrogen remains on the heat transfer surface in the second heat exchanger. If the process is interrupted, for example to regenerate and warm up the system, this nitrogen melts and is collected in a container, as at 110 indicated.
• the undesired components that have condensed in the first heat exchanger and have been transported to the second heat exchanger 11 as a liquid stream 1C are also collected in the container 110.
• a temperature of the helium stream to be cleaned after passing through the second heat exchanger 11 can in particular be regulated to 32 K.
• a pressure at this point can preferably be 24.8 bar.
• the device 100 has an adsorber 12 which is set up to subject the helium stream 1A to be cleaned to an adsorption process serving to separate hydrogen and / or neon after the second cooling step.
• the helium stream After passing through the adsorber 12, the helium stream, now referred to as the purified helium stream 1B to simplify the illustration, is passed through a first preparatory heat exchanger 13 in this embodiment.
• the helium stream now referred to as the purified helium stream 1B to simplify the illustration, is passed through a first preparatory heat exchanger 13 in this embodiment.
• this first one is referred to as the purified helium stream 1B to simplify the illustration.
• Preparation heat exchanger 13 is supplied with a cooling medium from a cooling medium source 3 via a second cooling medium valve 31 in a parallel flow direction. In this way, a temperature of the cooling medium and a temperature of the purified helium stream 1B can be matched to one another.
• the first preparatory heat exchanger 13 can also be operated in countercurrent. If the process is interrupted and the system is regenerated, a part of the purified helium stream 1B can be branched off via a first branch valve 17 and a first helium reservoir 5 after it has passed through the first preparatory heat exchanger 13 and before it re-enters the second heat exchanger , in particular a low-pressure cold box.
• Both the cooling medium and the purified helium stream 1B are then used for the second cooling step in the second heat exchanger 11 in countercurrent, but without being mixed with one another.
• the cooling medium and the purified helium stream 1B are heated, but are still cold enough to be used subsequently for the first cooling step.
• a branch 18 is provided for the purified helium stream 1B, via which part of the purified helium stream 1B is branched off by means of a second branch valve 15 and can be fed to the first helium reservoir 5.
• This branch serves to branch off part of the purified helium flow 1B in a controllable or regulatable manner, so that it is not available for the first cooling step.
• the cooling capacity can decrease and thus the temperature in the first heat exchanger can be increased, so that nitrogen or other undesirable components of the helium stream 1A to be purified can be frozen out in the first heat exchanger can be avoided.
• the cleaned helium stream 1B is fed to a second helium store 4 or a low-pressure cold box.
• the second cooling medium valve 32 can be completely closed.
• the second branch valve 15 can be opened between 10 and 30%, for example, in order to branch off part of the purified helium stream 1B from the second heat exchanger 11.
• a temperature of the second heat exchanger 11 can be controlled via the first cooling medium valve 31, essentially unaffected by the control values of the second branch valve 15 and the second cooling medium valve 32.
• the second branch valve 15 can be completely closed.
• the second refrigerant valve 32 can advantageously between 5 and 15% are opened in order to lower a temperature in the first heat exchanger 10.
• a temperature of the second heat exchanger 11 can be controlled or regulated via the first cooling medium valve 31, essentially unaffected by the control values of the second branch valve 15 and the second cooling medium valve 32.
• FIG. 2 shows an alternative embodiment of a device according to the invention, here designated by 200.
• the same reference symbols and components are not to be dealt with again in the following.
• the device 200 in FIG. 2 differs from the device 100 in FIG. 1 in that no branch 18 and no branch valve 15 are provided. It should be noted, however, that it is within the scope of the present invention to provide such a branch together with a corresponding connector in this embodiment as well.
• Heat exchanger 14 is provided.
• the cooling medium originating from the cooling medium source 3 is mixed with the further cooling medium after passing through the second heat exchanger 11 and supplied to the second preparatory heat exchanger 14.
• the cleaned helium stream 1B is fed to the second preparatory heat exchanger 14 after passing through the second heat exchanger, so that the temperatures can approach one another.
• a supply device 6 is provided for a warmer cooling medium, which can also be supplied to the cooling medium upstream of the second preparatory heat exchanger 14 via a heat supply valve 61.
• the warmer cooling medium can be, for example, warmer helium between 65 K and 283 K or warmer, but is not limited to this.
• the controllable or regulatable supply of a warmer cooling medium can also reduce the cooling capacity of the first heat exchanger 10.
• the second preparatory heat exchanger is not absolutely necessary, but is advantageous for this embodiment in order to prevent media with very different temperatures from reaching the first heat exchanger 10 in countercurrent.
• the cleaned helium stream 1B is supplied with warmer helium before it enters the first heat exchanger 10 to feed.
• This measure can also be combined with the measures of the first and / or second embodiment.
• the end temperature of the helium stream 1A to be cleaned can be corrected upwards and downwards after it has passed through the first heat exchanger 10.

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• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Engineering & Computer Science (AREA)
• Analytical Chemistry (AREA)
• Inorganic Chemistry (AREA)
• Physics & Mathematics (AREA)
• Mechanical Engineering (AREA)
• Thermal Sciences (AREA)
• General Engineering & Computer Science (AREA)
• Separation By Low-Temperature Treatments (AREA)

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Citations (5)

• 2021
  • 2021-03-30 KR KR1020227038409A patent/KR20230024884A/ko unknown
  • 2021-03-30 EP EP21716263.5A patent/EP4133228A1/de active Pending
  • 2021-03-30 WO PCT/EP2021/025121 patent/WO2021204422A1/de unknown
  • 2021-03-30 CN CN202180026876.1A patent/CN115362341A/zh active Pending
  • 2021-03-30 JP JP2022561635A patent/JP2023520804A/ja active Pending

Patent Citations (5)

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