[go: up one dir, main page]

EP4012249A1 - Verfahren und vorrichtung zur versorgung eines verbrauchers mit ethin einer gewünschten reinheit - Google Patents

Verfahren und vorrichtung zur versorgung eines verbrauchers mit ethin einer gewünschten reinheit Download PDF

Info

Publication number
EP4012249A1
EP4012249A1 EP21020118.2A EP21020118A EP4012249A1 EP 4012249 A1 EP4012249 A1 EP 4012249A1 EP 21020118 A EP21020118 A EP 21020118A EP 4012249 A1 EP4012249 A1 EP 4012249A1
Authority
EP
European Patent Office
Prior art keywords
ethyne
solvent
concentration
withdrawn
consumer
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.)
Withdrawn
Application number
EP21020118.2A
Other languages
English (en)
French (fr)
Inventor
Edward Feng
Michael Graf
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to CN202180088709.XA priority Critical patent/CN116670421A/zh
Priority to PCT/EP2021/025473 priority patent/WO2022122180A1/en
Priority to EP21819346.4A priority patent/EP4259964A1/de
Publication of EP4012249A1 publication Critical patent/EP4012249A1/de
Withdrawn legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C11/00—Use of gas-solvents or gas-sorbents in vessels
    • F17C11/002—Use of gas-solvents or gas-sorbents in vessels for acetylene

Definitions

  • the present invention relates to a method and an apparatus for supplying ethyne of a desired purity to a consumer.
  • High-quality (or purity) ethyne (also referred to as acetylene in the applied sciences) supply is required by some heat treatment processes, like Low Pressure Carburizing (LPC) and Diamond-Like Carbon coating (DLC), in the industry which requires a high standard of surface performance, especially for automobile industry.
  • LPC Low Pressure Carburizing
  • DLC Diamond-Like Carbon coating
  • Typical purities are 99.5% for LPC, and 99.7% or 99.9% for DLC.
  • acetone is widely used as the solvent due to its properties.
  • acetone is quite volatile, so solvent withdrawing is inevitable in the applications, and solvent concentration differs depending on the solvent type, temperature, gas flow rate and cylinder pressure, etc.
  • the solvent (acetone vapor CH 3 COCH 3 ) sent to LPC furnaces can lead to negative impacts, including contaminating the pipeline, valves, mass flow controllers, gas injection nozzles, producing variances to the process control (by adding extra oxygen), creating soot and/or tar, and lowering the efficiency of the vacuum system, gauges and pump, and decreasing yield and product quality, etc.
  • Solvent withdrawing is well known by gas suppliers and users, and some measures are taken to alleviate the impact to the process, including, for example, limiting acetylene withdrawal rate to a maximum value, e.g. 500 l/h per cylinder (or other container), defining a minimum residual cylinder pressure or weight in use (switch-over pressure), typically in the range from 3 bar to 8 bar, or installing filters made of porous material. All of the mentioned measures for purity control are based on empirical observations and are therefore either prone to failure in application or cause excessive costs (e.g. by defining a higher residual pressure and therefore wasting more ethyne than necessary).
  • ethyne also known as acetylene
  • the invention relies on determining a concentration of a solvent, particularly acetone, within a stream of ethyne withdrawn from a container and transporting the withdrawn ethyne depending on the determined concentration. It is therefore possible, to only transport ethyne if the purity requirement is fulfilled, thereby ensuring quality and safety of downstream process products and equipment, respectively. In some embodiments, the purity of the withdrawn ethyne may also be improved, if the determined concentration does not fulfill the purity requirement.
  • a method of supplying ethyne of a desired purity to a consumer comprises withdrawing ethyne from a container in which ethyne is solved in a solvent under pressure, determining a concentration of the solvent within the withdrawn ethyne and transporting the withdrawn ethyne to the consumer in dependence of the determined concentration.
  • the solvent may comprise acetone and/or dimethylformamide or other organic compounds.
  • determining the concentration of the solvent comprises determining a density of the withdrawn ethyne and/or reacting a part of the withdrawn ethyne with oxygen and determining the amount of oxygen consumed in the reaction. Both of these determination methods are robust, accurate and easy to implement within existing or new facilities and do not require expensive or overly complex equipment
  • the withdrawn ethyne is transported to the consumer, when the determined concentration of the solvent is below a threshold concentration.
  • a minimum purity of ethyne can be set and guaranteed.
  • a measure is taken, when the determined concentration of the solvent exceeds a threshold concentration. This enables control of the purity of ethyne supplied to downstream consumers, especially in situations when this purity is lower than the desired purity or approaching a minimum purity.
  • the measure in such a case, advantageously comprises one or more of issuing a warning signal, stopping withdrawal of ethyne from the container and starting withdrawal of ethyne from a second container.
  • the measure may also comprise purifying the withdrawn ethyne by separating the solvent at least partially from the ethyne. This enables a variety of counter measures to ensure the purity of ethyne delivered to the consumer meets quality requirements.
  • the method comprises removing the at least one solvent at least partially from the withdrawn ethyne affording purified ethyne by controlled condensation of the at least one solvent, and providing the purified ethyne to the consumer.
  • removing the at least one solvent is at least partially effected by cryotrapping, particularly at a pressure of more than 100 or 150 kPa (high pressure) and/or by adsorbing the at least one solvent, particularly at a pressure of below 150 or 100 kPa (so-called medium or middle pressure, also referred to as low pressure herein).
  • cryotrapping may also be performed at the lower pressure (i.e. in a middle or medium pressure pipe) which provides benefits regarding operating security as ethyne under high pressure conditions tends to be thermodynamically unstable.
  • the relative content of ethyne in the purified ethyne advantageously exceeds 99.0%, 99.5%, 99.8%, 99.9% or 99.99%. In such qualities, remaining impurities have no or at least only acceptable adversary effects on downstream processes and/or equipment
  • the threshold concentration is preferably below 10%, 5%, 3%, 1%, 0.5%, 0.1%, 0,01% or 0.001% by volume. This provides a large range of relevant purities and, therefore, flexible possibilities of process control or regulation.
  • the threshold (or thresholds) may be chosen by a user of the invention.
  • An apparatus for supplying ethyne of a desired purity to a consumer comprises means for connecting at least one container configured to store ethyne solved in a solvent to the apparatus, a concentration determining device, configured to determine a concentration of the solvent within a stream of ethyne, and means for transporting ethyne to the consumer with or without an intermedium buffer vessel, depending on a concentration value determined by the concentration determining device.
  • the apparatus may comprise (further) means for performing a method as described herein.
  • the apparatus may comprise at least one trap for trapping at least one solvent from a mixture containing ethyne and the at least one solvent, and means for transporting ethyne from the one or more connector(s) through the trap to the consumer, so as to purify the withdrawn ethyne, if necessary.
  • Such a trap may comprise a cryotrap, configured to condense the at least one solvent and to not condense ethyne. This is based on different condensation temperatures at a given pressure, wherein ethyne typically exhibits a lower condensation temperature as compared to the relevant solvent(s), particularly acetone or dimethylformamide.
  • the trap may comprise at least one adsorber with an adsorbent selectively adsorbing the at least one solvent over ethyne.
  • adsorbents typically comprise highly porous materials such as active carbon or porous ceramics.
  • condensation temperatures may be strongly increased locally, due to surface effects. Therefore, an adsorber may have a similar effect on residual solvent concentration as the above mentioned cryotrap.
  • a combination of cryotrapping and adsorbing of the at least one solvent may be implemented, e.g. by cooling the adsorber to cryogenic temperatures or by arranging a cryotrap upstream of the adsorber.
  • This latter arrangement may provide the advantage, that rough purification of ethyne may be effected in the cryotrap, whereas fine purification may be effected in the adsorber due to a much higher contact surface between the ethyne and the adsorbent in comparison to the contact surface between a wall of the cryotrap and the ethyne.
  • FIG. 1 an advantageous embodiment of an apparatus according to the invention is depicted in a schematic block diagram and collectively referred to as 100.
  • An advantageous embodiment of a method according to the invention is schematically shown in Figure 2 and collectively referred to as 200.
  • references to components of an apparatus in the following refer to the apparatus 100 as shown in Figure 1
  • references to steps of a method generally refer to the method 200 as illustrated in Figure 2 .
  • the apparatus 100 comprises a gas supply unit 110, a concentration determining device 130, a treatment unit 150 and a computing unit 140.
  • the gas supply unit may, for example, comprise a first container 112, a second container 114 and a selection means 116, which may be e.g. a three-way-valve.
  • the first 112 and second 114 containers may each comprise one or more storage tanks and are configured to store ethyne (aka acetylene) in a dissolved state, i.e. mixed with a solvent, for example acetone and/or dimethylformamide.
  • the selection means 116 is configured to selectively withdraw a gas 10 from at least one of the first 112 and second 114 containers. In some embodiments, it may also be configured to withdraw the gas 10 from both first and second containers 112, 114, simultaneously.
  • the selection means 116 is controlled by the computing unit 140, particularly electronically.
  • the concentration determining device 130 is configured to determine a concentration of the solvent, present in the containers 112, 114 within the withdrawn gas 10 and is arranged between the gas supply unit 110 and the treatment unit 150. In use, the concentration determining unit 130 delivers a signal containing information about the concentration of the solvent to the computing unit 140. Specific embodiments of such a concentration determining device 130 are described herein below in connection with Figures 3 and 4 .
  • the computing unit 140 may be provided, by way of example, as a microcomputer, a computing center, a server or a control unit, configured to control a complete operation of the apparatus 100.
  • the treatment unit 150 may comprise a furnace configured to controlled heating of an article, a substrate or other objects to be treated, for example, a furnace configured to perform a (low pressure) carburization (LPC) process of a steel article, a furnace for diamond-like carbon coating (DLC) or similar processes requiring ethyne of high purity.
  • the treatment unit 150 may also be controlled by the computing unit 140.
  • Step 210 may, therefore, comprise controlling the selecting means 116 to selectively connect the first container 112 to piping leading the withdrawn gas 10 to the treatment unit 150, passing the concentration determining device 130.
  • selecting means 116 may also be configured for controlling a downstream pressure of the gas 10.
  • step 210 may also comprise controlling selection means 116 to set or regulate a target pressure in the withdrawn gas 10.
  • a concentration of a solvent, for example acetone or dimethylformamide, within the withdrawn gas 10 is determined. Details regarding the method of determining the concentration will be discussed below in connection with the specific embodiments of concentration determining devices 130.
  • a decision step 230 the determined solvent concentration is compared to a threshold value, which optionally may be selected by a user or may be preset. If the solvent concentration is below the threshold value, the method 200 continues with a supply step 240, in which the withdrawn gas 10 is transported to the treatment unit 150 and used for the treatment process performed there. The method 200 may then return to step 210 and continue withdrawing gas 10 from the first container 112.
  • a threshold value which optionally may be selected by a user or may be preset. If the solvent concentration is below the threshold value, the method 200 continues with a supply step 240, in which the withdrawn gas 10 is transported to the treatment unit 150 and used for the treatment process performed there. The method 200 may then return to step 210 and continue withdrawing gas 10 from the first container 112.
  • step 230 the method 200 continues with an action step 250, in which a measure is taken in order to return the solvent concentration to below the threshold value.
  • a measure may comprise one or more of issuing a warning signal, e.g. to a user of the apparatus 100 or the computing unit 140, stopping withdrawal of ethyne from the first container 112 and starting withdrawal of ethyne from the second container 114.
  • a control signal may be sent to the selecting means 116, such that the first container 112 is disconnected from the supply line to the treatment unit 150 and the second container 114 is connected to the supply line in its stead.
  • the method 200 may then continue with step 210, now withdrawing the gas 10 from the second container 114 instead of the first container 112. This enables seamless operation of the treatment unit 150 while warranting the required or desired purity of the supplied gas 10.
  • the discussed issuance of a warning signal to a user of the apparatus enables the user to replace the first container 112 with a fresh first container 112, so that in a later step 250, the selecting means 116 may switch the gas supply unit 110 back to the first container 112 without adversely affecting the purity of gas 10.
  • FIG 1A an advantageous variation of the apparatus 100, as described with reference to Figure 1 , is schematically shown and collectively referred to with 100A.
  • the apparatus 100A additionally comprises a solvent trapping device 135.
  • the solvent trapping device 135 in the shown embodiment is connected to the piping upstream of it via a three-way-valve, controlled by the computing unit 140 according to the solvent concentration determined.
  • the apparatus 100A may comprise a pressure reducing valve to set a gas pressure to a pressure level required by treatment unit 150.
  • the pressure reducing valve may be regulated or controlled pneumatically through a pressure control device.
  • the pressure control may also be effected by electronic, hydraulic, magnetic or any other suitable means.
  • a decomposition barrier Downstream of the pressure reducing valve a decomposition barrier may be arranged downstream of the pressure reducing valve.
  • a decomposition barrier also known as flashback arrestor, is typically configured to stop a decomposition front running from downstream it into an upstream direction in order to prevent a dangerous chain reaction, in which gas supply unit 110 might otherwise be critically damaged or destroyed.
  • Such a decomposition front may arise from too high temperatures in downstream components, particularly in treatment unit 150.
  • the decomposition barrier prevents the decomposition front from expanding upstream by diverting flow and decelerating the reaction.
  • An automatically closing valve at the entrance of the decomposition barrier may be provided to physically disconnect the barrier from upstream components of apparatus 100/100A.
  • the solvent trapping device 135 there positions in a high pressure region of apparatus 100A, i.e. upstream of the mentioned pressure reducing valve, and positions in a low pressure region of apparatus 100A, i.e. downstream of the pressure reducing valve and preferably also downstream of the decomposition barrier.
  • the high pressure region is operated at a pressure in the range of more than 100 or 150 kPa up to 2.5 MPa, while the low (or medium resp. middle) pressure region may be operated at a pressure in the range of 20 kPa to below 150 or 100 kPa.
  • the separation limit between the two pressure regions may depend on local legislation and/or standards.
  • a cryotrap may be installed in the high pressure region.
  • the cryotrap may particularly comprise a vessel through which the gas 10 is conducted and which comprises a heat exchanger, wherein the medium to which heat is transferred may comprise liquid nitrogen, liquid argon or any other suitable medium capable of being operated at cryogenic temperatures, particularly at temperature levels below -20 °C.
  • the solvent if contained within the gas 10 withdrawn from gas supply unit 110, will at least partially condense at the wall of the vessel of the cryotrap, such that a remaining partial pressure of the solvent is below a tolerable value.
  • a regeneration of the cryotrap may simply be effected by emptying the vessel, e.g. in predefined time intervalls or when the vessel is filled to a certain degree or level, as may be determined by a sensor within the cryotrap.
  • the preferred position is in the low pressure region of apparatus 100A in order to prevent ethyne adsorption to the adsorber.
  • the lower pressure increases adsorption selectivity towards the solvent.
  • an adsorber may, for example, be configured for temperature swing adsorption (TSA), pressure swing adsorption (PSA) or vacuum pressure swing adsorption (VPSA).
  • TSA temperature swing adsorption
  • PSA pressure swing adsorption
  • VPSA vacuum pressure swing adsorption
  • two adsorbers may be provided in parallel and operated alternately, such that during an adsorption phase, in which a first adsorber is provided with the gas 10 withdrawn from gas supply unit 110, a second adsorber is regenerated, i.e.
  • adsorbed solvent is withdrawn from the second adsorber, e.g. by lowering the pressure (PSA/VPSA) or increasing the temperature (TSA) and optionally flushing with a purge gas (e.g. gas 10 or a partial stream of purified gas 10).
  • a purge gas e.g. gas 10 or a partial stream of purified gas 10.
  • This operation scheme may be reversed periodically, such that each of the first and second adsorbers is regenerated and used for purification alternatingly.
  • the solvent removed from the trapping device 135 may be collected in a solvent stream 14.
  • step 250 may comprise controlling the three-way-valve 118 to open the path towards the solvent trapping device 135 and closing the direct path towards the treatment unit 150.
  • the concentration determining device 130 may also be arranged downstream the solvent trapping device 135, thereby enabling a determination after which time, a regeneration of the solvent trapping device 135 may be necessary or a determination, when a changeover between the first 112 and second 114 containers of the gas supply unit 110 is necessary. This may be the case, when the solvent concentration in the withdrawn raw ethyne 10 upstream the solvent trapping device 135 increases to such high amounts that the purification capacity of the solvent trapping device is insufficient to lower this concentration to a concentration below the acceptable threshold.
  • the depicted apparatus 100 corresponds, in its essential parts, to the apparatus 100 as described in connection with Figure 1 , above. Attention is drawn to the specific design of the concentration determining device 130, which in this example comprises a combustion chamber 132, configured to react a partial stream 13 of the withdrawn gas 10 with oxygen 136 to an exhaust gas product 15.
  • the combustion chamber 132 may be equipped with suitable catalyst materials in order to enable or accelerate the reaction of the gas of partial stream 13 with the oxygen 136.
  • the device 130 further comprises a sensor 134 for determining an oxygen concentration within the exhaust gas product 15.
  • This sensor 134 may, for example, be provided in the form of a lambda sensor, particularly a broadband lambda sensor, such that a signal provided by the sensor contains information about the concentration of oxygen within the exhaust gas product Combined with an information about the amounts of oxygen 136 and gas in partial stream 13, this enables determining a composition of the partial stream 13. This determination is based on different oxygen consumption during combustion by ethyne (2.5 molecules of oxygen per molecule of ethyne) and solvent (4 molecules of oxygen per molecule of acetone, or 4.25 molecules of oxygen per molecule of dimethylforamide), respectively.
  • ethyne 2.5 molecules of oxygen per molecule of ethyne
  • solvent molecules of oxygen per molecule of acetone, or 4.25 molecules of oxygen per molecule of dimethylforamide
  • the amount of oxygen consumed by the reaction in the combustion chamber 132 can be easily calculated and the composition of the two-compound stream 13 can be deduced from this information.
  • the temperature of the sensor 134 may be controlled to be in a range in which the sensor 134 exhibits a high sensitivity towards oxygen concentration, e.g. by a sensor heater. This is an important influence parameter regarding the overall performance of the invention in this embodiment.
  • a partial stream 13 of the withdrawn gas 10 is directed to the combustion chamber 132.
  • This partial stream 13 can amountto, for example, less than 10%, 5%, 1%, 0.1% or 0.01% of the withdrawn gas 10.
  • the amount of the partial stream 13 may be controlled with a mass flow controller, for example.
  • an oxygen gas stream 136 is provided to the combustion chamber 132, again under controlled conditions, such that a ratio between the amount of partial stream 13 and oxygen gas 136 in combustion chamber 132 is known.
  • the mixture resulting in combustion chamber 132 may then be ignited in order to react the gas of partial stream 13 completely with the oxygen of stream 136.
  • the produced exhaust gas 15 is then analyzed with the sensor 134, e.g. a conventional lambda sensor or another type of electrochemical oxygen probe, such that a signal of the sensor includes information about the oxygen content within the exhaust gas 15.
  • the sensor 134 e.g. a conventional lambda sensor or another type of electrochemical oxygen probe, such that a signal of the sensor includes information about the oxygen content within the exhaust gas 15.
  • a signal from an electrochemical sensor i.e. a concentration element
  • the sensor signal may be used to control the amount of oxygen 136 provided to the combustion chamber 132, e.g. by a mass flow controller.
  • the amount of oxygen in such a case is controlled in such a manner, that the signal of sensor 134 remains constant, while the amount of partial stream 13 is also kept at a constant flow. Then, the amount of oxygen 136 provided to the combustion chamber 132 can be used for determining the ratio of ethyne to solvent in partial stream 13.
  • FIG 4 an advantageous embodiment of an apparatus 100 with another exemplary embodiment of a concentration determining device 130, usable in connection with the invention is schematically illustrated.
  • the working principle of concentration determining device 130 is based on a measurement of a mass density of the withdrawn gas 10, e.g. by measuring buoyancy acting upon a probe body 135 within the gas 10.
  • This relies on the different densities of ethyne ( ⁇ 1.1 kg/m 3 at standard temperature and pressure) and the solvent vapor ( ⁇ 2.6 kg/m 3 for acetone, ⁇ 3 kg/m 3 for dimethylforamide), respectively.
  • the relative densities therefore, correspond to about 0.9 for ethyne, about 2 for acetone and roughly 2.5 for dimethylformamide, as compared to air.
  • step 220 comprises determining the density of the gas stream 10, e.g. by measuring the buoyancy of a probe body 135 within the gas 10 and calculating the solvent concentration from the density determined.
  • determining the concentration of the solvent within gas 10 may be performed simultaneously with providing the gas 10 to the treatment unit 150 (step 240).
  • the threshold value is preferably selected such that even after exceeding the threshold concentration, the minimum purity requirements for ethyne, as acceptable for the treatment in step 240, are still met. This means that a switch over (step 250) to the second container 114 is still timely enough, even after exceeding the threshold in step 230, if performed directly after the threshold value was exceeded.
  • a similar argumentation may hold for different sets of method steps. Even the stepwise arrangement of method 200 altogether may be altered in favor of a continuous performance, so that the existence of distinct steps may be avoided altogether, in some embodiments. Therefore, the stepwise performance of method 200 is to be understood solely for illustration purposes and in no way limiting the scope of the present invention.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
EP21020118.2A 2020-12-11 2021-03-03 Verfahren und vorrichtung zur versorgung eines verbrauchers mit ethin einer gewünschten reinheit Withdrawn EP4012249A1 (de)

Priority Applications (3)

Application Number Priority Date Filing Date Title
CN202180088709.XA CN116670421A (zh) 2020-12-11 2021-11-30 用于向消费者供应期望纯度的乙炔的方法和设备
PCT/EP2021/025473 WO2022122180A1 (en) 2020-12-11 2021-11-30 Method and an apparatus for supplying ethyne of a desired purity to a consumer
EP21819346.4A EP4259964A1 (de) 2020-12-11 2021-11-30 Verfahren und vorrichtung zum zuführen von ethin gewünschter reinheit zu einem verbraucher

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP20020608 2020-12-11

Publications (1)

Publication Number Publication Date
EP4012249A1 true EP4012249A1 (de) 2022-06-15

Family

ID=74194458

Family Applications (1)

Application Number Title Priority Date Filing Date
EP21020118.2A Withdrawn EP4012249A1 (de) 2020-12-11 2021-03-03 Verfahren und vorrichtung zur versorgung eines verbrauchers mit ethin einer gewünschten reinheit

Country Status (1)

Country Link
EP (1) EP4012249A1 (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2024084701A (ja) * 2022-12-13 2024-06-25 レール・リキード－ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード アセチレンを供給するシステム及び方法

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5884896A (ja) * 1981-11-13 1983-05-21 Nichigou Asechiren Kk アセトン含有量の少ないアセチレンガスまたはアセチレンを主体とする混合ガスの放散方法
JP2013194004A (ja) * 2012-03-21 2013-09-30 Taiyo Nippon Sanso Corp 溶解アセチレンの精製方法

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5884896A (ja) * 1981-11-13 1983-05-21 Nichigou Asechiren Kk アセトン含有量の少ないアセチレンガスまたはアセチレンを主体とする混合ガスの放散方法
JP2013194004A (ja) * 2012-03-21 2013-09-30 Taiyo Nippon Sanso Corp 溶解アセチレンの精製方法

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2024084701A (ja) * 2022-12-13 2024-06-25 レール・リキード－ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード アセチレンを供給するシステム及び方法
EP4390605A1 (de) * 2022-12-13 2024-06-26 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude System und verfahren zur zufuhr von acetylen

Similar Documents

Publication Publication Date Title
US7258725B2 (en) Gas supplying method and system
EP2111905B1 (de) Verbesserungen von zyklischen Wechseladsorptionsverfahren
TWI494302B (zh) 純化乙炔之方法
US20080242912A1 (en) Methods and Apparatus for Providing a High Purity Acetylene Product
CA2641155C (en) Purification of noble gases using online regeneration of getter beds
US5296017A (en) Method and apparatus for concentrating chlorine gas
US8915992B2 (en) Process and system for providing acetylene
EP1841690A1 (de) Verfahren zur rückgewinnung eines edelgases aus einem gasgemisch
KR101486110B1 (ko) 오염물이 가스 정제기에 도달하는 것을 방지하기 위한 시스템
US8187365B2 (en) Process for removal of metal carbonyls from a synthesis gas stream
EP1101732A1 (de) Verfahren und Vorrichtung zur kontinuierlichen Erzeugung von hochkonzentriertem Ozongas
EP0471213B1 (de) Methode und System der Regelung mit Membran oder Deoxo
EP4012249A1 (de) Verfahren und vorrichtung zur versorgung eines verbrauchers mit ethin einer gewünschten reinheit
JP6483465B2 (ja) 塩化水素の製造方法
EP4259964A1 (de) Verfahren und vorrichtung zum zuführen von ethin gewünschter reinheit zu einem verbraucher
CN114401781A (zh) 纯化气体的制造方法、有价值物的制造方法、气体纯化装置和有价值物制造装置
CN116670421A (zh) 用于向消费者供应期望纯度的乙炔的方法和设备
US20070151452A1 (en) Systems for purifying gases having organic impurities using granulated porous glass
JP3570732B2 (ja) 塩素ガスの濃縮方法および装置
CN116966749A (zh) 工业氮提纯装置及工业氮提纯工艺方法
US20060198780A1 (en) Method and apparatus for removing CO2 in mixed gas such as biogas
JP5108184B2 (ja) 一酸化炭素の精製方法
JPH08117542A (ja) 圧力変動吸着分離法における製品ガス安定化方法
Zhou et al. Experiments of Removing Trace Hydrogen Sulfide from Natural Gas with Two Column Pressure Swing Operation
JP2002068717A (ja) 三フッ化窒素の精製方法

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION HAS BEEN PUBLISHED

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20221216