WO2018056203A1 - Procédé de purification d'hydrogène ou de gaz hélium, et appareil de purification d'hydrogène ou de gaz hélium - Google Patents

Procédé de purification d'hydrogène ou de gaz hélium, et appareil de purification d'hydrogène ou de gaz hélium Download PDF

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Publication number
WO2018056203A1
WO2018056203A1 PCT/JP2017/033430 JP2017033430W WO2018056203A1 WO 2018056203 A1 WO2018056203 A1 WO 2018056203A1 JP 2017033430 W JP2017033430 W JP 2017033430W WO 2018056203 A1 WO2018056203 A1 WO 2018056203A1
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Prior art keywords
gas
adsorbent
adsorption tower
adsorption
hydrogen
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PCT/JP2017/033430
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English (en)
Japanese (ja)
Inventor
光利 中谷
沙織 田中
貴裕 土屋
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住友精化株式会社
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Priority to JP2018541039A priority Critical patent/JP6979023B2/ja
Priority to KR1020197009111A priority patent/KR102391642B1/ko
Priority to CN201780058840.5A priority patent/CN109789368A/zh
Publication of WO2018056203A1 publication Critical patent/WO2018056203A1/fr
Priority to PH12019500649A priority patent/PH12019500649A1/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B01D53/053—Pressure swing adsorption with storage or buffer vessel
    • 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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids

Definitions

  • the power cost for applying the vacuum is high. Further, in the method using a high-purity product gas purified as a purge gas for regenerative cleaning, the cost is increased due to the use of the product gas. Furthermore, the regeneration by heating also leads to an increase in cost for the energy required for heating.
  • the present invention has been conceived under such circumstances, using a pressure fluctuation adsorption method, while reducing costs from a raw material gas containing hydrocarbon gas or volatile hydrocarbon as an impurity. It is an object of the present invention to provide a method and an apparatus suitable for obtaining high-purity hydrogen or helium.
  • hydrocarbon gas or volatile as impurities can be obtained by repeating the cycle of the pressure fluctuation adsorption method performed using three or more adsorption towers filled with an adsorbent for each adsorption tower.
  • a method for purifying hydrogen or helium from a source gas containing at least one of hydrocarbons and containing hydrogen or helium as a main component In the cycle, in the state where the adsorption tower is at a predetermined high pressure, the raw material gas is introduced into the adsorption tower, and at least one of the hydrocarbon gas or volatile hydrocarbon in the raw material gas is used as the adsorbent.
  • An adsorption process for adsorbing and discharging a product gas having a high hydrogen or helium concentration from the adsorption tower, and a gas remaining in the tower from the adsorption tower after the adsorption process is exhausted to lower the pressure in the tower A depressurization step, a desorption step in which at least one of the hydrocarbon gas or volatile hydrocarbon is desorbed from the adsorbent in the adsorption tower after the depressurization step and the gas in the column is discharged, and the other in the depressurization step And a cleaning step of introducing the gas discharged from the adsorption tower into the adsorption tower after the desorption step and discharging the gas remaining in the tower.
  • the source gas contains hydrogen sulfide as an impurity.
  • the first region is filled with a silica gel-based first adsorbent having a filling ratio in the range of 15 to 65 vol%.
  • the first region is filled with an activated carbon-based second adsorbent having a filling ratio in the range of 10 to 50 vol%.
  • the third region is filled with a zeolite-based third adsorbent having a filling ratio in the range of 25 to 75 vol%.
  • the source gas contains hydrogen sulfide as an impurity.
  • the first adsorbent is made of hydrophilic silica gel.
  • the present inventors diligently studied a method for separating hydrogen or helium from a source gas containing hydrocarbon gas or volatile hydrocarbon and hydrogen sulfide as impurities by the pressure fluctuation adsorption method.
  • silica gel which is an adsorbent
  • activated carbon which is an adsorbent that does not adsorb volatile hydrocarbons
  • the desorption process is completed using a relatively clean gas in the zeolite layer.
  • the present invention it is possible to purify the content of plural kinds of hydrocarbons contained as impurities in hydrogen or helium to 1 volppm or less and hydrogen sulfide to 0.2 ppb or less at low cost and in a space-saving device.
  • FIG. 1 shows a schematic configuration of a purification apparatus X that can be used for carrying out the method for purifying hydrogen or helium according to the present invention.
  • the purification apparatus X includes three adsorption towers 10A, 10B, and 10C, a raw material gas supply source 21, a product storage tank 22, an offgas tank 23, a cooler 24, a gas-liquid separator 25, and lines 31 to 35.
  • the purification apparatus X is configured to be capable of concentrating and separating hydrogen or helium from a source gas containing hydrogen or helium (crude hydrogen or crude helium) using a pressure fluctuation adsorption method (PSA method).
  • PSA method pressure fluctuation adsorption method
  • the raw material gas there can be mentioned a gas mainly containing hydrogen produced from organic hydride and containing impurities such as hydrocarbon gas, volatile hydrocarbon and hydrogen sulfide.
  • the hydrocarbon gas means a hydrocarbon which has 4 or less carbon atoms and is a gas at normal temperature and pressure, and includes, for example, methane, ethane, propane, butane, ethylene, butylene, propylene and the like.
  • the volatile hydrocarbon refers to a hydrocarbon having 5 to 18 carbon atoms and liquid at normal temperature and pressure, and includes, for example, toluene, cyclohexane, methylcyclohexane, benzene and the like.
  • the present invention can also be applied to the case where the main component of the source gas is helium. Further, the following description will be made on the case where hydrocarbon gas, volatile hydrocarbon, and hydrogen sulfide are included as impurities. However, the present invention may be any one of hydrocarbon gas and volatile hydrocarbon, or hydrocarbon gas as impurities. It is also applicable to the case where any one of volatile hydrocarbons and hydrogen sulfide is included.
  • An adsorbent 132 and a third adsorbent 133 are sequentially stacked.
  • an adsorbent having a property of preferentially adsorbing volatile hydrocarbons is used.
  • adsorbents include silica gel-based adsorbents (hydrophilic silica gel, hydrophobic silica gel, etc.), among which hydrophilic silica gel, particularly silica gel B type is preferable.
  • hydrophilic silica gel particularly silica gel B type is preferable.
  • second and third adsorbents 132 and 133 adsorbents having relatively low adsorbability for volatile hydrocarbons are used.
  • the second adsorbent 132 one having the property of preferentially adsorbing hydrogen sulfide is used.
  • Examples of such an adsorbent include activated carbon derived from coconut shell or coal.
  • As the 3rd adsorption agent 133 what has the property to adsorb hydrocarbon gas preferentially is used.
  • Examples of such adsorbents include zeolite-based adsorbents (A-type zeolite, CaA-type zeolite, Y-type zeolite, etc.), among which CaA-type zeolite is preferable. These adsorbents are generally commercially available, are readily available, and do not require pretreatment.
  • Silica gel (or silica) is inherently hydrophilic because it has a hydroxyl group on the surface, and becomes hydrophobic when subjected to a hydrophobizing treatment such as high temperature heating or reaction with an alkylsilylating agent. Conventionally, this hydrophobization treatment has been a cause of cost increase.
  • the product storage tank 22 is a pressure vessel for storing gas (product gas described later) discharged from the gas passage port 12 of the adsorption towers 10A, 10B, and 10C.
  • the line 34 is for supplying a part of product gas flowing through the line 33 (main trunk line 33 ′) to the adsorption towers 10 A, 10 B, 10 C, and is connected to the main path 33 ′ of the line 33.
  • An automatic valve 341 and a flow rate adjustment valve 342 are provided on the main trunk line 34 '.
  • Automatic valves 34a, 34b, 34c are provided in the branch paths 34A, 34B, 34C.
  • each of the adsorption towers 10A, 10B, and 10C includes an adsorption process, a pressure reduction process, a pressure equalization process (decompression), a desorption process, a cleaning process, a pressure equalization process (pressure increase), and a pressure increase process.
  • adsorption process DP Depressurization process
  • DS Desorption process
  • RN Cleaning process
  • PR Pressure increase process
  • Eq-DP Pressure equalization pressure reduction process
  • Eq-PR Pressure equalization pressure increase process
  • step 1 the automatic valves 31a, 33a, 32b, 34b, 35c, 351 and the flow rate adjusting valve 352 are opened, and the gas flow state as shown in FIG. 2a is achieved.
  • step 2 the adsorption step is continued in the adsorption tower 10A. Also in step 2, the gas passage ports 12 of the adsorption towers 10B and 10C communicate with each other via lines 34 and 35, respectively. On the other hand, the automatic valve 32b is closed for the adsorption tower 10B. At the start of step 2, the pressure in the adsorption tower 10C is still higher than that in the adsorption tower 10B. Therefore, pressure equalization / pressure reduction is performed in the adsorption tower 10C, and pressure equalization / pressure increase is performed in the adsorption tower 10B.
  • the gas in the adsorption tower 10C is introduced into the adsorption tower 10B via the lines 35 and 34, the pressure in the adsorption tower 10C is reduced, and the pressure in the adsorption tower 10B is increased. .
  • the operation time in step 2 is, for example, about 15 seconds.
  • Steps 7 to 9 the operation performed on the adsorption tower 10A in Steps 1 to 3 is performed on the adsorption tower 10C, and the operation performed on the adsorption tower 10B in Steps 1 to 3 is performed.
  • the operation performed on the adsorption tower 10A and the operation performed on the adsorption tower 10C in steps 1 to 3 are performed on the adsorption tower 10B.
  • the filling ratio of the first adsorbent 131 is less than 15 vol%, volatile hydrocarbons may not be sufficiently removed.
  • the filling ratio of the first adsorbent 131 exceeds 75 vol%, the ratio of the cleaning gas remaining in the third adsorbent 133 decreases, the amount of cleaning gas decreases, and the cleaning in the cleaning process becomes insufficient. There is a fear.
  • the filling ratio of the second adsorbent 132 is less than 10 vol%, hydrogen sulfide may not be sufficiently removed.
  • the cleaning gas exhausted from the adsorption tower in the depressurization process after completion of the adsorption process and used for cleaning other adsorption towers in the desorption process after completion of the desorption process is Hydrogen desorbed from the third adsorbent 133 is added to the concentrated hydrogen gas remaining in the gas (mainly the gas in the filling region of the third adsorbent 133 close to the gas passage port 12).
  • the other adsorption tower after the completion of the desorption process can be effectively cleaned using the cleaning gas having an increased hydrogen content.
  • the present invention is not limited to these embodiments, and various modifications can be made without departing from the spirit of the invention.
  • a configuration different from the above-described embodiment may be adopted for the configuration of the line (pipe) forming the gas flow path in the apparatus for carrying out the method for purifying hydrogen or helium according to the present invention.
  • the number of adsorption towers is not limited to the three-column type shown in the above embodiment, and the same effect can be expected even when there are four or more towers.
  • adsorption towers 10A, 10B, and 10C cylindrical ones having an inner diameter of 35 mm were used, and the adsorbent filling capacity was about 1 L (liter).
  • silica gel B type Fluji Silica Silica B type manufactured by Fuji Silysia Chemical Co.
  • Activated carbon as 132 PGAR manufactured by Caterer
  • CaA-type zeolite 5AHP manufactured by Union Showa
  • Example 2 The same as in Example 1 except that the adsorbent filling ratio (volume ratio) was 10 vol% for the first adsorbent 131, 10 vol% for the second adsorbent 132, and 80 vol% for the third adsorbent 133. Hydrogen was purified from the source gas. Moreover, when the impurity concentration in the obtained concentrated hydrogen gas (product gas) was measured with a hydrogen flame ion detector (FID) and a flame photometric detector (FPD), the toluene concentration in the product gas was 3000 volppm, and the methane concentration was The 0.01 volppm, hydrogen sulfide concentration was below the lower limit of quantification (0.1 volppb or less), and the hydrogen gas recovery rate was 70%. The results of this comparative example are shown in Table 1.
  • FID hydrogen flame ion detector
  • FPD flame photometric detector

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Combustion & Propulsion (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

Dans ce procédé de purification de gaz d'hydrogène ou d'hélium à l'aide du procédé PSA, dans lequel des colonnes d'adsorption (10A-10C) remplis d'adsorbants sont utilisés pour purifier un gaz d'alimentation qui contient au moins un hydrocarbure gazeux ou un hydrocarbure volatil en tant qu'impureté et contient de l'hydrogène ou du gaz d'hélium en tant que composant principal, un cycle comprenant une étape d'adsorption, une étape de décompression, une étape de désorption et une étape de lavage est effectué de façon répété. Chaque colonne d'adsorption est divisée dans l'ordre en une première zone, une deuxième zone et une troisième zone depuis le côté amont vers le côté aval dans la direction d'écoulement du gaz d'alimentation dans la colonne d'adsorption. La première zone est remplie d'un premier adsorbant à base de gel de silice (131), dont le rapport de remplissage est dans la plage de 15 à 65 % en volume par rapport à la capacité de remplissage totale de l'adsorbant. La seconde zone est remplie d'un second adsorbant à base de charbon actif (132), dont le rapport de remplissage est dans la plage de 10 à 50 % en volume. La troisième zone est remplie d'un troisième adsorbant à base de zéolithe (133), dont le rapport de remplissage se situe dans la plage de 25 à 75 % en volume.
PCT/JP2017/033430 2016-09-26 2017-09-15 Procédé de purification d'hydrogène ou de gaz hélium, et appareil de purification d'hydrogène ou de gaz hélium WO2018056203A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
JP2018541039A JP6979023B2 (ja) 2016-09-26 2017-09-15 水素またはヘリウムの精製方法、および水素またはヘリウムの精製装置
KR1020197009111A KR102391642B1 (ko) 2016-09-26 2017-09-15 수소 또는 헬륨의 정제방법 및 수소 또는 헬륨의 정제장치
CN201780058840.5A CN109789368A (zh) 2016-09-26 2017-09-15 氢气或氦气的精制方法、以及氢气或氦气的精制装置
PH12019500649A PH12019500649A1 (en) 2016-09-26 2019-03-25 Method for purifying hydrogen or helium gas, and apparatus for purifying hydrogen or helium gas

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JP2016-186677 2016-09-26
JP2016186677 2016-09-26
JP2016238474 2016-12-08
JP2016-238474 2016-12-08

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JP (1) JP6979023B2 (fr)
KR (1) KR102391642B1 (fr)
CN (1) CN109789368A (fr)
PH (1) PH12019500649A1 (fr)
TW (1) TWI734835B (fr)
WO (1) WO2018056203A1 (fr)

Cited By (1)

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Publication number Priority date Publication date Assignee Title
CN114950068A (zh) * 2021-02-22 2022-08-30 国家能源投资集团有限责任公司 混合气变温变压吸附分离的方法和系统

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CN113735078A (zh) * 2020-05-27 2021-12-03 中国石油化工股份有限公司 从lng工厂的bog尾气中回收氦气的方法、系统及回收的氦气

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH119935A (ja) * 1997-06-25 1999-01-19 Nippon Steel Corp Ｐｓａ法による製品水素ガスの品質制御方法
JP2001300244A (ja) * 2000-04-20 2001-10-30 Mitsubishi Kakoki Kaisha Ltd 水素製造用圧力変動吸着装置の吸着塔
JP2004042013A (ja) * 2001-12-28 2004-02-12 Syst Enji Service Kk 揮発性炭化水素含有排ガスの処理方法及び該方法を実施するための装置
US20060254425A1 (en) * 2002-12-24 2006-11-16 Baksh Mohamed Safdar A Process and apparatus for hydrogen purification
WO2008047828A1 (fr) * 2006-10-20 2008-04-24 Sumitomo Seika Chemicals Co., Ltd. Procédé et appareil de séparation de gaz d'hydrogène

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP3011094B2 (ja) 1995-05-27 2000-02-21 システム エンジ サービス株式会社 廃棄ガスに含まれるガス状炭化水素の処理・回収方法
JP2925522B2 (ja) 1997-06-17 1999-07-28 システム エンジ サービス株式会社 ガス状炭化水素を含む廃棄ガスから炭化水素を液状で回収する方法
JP3089297B2 (ja) 1998-03-18 2000-09-18 農林水産省畜産試験場長 嫌気性汚水処理用後処理装置
JP2000102779A (ja) 1998-09-29 2000-04-11 Kubota Corp メタンガス発生促進方法
US6913638B2 (en) * 2000-12-25 2005-07-05 Sumitomo Seika Chemicals Co., Ltd. Method for separating hydrogen gas
JP2002275482A (ja) 2001-03-16 2002-09-25 Ebara Corp 消化ガスによる発電方法及び発電システム
FR2836061B1 (fr) 2002-02-15 2004-11-19 Air Liquide Procede de traitement d'un melange gazeux comprenant de l'hydrogene et du sulfure d'hydrogene
US7390350B2 (en) * 2005-04-26 2008-06-24 Air Products And Chemicals, Inc. Design and operation methods for pressure swing adsorption systems
EP2080735A4 (fr) * 2006-11-08 2010-12-01 Sumitomo Seika Chemicals Procédé de séparation de l'hydrogène gazeux et appareil de séparation
CN102199433A (zh) * 2011-03-05 2011-09-28 何巨堂 一种以co2为燃烧过程控温组分的煤炭化工艺
JP5675505B2 (ja) * 2011-06-07 2015-02-25 住友精化株式会社 目的ガス分離方法、および目的ガス分離装置
US20160097013A1 (en) * 2013-06-19 2016-04-07 Kent S. Knaebel & Associates, Inc. PSA Separation of Nitrogen from Natural Gas

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH119935A (ja) * 1997-06-25 1999-01-19 Nippon Steel Corp Ｐｓａ法による製品水素ガスの品質制御方法
JP2001300244A (ja) * 2000-04-20 2001-10-30 Mitsubishi Kakoki Kaisha Ltd 水素製造用圧力変動吸着装置の吸着塔
JP2004042013A (ja) * 2001-12-28 2004-02-12 Syst Enji Service Kk 揮発性炭化水素含有排ガスの処理方法及び該方法を実施するための装置
US20060254425A1 (en) * 2002-12-24 2006-11-16 Baksh Mohamed Safdar A Process and apparatus for hydrogen purification
WO2008047828A1 (fr) * 2006-10-20 2008-04-24 Sumitomo Seika Chemicals Co., Ltd. Procédé et appareil de séparation de gaz d'hydrogène

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114950068A (zh) * 2021-02-22 2022-08-30 国家能源投资集团有限责任公司 混合气变温变压吸附分离的方法和系统

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TW201827335A (zh) 2018-08-01
TWI734835B (zh) 2021-08-01
PH12019500649A1 (en) 2019-07-29
JPWO2018056203A1 (ja) 2019-07-04
KR102391642B1 (ko) 2022-04-27
KR20190052018A (ko) 2019-05-15
CN109789368A (zh) 2019-05-21
JP6979023B2 (ja) 2021-12-08

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