WO1997016399A1 - Procede et appareil de concentration du methane dans les gaz de fermentation digestive anaerobie - Google Patents

Procede et appareil de concentration du methane dans les gaz de fermentation digestive anaerobie Download PDF

Info

Publication number
WO1997016399A1
WO1997016399A1 PCT/JP1996/003050 JP9603050W WO9716399A1 WO 1997016399 A1 WO1997016399 A1 WO 1997016399A1 JP 9603050 W JP9603050 W JP 9603050W WO 9716399 A1 WO9716399 A1 WO 9716399A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
module
methane
separation membrane
permeate
Prior art date
Application number
PCT/JP1996/003050
Other languages
English (en)
Japanese (ja)
Inventor
Masahiro Inoue
Kazuo Haruna
Original Assignee
Sumitomo Seika Chemicals Co., Ltd.
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 Sumitomo Seika Chemicals Co., Ltd. filed Critical Sumitomo Seika Chemicals Co., Ltd.
Priority to AU73345/96A priority Critical patent/AU7334596A/en
Publication of WO1997016399A1 publication Critical patent/WO1997016399A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • 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
    • B01D53/22—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 diffusion
    • B01D53/225—Multiple stage diffusion
    • B01D53/226—Multiple stage diffusion in serial connexion
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/144—Purification; Separation; Use of additives using membranes, e.g. selective permeation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present invention relates to a technique for removing carbon dioxide from a mixed gas containing methane and carbon dioxide as main components, such as an anaerobic digester gas, and recovering methane.
  • a hydrocarbon-containing gas generated by anaerobic digestion and fermentation such as sewage sludge or human waste sludge as a raw material to generate power by a fuel cell.
  • an anaerobic digestive fermentation gas is a mixed gas containing methane and carbon dioxide as main components. If methane in the mixed gas can be easily separated, the methane is further decomposed.
  • Hydrogen gas can be obtained by using the hydrogen gas as fuel in a fuel cell.
  • Japanese Patent Application Laid-Open Nos. 61-53994 Reference 1
  • Japanese Patent Application Laid-Open No. 4-17713 Reference 2
  • Japanese Patent Publication No. 6-89349 Japanese Patent Laid-Open Publication No. H10-177,1992 discloses a method for removing methane from a mixed gas of methane and carbon dioxide using a gas separation membrane to enrich methane. That is, in the method of Reference 1, in order to recover methane from the landfill, the anaerobic deoxidizing enzyme is passed through a gas separation membrane through which carbon dioxide gas can easily pass.
  • a membrane separation device is used to recover methane from a mixed gas of methane and carbon dioxide generated from an anaerobic wastewater treatment device. Furthermore, in Reference 3, low-temperature steam reforming of hydrodesulfurized hydrocarbons was performed. A method for producing alternative natural gas for city gas containing methane as the main component by using a membrane to obtain methane-based gas from methane-carbon dioxide-containing reformed gas obtained by low-temperature steam reforming. A separation device is used.
  • the methods described in the above-mentioned documents have not yet examined the separation performance such as the throughput, methane concentration, and yield in a system using a gas separation membrane.
  • the membrane separation of the methane / carbon dioxide gas mixture is performed in one stage, and a sufficiently satisfactory high methane concentration is achieved due to the limitations imposed by the performance of the existing gas separation membrane. I could't do that.
  • the composition of the raw material gas supplied to the fuel cell unit is such that the concentration of carbon dioxide is 10% or less and the degree of methane is 90% or more.
  • the methane yield is expected to be 85%, preferably 90% or more.
  • the present invention has been conceived in view of such circumstances, and has been developed by using a simple system using a gas separation membrane to convert anaerobic digestive acid-enzyme gas containing methane and carbon dioxide gas as main components.
  • the task is to realize high concentration, high yield separation and recovery of methane.
  • Two-stage module and rear-stage module are arranged in series, and anaerobic digestive acid gas is supplied to the front module under pressure, and permeated gas from front module is depressurized and exhausted, and non-permeation from front module is performed.
  • the gas is supplied to the downstream module by residual pressure, the permeated gas of the downstream module is recycled to the upstream module, and the non-permeated gas of the downstream module is converted into a methane-enriched gas with a methane concentration of 90% or more.
  • a method for concentrating anaerobic digestive acid-fermented methane gas characterized in that the anaerobic digested acid gas is recovered at 5% or more.
  • the gas supply pressure to the front module is a 2 to 4 1 0 5 Pa, the pressure of the permeate gas of the preceding module to 0. 2 ⁇ 0. 9 x 1 0 s Pa. Ma
  • the pressure of the permeated gas in the subsequent module is set to atmospheric pressure.
  • the methane concentration of the anaerobic deoxidizing ifc ⁇ fermentation gas supplied to the pre-stage module is 50 to 70%
  • the methane concentration of the non-permeate gas of the pre-stage module is 75 to 8 Rises to 5%.
  • the methane concentration in the product gas recovered as the non-permeated gas of the latter module is as follows: The methane yield is more than 90% and the methane yield is more than 85%.
  • the methane yield is increased by recycling the permeated gas of the latter module to the former module, and the methane concentration is significantly increased by using two membrane modules in series. It enables high-concentration methane recovery with high yield.
  • it has been found that it is extremely important to properly balance the supply E power to the pre-stage module and the permeation pressure of the pre-stage module in order to perform high-yield and high-concentration methane recovery. That is, the gas supply pressure to the front module is less than 2 x 1 0 5 Pa, permeate side pressure is zero. If it is less than 2 x 1 0 5 Pa, 9 0% or more methane Umido, 8 5% It is difficult to obtain the above methane yield.
  • the area of the gas separation membrane of the subsequent module 2 it has been found that it is advantageous to make the area of the gas separation membrane of the subsequent module 2 to 4 times the area of the gas separation membrane of the previous module. If the membrane area of the latter module is smaller than twice the membrane area of the former module, the permeation of carbon dioxide will be insufficient and the expected methane concentration will not be obtained. If the membrane area of the downstream module is larger than 4 times the membrane area of the upstream module, the amount of permeation will increase and the amount of recycling will increase. As a result, the size of the equipment will increase, and it will not be economical.
  • the gas separation membrane incorporated in each module only needs to have characteristics that make it difficult for methane to permeate and permeate carbon dioxide gas.
  • membrane materials having such properties include ft® cellulose, polysulfone, boriamid, and boride. It can increase the limit etc.
  • a supply pipe provided with a combustor and supplied with an anaerobic enzyme ifcS enzyme gas
  • a pre-stage separation membrane module having an inlet connected to the supply pipe, An exhaust pipe connected to a permeated gas outlet of the pre-stage separation membrane module and having a decompression pump; a non-permeate gas pipe having one end connected to the non-permeate gas outlet of the pre-stage separation membrane module; A rear separation membrane module having an inlet connected to the other end of the pipe, and one end kneaded at a permeated gas outlet of the rear separation membrane module, and the other end of the supply pipe located upstream of the combessor. And a product gas pipe connected to a non-permeate gas outlet of the post-separation membrane module. Is done.
  • FIG. 1 is a schematic diagram showing one embodiment of a methane concentration and recovery apparatus according to one embodiment of the present invention.
  • BEST MODE FOR CARRYING OUT THE INVENTION is a schematic diagram showing one embodiment of a methane concentration and recovery apparatus according to one embodiment of the present invention.
  • FIG. 1 shows an embodiment of a configuration of a methane purulent collection apparatus according to one embodiment of the present invention.
  • This methane concentration and recovery apparatus 10 mainly includes two-stage gas separation membrane modules 11 and 12 arranged in series.
  • the interior of the pre-stage separation membrane module 1 1 is divided into a permeate side 1 lb and a non-permeate side 11 c by a separation membrane 1 la, and an anaerobic digestive acid gas is supplied to the inlet of the non-permeate side 11 c.
  • the supply gas pipe 13 in which the supplied compressor 14 is interposed is connected.
  • the outlet of the permeating side 11 b is connected to the exhaust pipe 15 through a decompression bomb 16 such as a vacuum bomb, while the outlet of the non-permeating side 11 c is connected to the non-permeating gas pipe 17. It is connected to one end.
  • the interior of the rear separation membrane module 12 is also divided into a permeate side 12 b and a non-permeate side 12 c by the separation membrane 12 a, and the above-described non-permeate is provided at the entrance of the non-permeate side 12 c.
  • Gas pipe 1 7 Is kneaded at the other end.
  • the outlet of the permeate side 12 b of the latter separation membrane module 12 is connected to one end of the recycle pipe 18.
  • the other end of the recycle pipe 18 is connected to the upstream side of the compressor 14 in the supply gas pipe 13 c.
  • the other end of the non-permeate side 12 c in the post-separation membrane module 12 is connected.
  • the outlet leads to the product gas pipe 19.
  • the gas supply pressure to the pre-stage separation membrane module 11 by the compressor 14 is preferably set to 2 to 4 ⁇ 10 5 Pa.
  • the area of the separation membrane 12 a in the rear module 12 is set to be larger than the area of the separation membrane 11 a in the front module 11.
  • the area of the separation membrane 12 a in the rear module 12 is set to be 2 to 4 times the area of the separation membrane 11 a in the front module 11.
  • the separation membranes 1 la and 12 a in each of the modules 11 and 12 can be, for example, a hollow hollow fiber membrane.
  • an anaerobic depleted itgf enzyme gas having a methane concentration of 60% is supplied from the supply gas pipe 13 for example.
  • the anaerobic digestion acid fermentation gas, combined with recycle gas to merge from the recycle pipe 1 8 is supplied Konburessa 1 4, for example, by 2-4 1 0 pressurized to 5 Pa in the preceding stage separation membrane module 1 1.
  • the transmission side 1 1 b in the front module 1 1 because it is pressed reduced to 0. 2 ⁇ 0. 9 xl 0 5 Pa by Metsu ⁇ bomb 1 6, carbon dioxide gas is efficiently removed , Exhausted.
  • the gas methane-enriched on the non-permeate side 11 c of the first separation membrane module 11 is supplied to the second separation membrane module 12 via the non-permeate gas pipe 17, and the gas is condensed on the non-permeate side 12 c Furthermore, methane is concentrated.
  • the permeate side 12 b of the latter separation membrane module 12 is preferably set to the atmospheric pressure, and 20 to 40% of the supply gas amount to the latter separation membrane module 12 is supplied to the supply gas pipe via the recycle pipe 18. Recycled to 13 That is, methane remaining in the permeated gas of the subsequent separation membrane module 12 is recycled for re-concentration without being exhausted as it is.
  • the pre-stage separation membrane module 1 1 The methane concentration at the outlet of the non-permeate side 11 c of this product is 75 to 85%, and the methane concentration of the product gas at the outlet of the non-permeate side 12 c of the post-stage separation membrane module 12 is 90% or more.
  • the methane yield is more than 85%.
  • the separation membranes 11a and 12a of the first module 11 (diameter 25 iraix length 2 14 mm) and the rear module 12 (diameter 25 mm x length 642 mm) are volume adjusted.
  • a hollow fiber membrane (made by Ube Industries, Ltd.) was used, and the membrane area ratio was set to 1: 3.
  • Permeate side 1 1 b of the front module 1 1 was decompressed to 0. 6 x 1 0 5 Pa by vacuum pump 1 6 was aspirated evacuated transparently gas.
  • the separation membranes 11a and 12a of the front module 11 (diameter 25mm x length 2 14mm) and the rear module 12 (diameter 25mm x length 428mm) are polyimid.
  • the membrane surface ratio was 1: 2.
  • Methane concentration of 60% was fed the carbon dioxide concentration of 40% of the gas mixture pressurized to supply pressure 4 X 1 0 5 Pa by Konburessa 1 4, at a feed rate 40 0 ⁇ ZHr.
  • the permeate side 11 b of the pre-stage module 11 was reduced to 0.9 ⁇ 10 5 Pa by the decompression pump 16, and the permeated gas was suctioned and exhausted.
  • a permeated gas corresponding to 23% of the supply gas amount to the subsequent module 12 was recycled to the supply gas pipe 13 at atmospheric pressure via the recycling pipe 18.
  • the methane concentration in the non-permeate gas of the former module 11 was 77%, and the methane concentration in the recycled gas was 50%.
  • Product gas as non-permeate gas for the latter module 1 and 2 The methane concentration in it was 90% and the methane yield was 86%.
  • the separation membranes 1 1 a, 1 a, and 2 in the front module 11 (diameter 25 mm x length 2 14 mm) and the rear module 12 (diameter 50 fields X length 2 14 ⁇ ) are used.
  • a hollow hollow fiber membrane was used as 12a, and the membrane area ratio was 1: 4.
  • a mixed gas having a methane concentration of 60% and a carbon dioxide gas concentration of 40% was supplied by pressurizing the supply pressure of 2 ⁇ 10 s Pa by the compressor 14.
  • the pressure on the permeate side 11 b of the pre-stage module 11 was reduced to 0.2 ⁇ 10 5 Pa by the vacuum pump 16, and the permeated gas was suctioned and exhausted.
  • a permeated gas equivalent to 38% of the gas supplied to the subsequent module 12 was recycled to the supply gas pipe 13 at atmospheric pressure via the recycle pipe 18.
  • the methane concentration in the non-permeate gas of the former module 11 was 82%, and the methane concentration in the recycled gas was 59%.
  • the methane concentration in the product gas as the non-permeate gas of the latter module 12 was 90%, and the methane yield was 89%.
  • the separation membranes 1 1a and 1 1 of the front module 11 (diameter 25 mm x length 2 14 om) and the rear module 12 (diameter 25 mm x length 6 42 om) were used.
  • 2a was a polyimide hollow fiber membrane, and the membrane area ratio was 1: 3.
  • Methane concentration 6 0% test the carbon dioxide concentration 4 0% mixed gas ⁇ force 1.
  • 2 X 1 0 5 pressurized to Pa was fed at a feed rate 4 0 0 Hr.
  • the pressure of 1 lb on the permeate side of the first-stage module 11 was reduced to 0.15 ⁇ 10 5 Pa by a decompression pump 16, and the permeated gas was suctioned and exhausted.
  • the separation membranes 1 1a, 1a, in the front module 11 (diameter 25 mm x length 21 mra) and the rear module 12 (diameter 25 x length 642) are used.
  • 12a was a polyimide hollow fiber membrane, and the membrane area ratio was 1: 3. Methane concentration 6 0 %, Carbon dioxide concentration of 4 0% of a mixed gas supply pressure 4.5 1 0 5 Pa pressurized and fed at a feed rate 4 0 0 Hr.
  • the permeated gas from the former module 11 was exhausted at atmospheric pressure.
  • a permeated gas equivalent to 50% of the supply gas amount to the rear module 12 was recycled to the supply gas pipe 13 via the recycle pipe 18 at atmospheric pressure.
  • the methane concentration in the product gas as a non-permeate gas of the latter module 12 was 90%, and the methane yield was 81%.
  • the decompression bomb 16 in FIG. 1 was not provided.
  • the two-stage gas separation membrane modules 11 and 12 are used, and the operating conditions of the apparatus are set within a predetermined range. Thus, a methane yield of 85% or more has been achieved.
  • Comparative Examples 1 and 2 are intended to show the effect of operating conditions (such as gas supply pressure) on the methane concentration and methane yield, and do not show a comparison with the prior art.
  • the apparatus used in Comparative Examples 1 and 2 is similar to Examples 1 to 3 in that two-stage gas separation modules 11 and 12 connected in series are used. This is different from the prior art in which only a gas separation membrane module is used.
  • the methane concentration in the non-permeated gas from the preceding module 11 corresponds to the methane concentration that can be achieved by the conventional technology employing the single-stage gas separation membrane module. Is done. According to this, it can be seen that, in any of the examples, the main gas concentration in the product gas can be increased by employing the two-stage gas separation membrane modules 11 and 12 in series.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Water Supply & Treatment (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

Cette invention concerne un procédé de concentration du méthane, lequel permet d'éliminer l'acide carbonique gazeux des gaz de fermentation digestive anaérobie, ainsi que de concentrer et de récupérer le méthane. Ce procédé fait appel à un appareil (10) qui comprend un module primaire (11) comportant une membrane (11a), ainsi qu'un module secondaire (12) comportant également une membrane (12a), les deux modules étant montés en série. D'après ce procédé, le gaz de fermentation digestive anaérobie est envoyé sous pression au module primaire (11) à l'aide d'un compresseur (14). Le gaz passant à travers le module primaire (11) est déchargé à l'aide d'une pompe à vide (16), tandis que le gaz restant dans ce même module (11) est ensuite envoyé à l'aide d'une pression résiduelle vers le module secondaire (12). Le gaz passant à travers le module secondaire (12) est renvoyé vers le module primaire (11) par une conduite de recyclage (18), tandis que le gaz restant dans le module (12) est récupéré sous forme de méthane concentré, la concentration étant d'au moins 90 % et le contenu en méthane d'au moins 85 %.
PCT/JP1996/003050 1995-11-01 1996-10-18 Procede et appareil de concentration du methane dans les gaz de fermentation digestive anaerobie WO1997016399A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU73345/96A AU7334596A (en) 1995-11-01 1996-10-18 Method and apparatus for concentrating methane in anaerobic digestive fermentation gas

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP7284918A JPH09124514A (ja) 1995-11-01 1995-11-01 嫌気性消化醗酵ガスのメタン濃縮方法および装置
JP7/284918 1995-11-01

Publications (1)

Publication Number Publication Date
WO1997016399A1 true WO1997016399A1 (fr) 1997-05-09

Family

ID=17684750

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP1996/003050 WO1997016399A1 (fr) 1995-11-01 1996-10-18 Procede et appareil de concentration du methane dans les gaz de fermentation digestive anaerobie

Country Status (3)

Country Link
JP (1) JPH09124514A (fr)
AU (1) AU7334596A (fr)
WO (1) WO1997016399A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20160304416A1 (en) * 2013-12-02 2016-10-20 Braskem S.A. Fermentation hydrocarbon gas products separation via membrane

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2007254572A (ja) * 2006-03-23 2007-10-04 Ngk Insulators Ltd メタン濃縮システム及びその運用方法
JP5124158B2 (ja) * 2007-04-13 2013-01-23 株式会社ノリタケカンパニーリミテド メタン濃縮装置およびメタン濃縮方法
JP2009242773A (ja) * 2008-03-14 2009-10-22 Air Water Inc メタンガス濃縮装置および方法ならびに燃料ガスの製造装置および方法
JP2013095726A (ja) * 2011-11-03 2013-05-20 Toho Gas Co Ltd バイオガスのメタン濃縮方法及びメタン濃縮装置
KR101529129B1 (ko) * 2014-09-18 2015-06-17 한국화학연구원 고순도 메탄가스의 분리를 위한 다단계 막분리 정제공정 및 장치
US10047310B2 (en) 2014-09-18 2018-08-14 Korea Research Institute Of Chemical Technology Multistage membrane separation and purification process and apparatus for separating high purity methane gas
KR101531605B1 (ko) * 2014-09-18 2015-06-26 한국화학연구원 고순도 메탄가스의 분리를 위한 저온, 저압의 운전조건을 가진 2 단 막분리 정제공정 및 장치
US11458435B2 (en) * 2018-06-18 2022-10-04 Japan Oil, Gas And Metals National Corporation Acidic gas separation device and acidic gas separation method

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS51147480A (en) * 1975-06-14 1976-12-17 Toshiba Corp A separating apparatus for mixed gas
JPS6153994A (ja) * 1984-08-24 1986-03-18 モンサント　コンパニ− ごみ埋立処理地からのメタンの回収方法
JPH0525482A (ja) * 1991-07-22 1993-02-02 Mitsubishi Kakoki Kaisha Ltd 代替天然ガスの製造方法

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS51147480A (en) * 1975-06-14 1976-12-17 Toshiba Corp A separating apparatus for mixed gas
JPS6153994A (ja) * 1984-08-24 1986-03-18 モンサント　コンパニ− ごみ埋立処理地からのメタンの回収方法
JPH0525482A (ja) * 1991-07-22 1993-02-02 Mitsubishi Kakoki Kaisha Ltd 代替天然ガスの製造方法

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20160304416A1 (en) * 2013-12-02 2016-10-20 Braskem S.A. Fermentation hydrocarbon gas products separation via membrane
US10427996B2 (en) * 2013-12-02 2019-10-01 Braskem S.A. Fermentation hydrocarbon gas products separation via membrane

Also Published As

Publication number Publication date
AU7334596A (en) 1997-05-22
JPH09124514A (ja) 1997-05-13

Similar Documents

Publication Publication Date Title
EP2366447B1 (fr) Procédé et appareil pour la production d'hydrogène et la récupération de dioxyde de carbone
US6500241B2 (en) Hydrogen and carbon dioxide coproduction
US9988326B2 (en) Method for the final purification of biogas for producing biomethane
US11370658B2 (en) Method for the preparation of ammonia synthesis gas
US6946016B2 (en) PSA sharing
EP0908219A1 (fr) Procédé à plusieurs étapes de séparation/récuperation de gaz
JPS63296820A (ja) 高純度水素又はヘリウムの製造方法
AU2001297607A1 (en) Improved hydrogen and carbon dioxide coproduction
CN110697655A (zh) 一种膜分离浓缩回收氢气的方法及系统装置
KR20090051168A (ko) 수소 정제 방법
US11535514B2 (en) System and method for recycling pressure swing absorber off-gas
WO1997016399A1 (fr) Procede et appareil de concentration du methane dans les gaz de fermentation digestive anaerobie
US20240226803A9 (en) Process and apparatus for separating a mixture of hydrogen and carbon dioxide
JP2007254572A (ja) メタン濃縮システム及びその運用方法
EP0792185A1 (fr) Azote d'une tres grande purete obtenu par separation par membrane
CN115417378B (zh) 从含氢气体中回收和提纯氢气的方法及系统
CN107381504B (zh) 一种合成气制备高纯度氢气装置及方法
JPH0733253B2 (ja) アンモニア及びメタノールの併産方法
CN115109625A (zh) 用于根据运输网络的特性获得生物甲烷的设备和方法
EP0243350A1 (fr) Recuperation amelioree d hydrogene dans les ecoulements de gaz de rejet
US20240075423A1 (en) A process for separating h2 from a gas mixture
CN117466248A (zh) 一种从混氢天然气中高回收率提取高纯度氢气的工艺
CN221593261U (zh) 一种用低温法回收天然气和氢气的装置
CN111943139B (zh) 煤经甲醇制烯烃装置甲醇驰放气的回收利用系统及方法
KR20160106419A (ko) 바이오가스 정제장치 및 이를 구비한 연료전지 시스템

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AU CA KR US

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES FI FR GB GR IE IT LU MC NL PT SE

121 Ep: the epo has been informed by wipo that ep was designated in this application
122 Ep: pct application non-entry in european phase
NENP Non-entry into the national phase

Ref country code: CA