[go: up one dir, main page]

WO2018149709A1 - Procédé d'élimination d'oxygène d'un gaz industriel - Google Patents

Procédé d'élimination d'oxygène d'un gaz industriel Download PDF

Info

Publication number
WO2018149709A1
WO2018149709A1 PCT/EP2018/053027 EP2018053027W WO2018149709A1 WO 2018149709 A1 WO2018149709 A1 WO 2018149709A1 EP 2018053027 W EP2018053027 W EP 2018053027W WO 2018149709 A1 WO2018149709 A1 WO 2018149709A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
oxygen
feed
heated
removal
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.)
Ceased
Application number
PCT/EP2018/053027
Other languages
English (en)
Inventor
Kresten Egeblad
Niklas Bengt Jakobsson
Rasmus TRANE-RESTRUP
Jacob Hjerrild Zeuthen
Troels Dahlgaard Stummann
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.)
Topsoe AS
Original Assignee
Haldor Topsoe AS
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 Haldor Topsoe AS filed Critical Haldor Topsoe AS
Publication of WO2018149709A1 publication Critical patent/WO2018149709A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8671—Removing components of defined structure not provided for in B01D53/8603 - B01D53/8668
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8603—Removing sulfur compounds
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/869—Multiple step processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/202—Hydrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/204—Carbon monoxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2067—Urea
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/208—Hydrocarbons
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/10—Single element gases other than halogens
    • B01D2257/104—Oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/202—Single element halogens
    • B01D2257/2025—Chlorine
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/304—Hydrogen sulfide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/306—Organic sulfur compounds, e.g. mercaptans
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/55—Compounds of silicon, phosphorus, germanium or arsenic
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/65—Employing advanced heat integration, e.g. Pinch technology
    • 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 novel method for the re ⁇ moval of oxygen from an industrial gas through selective catalytic oxidation via reactant injection.
  • the invention concerns an alternative route to reduce the oxygen content in industrial gases, where the reduction of the content of oxygen is crucial for the valorization of the gas.
  • the method of the invention is especially focused on siloxane/silanol removal and/or sul ⁇ fur conversion/removal taking place in the hot loop rather than before it.
  • the method of the invention is focusing on landfill gas, digester gas and industrial CO 2 off-gas.
  • oxygen re ⁇ moval is accomplished through PSA (pressure swing adsorp ⁇ tion) , membrane or scrubber technologies with very high capital expenditure (CAPEX) and also a substantial loss of valuable components, such as methane in the main gas to the oxygen-containing off-gas.
  • PSA pressure swing adsorp ⁇ tion
  • CAEX very high capital expenditure
  • the present invention comprises addition of components, such as 3 ⁇ 4, CO, methanol, ammonia or ethanol, to the main gas stream and leading the result ⁇ ant gas stream to at least one catalytic reactor.
  • the oxygen is converted selectively to CO 2 and water across the catalyst.
  • Removal of oxygen from fuel gas streams is often a require ⁇ ment for distribution of the gas in the natural gas grid, and it is also a requirement when utilizing the gas as a vehicle transportation fuel.
  • removal of oxygen is also critical for the utilization of other industrial gas streams, such as in producing merchant or industrial grade CO 2 from oxygen-containing off-gases.
  • US 3.361.531 describes the removal of oxygen from oxygen- containing environments and gas mixtures by absorption in a solid material contact mass. More specifically, a compound selected from copper carbonate, manganese carbonate and iron carbonate is contacted with a hydrogen-containing gas at an elevated temperature below about 500 °C, thereby re- ducing the carbonate to the corresponding oxide compound.
  • This oxide compound is brought into contact with said oxy ⁇ gen-containing environment at around ambient temperature, thereby absorbing the oxygen and oxidizing the oxide compound .
  • US 2013/0209338 Al discloses an integrated cleaning system to clean biogas from sources such as landfills and digest ⁇ ers for heat and power generation systems. Siloxanes, chlo ⁇ rine, oxygen and sulfur are removed to ppb levels, and the majority of water and some VOCs is removed as well.
  • the system cools a biogas stream to partially remove contami ⁇ nants, blends in a small concentration of hydrogen gas and then combusts the remaining oxygen to heat the biogas and leave sufficient hydrogen suitable for a downstream se- quence of further contaminant conversion and removal in stages using a hydrodesulfurization bed and adsorbent media beds.
  • the approach according to the present invention is different in that methanol or other reducing agents can be used, and the impurities are kept in oxidized form to be removable from the stream by using a scrubber.
  • the technologies dominating the industry today are PSA and membrane based technologies in small and medium sized pro ⁇ jects (typically up to 10,000 Nm 3 /h gas), whereas distilla- tion and cryogenic separation are dominating in larger scale applications.
  • one or more components suitable for catalytic oxidation are in- jected into the oxygen-containing main gas stream after removal of sulfur-containing compounds and siloxanes from the gas.
  • the components and the catalyst are chosen so that the catalyst oxidizes the injected components using the oxygen in the stream without substantially oxidizing the valuable components, such as methane, in the gas stream.
  • the components to be injected may comprise one or more of i.a. 3 ⁇ 4, CO, ammonia, urea, ethanol and dimethyl ether (DME) .
  • the active catalyst may comprise a metal selected among va ⁇ nadium, tungsten, chromium, copper, manganese, molybdenum, platinum, palladium, rhodium and ruthenium in metallic or metal oxide form supported on a carrier selected from alu ⁇ mina, titania, silica and ceria and combinations thereof.
  • Sulfur impurities in an industrial gas can create a corro ⁇ sive environment inside power generating equipment or even poison catalysts that may be present.
  • hydrogen sulfide present in the feed gas to gas engines will cause degradation of the lubricating oil and lead to a need of frequent maintenance.
  • 3 ⁇ 4S needs to be removed if the gas is to be sent to gas pipelines or used as fuel in vehicles.
  • Siloxanes are organosilicon compounds comprising silicon, carbon, hydrogen and oxygen which have Si-O-Si bonds.
  • Si ⁇ loxanes can be linear as well as cyclic. They may be pre ⁇ sent in digester or landfill gas because they are used in various beauty products, such as e.g. cosmetics and sham ⁇ poos that are washed down drains or otherwise disposed of, so that they end up in municipal wastewater and landfills. Siloxanes are not broken down during anaerobic digestion, and as a result, waste gas captured from treatment plants and landfills is often heavily contaminated with these com ⁇ pounds.
  • siloxanes can be removed using non-regenerative packed bed adsorption with activated car ⁇ bon or porous silica as sorbent.
  • Regenerative sorbents can also be used as well as units based on gas cooling to very low temperatures to precipitate the siloxanes out from the gas.
  • liquid extraction technologies are used. In addition, these technologies can be used in combination.
  • a silanol is a functional group in silicon chemistry with the connectivity Si-O-H. It is related to the hydroxy func ⁇ tional group C-O-H found in all alcohols.
  • siloxanes give rise to problems because they are converted to S1O 2 during combustion, leading to build-up of abrasive solid deposits inside the engine and causing damage, re ⁇ claimed service time and increased maintenance requirements for many components such as compressors, fans, blowers, burner nozzles, heat recovery surfaces in boilers and for gas engine components such as spark plugs, valves, pistons etc.
  • any catalysts installed to control ex- haust gas emissions are sensitive to S1O 2 entrained in the gas stream, in fact even more so than the engine itself.
  • the S1O 2 tolerance can be as low as 250 ppb .
  • the present invention relates to a method for the re ⁇ moval of oxygen from an industrial gas feed, said process comprising the steps of:
  • the gas feed, from which oxygen is to be re ⁇ moved is a landfill gas, a digester gas or an industrial CO2 off-gas.
  • a gas stream such as a landfill gas containing 3 ⁇ 4S and organic sulfur along with siloxanes, CO 2 , 3 ⁇ 40, methane and various VOCs (volatile organic carbon compounds) , is treated .
  • the components to be injected in step (d) comprise one or more of 3 ⁇ 4, CO, ammonia, urea, methanol, ethanol and dime ⁇ thyl ether (DME) .
  • Landfill gas of low quality i.e. having a high content of nitrogen and oxygen, is more difficult and expensive to up ⁇ grade to pipeline quality than gases with a lower content of nitrogen and oxygen.
  • Using the reactant injection to remove the oxygen from low quality landfill gases will lead to a high temperature increase in the reactor, which in turn will damage the catalyst. If, however, the reactant is dosed at two different points instead of one point, it is possible to use two reactors in series with cooling and re ⁇ actant injection in between.
  • This approach has the added benefit that the energy recovered after each reactor can be used in a reboiler in the CO 2 separation unit (amine wash) to regenerate the amine, and it can also be used as a feed preheater.
  • the energy for the reboiler and for preheating of the feed would otherwise have to come from electricity or from combustion of landfill gas or natural gas.
  • the heat coming from the oxidation can be transferred to an oil or steam circuit which is used both to run a reboiler in the amine wash in the subsequent CO2 removal and to pre ⁇ heat the feed.
  • the invention is illustrated further with reference to the figure, where the present invention is combined with Appli ⁇ cant's GECCOTM technology for digester and landfill gas conditioning.
  • the feed gas is heated to 200-450°C and fed to a siloxane or silanol absorption bed comprising alumina, alumina with nickel, silica or combinations thereof.
  • the gas is fed to a catalytic reactor containing a catalyst selected from tungsten, vanadium, molybdenum, platinum and palladium in metallic or metal oxide form supported on a T 1 O2 carrier.
  • the catalyst converts the sulfur compounds to S O2 and the VOC compounds (not methane and light [i.e. C3 and lower] hydrocarbons) to CO2 and water and also hydrogen halides if some of the VOCs are halogenated.
  • One or more components suitable for catalytic oxidation i.e. 3 ⁇ 4, CO, ammonia, urea, methanol, ethanol, DME etc., is/are injected into the main gas stream containing oxygen, and the gas stream is fed to the catalytic reactor contain- ing a catalyst such as vanadium, tungsten, chromium, copper, manganese, molybdenum, platinum, palladium, rhodium or ruthenium in metallic or metal oxide form supported on a carrier selected from alumina, titania, silica and ceria or combinations thereof.
  • a catalyst such as vanadium, tungsten, chromium, copper, manganese, molybdenum, platinum, palladium, rhodium or ruthenium in metallic or metal oxide form supported on a carrier selected from alumina, titania, silica and ceria or combinations thereof.
  • the injected compo- nent(s) is/are selectively oxidized to 3 ⁇ 40 and CO2 , while the valuable hydrocarbons, such as methane and light [i.e. C3 and lower] hydrocarbons, are substantially not con ⁇ verted.
  • the catalyst comprises tung ⁇ sten, vanadium, molybdenum, platinum or palladium in metallic or metal oxide form supported on a T 1 O2 carrier.
  • the hot reactor exit gas can be utilized to heat the reac ⁇ tor inlet gas by using a feed-effluent heat exchanger.
  • the additional heat generated in the oxygen removal step will provide a higher temperature difference for the feed- effluent heat exchanger, which reduces the CAPEX.
  • the S O2 Downstream from the heat exchanger, the S O2 is removed in a wet caustic or H2O2 scrubber or a dry scrubber using a caustic sorbent.
  • CO2 is removed by using amine-based technology, solvent-based CO2 removal technology, water-based CO2 removal technology or alterna ⁇ tively PSA and/or membrane technology.
  • Nitrogen removal can be accomplished using membrane or PSA based technology. Then water is removed by using cooling and condensation followed by a molecular sieve, alterna ⁇ tively in a TSA configuration.
  • the nitrogen removal unit is positioned downstream from the water re- moval unit.
  • the catalyst used for sulfur and/or oxygen removal is monolithic to decrease the power consumption for transport of the landfill gas through the cleaning section.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Catalysts (AREA)

Abstract

L'invention concerne l'élimination d'oxygène d'une alimentation gazeuse telle qu'un gaz d'enfouissement, un gaz de digestion ou un gaz de dégagement de CO2 industriel, consistant à éliminer les composés contenant du soufre et les siloxanes du gaz d'alimentation, à chauffer le gaz d'alimentation, à éliminer éventuellement les siloxanes et les silanols du gaz d'alimentation chauffé, à éliminer éventuellement une partie des composés contenant du soufre dans le gaz d'alimentation chauffé, à convertir éventuellement l'un quelconque ou tous les composés organiques volatils (COV) présents dans le gaz, y compris des composés contenant du soufre et/ou des composés contenant du chlore, dans le gaz d'alimentation chauffé, à injecter un ou plusieurs réactifs pour la conversion d'oxygène dans le gaz d'alimentation chauffé, à effectuer une conversion catalytique sélective de l'oxygène dans au moins un réacteur approprié, et à nettoyer le gaz appauvri en oxygène résultant. Les réactifs à injecter peuvent comprendre du H2, et/ou du CO, et/ou de l'ammoniac, et/ou de l'urée, et/ou du méthanol, et/ou de l'éthanol et/ou du diméthyléther (DME).
PCT/EP2018/053027 2017-02-16 2018-02-07 Procédé d'élimination d'oxygène d'un gaz industriel Ceased WO2018149709A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DKPA201700112 2017-02-16
DKPA201700112 2017-02-16

Publications (1)

Publication Number Publication Date
WO2018149709A1 true WO2018149709A1 (fr) 2018-08-23

Family

ID=61188811

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2018/053027 Ceased WO2018149709A1 (fr) 2017-02-16 2018-02-07 Procédé d'élimination d'oxygène d'un gaz industriel

Country Status (1)

Country Link
WO (1) WO2018149709A1 (fr)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2466554A (en) * 2008-12-24 2010-06-30 Johnson Matthey Plc Process for the manufacture of town gas from landfill gas
JP2011153245A (ja) * 2010-01-28 2011-08-11 Sumitomo Seika Chem Co Ltd メタンを主成分とするガスの処理方法および処理装置
WO2012006729A1 (fr) * 2010-07-15 2012-01-19 Quadrogen Power Systems, Inc. Système de purification de biogaz intégré pour enlever l'eau, les siloxanes, le soufre, l'oxygène, les chlorures et les composés organiques volatils

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2466554A (en) * 2008-12-24 2010-06-30 Johnson Matthey Plc Process for the manufacture of town gas from landfill gas
JP2011153245A (ja) * 2010-01-28 2011-08-11 Sumitomo Seika Chem Co Ltd メタンを主成分とするガスの処理方法および処理装置
WO2012006729A1 (fr) * 2010-07-15 2012-01-19 Quadrogen Power Systems, Inc. Système de purification de biogaz intégré pour enlever l'eau, les siloxanes, le soufre, l'oxygène, les chlorures et les composés organiques volatils

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
URBAN W ET AL: "Catalytically upgraded landfill gas as a cost-effective alternative for fuel cells", JOURNAL OF POWER SOURCES, ELSEVIER SA, CH, vol. 193, no. 1, 24 December 2008 (2008-12-24), pages 359 - 366, XP026150425, ISSN: 0378-7753, [retrieved on 20090603], DOI: 10.1016/J.JPOWSOUR.2008.12.029 *

Similar Documents

Publication Publication Date Title
US10675585B2 (en) Method for the removal of oxygen from an industrial gas
JP5684785B2 (ja) オフガス流れを処理する方法およびそのための装置
MX2009001742A (es) Proceso integrado de separacion y purificacion.
CN110621389A (zh) 通过二氧化硫选择性膜技术以及二氧化硫选择性吸收技术优化克劳斯尾气处理
EP2416872B1 (fr) Procédé de traitement d'un courant de gaz acide et appareil pour la mise en uvre de ce procédé
CN110603087A (zh) 利用二氧化硫选择性膜技术增强克劳斯尾气处理
KR20230171436A (ko) 재생 가능한 에너지를 사용하여 이산화탄소를 정제하고 변환하는 공정
US10933372B2 (en) Method for the removal of oxygen from an industrial gas feed
CN101193690A (zh) 燃料气体的处理
CN113663493A (zh) 改善从克劳斯法尾气中回收硫的系统和方法
JP4837176B2 (ja) 天然ガスからの硫黄化合物の除去方法
WO2017140662A1 (fr) Procédé et système de traitement de gaz pour l'élimination combinée de siloxanes et de composés contenant du soufre à partir de flux de biogaz
CN109789365A (zh) 从垃圾填埋气体中除去硅氧烷的方法
CA2568303C (fr) Methode de recuperation de composes du soufre presents dans les courants gazeux
CN107321178B (zh) 气体纯化设备和气体纯化方法
EP3481534B1 (fr) Procédé d'élimination combinée de siloxanes et de composés contenant du soufre du flux de biogaz
WO2018149709A1 (fr) Procédé d'élimination d'oxygène d'un gaz industriel
EP3463628B1 (fr) Procédé de purification d'un écoulement de gaz brut contenant principalement des hydrocarbures en c1-c5 et du dioxyde de carbone, et des impuretés constituées de composés sulfurés organiques et inorganiques, de composés organiques volatils halogénés et non halogénés et d'oxygène
WO2020173828A1 (fr) Procédé d'élimination combinée de siloxanes, de soufre et de cov
CA2830498C (fr) Procede et systeme pour eliminer le soufre de flux gazeux soufres
RU2827330C2 (ru) Способ обработки серосодержащих отходов перерабатывающих и обогатительных производств
Vatachi et al. Modified Claus Process Applied To Natural Gas For Sulfur Recovery

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 18703986

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 18703986

Country of ref document: EP

Kind code of ref document: A1