WO2018202406A1 - Procédé et dispositif de désulfuration d'un flux de gaz contenant de l'hydrogène sulfuré - Google Patents

Procédé et dispositif de désulfuration d'un flux de gaz contenant de l'hydrogène sulfuré Download PDF

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Publication number
WO2018202406A1
WO2018202406A1 PCT/EP2018/059616 EP2018059616W WO2018202406A1 WO 2018202406 A1 WO2018202406 A1 WO 2018202406A1 EP 2018059616 W EP2018059616 W EP 2018059616W WO 2018202406 A1 WO2018202406 A1 WO 2018202406A1
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WO
WIPO (PCT)
Prior art keywords
gas turbine
catalyst
washing medium
regeneration
regeneration stage
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/EP2018/059616
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German (de)
English (en)
Inventor
Ralph Joh
Jenny Larfeldt
Gerhard Zimmermann
Rüdiger Schneider
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.)
Siemens AG
Siemens Corp
Original Assignee
Siemens AG
Siemens Corp
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 Siemens AG, Siemens Corp filed Critical Siemens AG
Publication of WO2018202406A1 publication Critical patent/WO2018202406A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • 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
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/103—Sulfur containing contaminants
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2270/00—Specifically adapted fuels
    • C10L2270/04—Specifically adapted fuels for turbines, planes, power generation
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/12—Regeneration of a solvent, catalyst, adsorbent or any other component used to treat or prepare a fuel
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/541—Absorption of impurities during preparation or upgrading of a fuel
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/544—Extraction for separating fractions, components or impurities during preparation or upgrading of a fuel
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/56—Specific details of the apparatus for preparation or upgrading of a fuel
    • C10L2290/562—Modular or modular elements containing apparatus

Definitions

  • the invention relates to a process for the desulfurization of a gas stream containing hydrogen sulfide, in particular a gas stream usable for combustion in a gas turbine. Furthermore, the invention relates to a device for the defluxation of a gas stream containing hydrogen sulfide.
  • Natural gas is a fossil fuel with comparatively low carbon dioxide (C0 2 ) emissions and comparatively low emissions of other waste products from incineration. Its contribution as one of the most important energy resources of the world continues to increase. In view of the shortage of raw materials, the permanently rising energy demand and rising prices of high-quality fossil fuels, the exploitation of non-specified fuels is becoming increasingly important. For example, there is a growing interest in emitting acid gases directly as well.
  • H2S hydrogen sulphide
  • This liquid redox process is based on the concept of reactive absorption, ie a combination of absorption and oxidation.
  • a washing medium To separate the hydrogen sulphide from the respective gas, it is brought into contact with a washing medium and the hydrogen sulphide contained in the gas is bound chemically or physically to an active substance of the washing medium.
  • the fuel gas purified by hydrogen sulfide can then be combusted directly in a gas turbine.
  • Washing medium is then carried out by a catalyst (also known as catalytically active components or redox agent), which converts Schweielwasserstoff contained in the washing medium into elemental sulfur and thus removes the hydrogen sulfide from the washing medium.
  • a catalyst also known as catalytically active components or redox agent
  • the catalyst itself is reduced in the oxidation of hydrogen sulfide (H 2 S conversion).
  • H 2 S conversion oxidation of hydrogen sulfide
  • the washing medium containing the reduced catalyst to be regenerated in a separation of hydrogen sulfide downstream process step in an appropriate regeneration stage for example, a bubble column as a contact apparatus
  • an oxygen-containing gas usually ambient air
  • the limiting step is the absorption rate of oxygen in the wax medium, which is due to the low solubility of oxygen in the wash medium.
  • Washing medium is increased. With a reduction of
  • Umpumpmenge can be used correspondingly smaller and structurally cheaper apparatus, which reduces the investment and operating costs.
  • the regeneration of the washing medium in the context of the separation of hydrogen sulfide from acidic gases usually with oxygen-containing air at pressures not far above atmospheric pressure.
  • a so-called flash stage in which the washing medium is released before the regeneration and dissolved methane can escape.
  • the resulting gas stream is again compressed and fed to the (sweet) gas purified by hydrogen sulphide.
  • the flash container used for the expansion of the washing medium must be designed comparatively large volume for satisfactory degassing in order to ensure a sufficiently long residence time of the washing medium.
  • This also increases the necessary footprint of the system and makes, for example, an off-shore application of liquid redox method, which offers itself in principle due to the comparatively simple and compact design, again unattractive.
  • Foaming tendency of the washing medium must also be designed very large volume.
  • the invention is therefore based on the object of specifying a possibility which provides an efficient and cost-effective preparation of hydrogen sulfide-containing gas streams allowed.
  • a gas stream containing hydrogen sulphide for the removal of a gas stream containing hydrogen sulphide, it is contacted with a washing medium containing a catalyst for absorbing the hydrogen sulphide and forming elemental sulfur, the catalyst being reduced in the formation of the elemental sulfur, and with the reduced catalyst containing wash medium is fed to a regeneration stage, in which the reduced catalyst is regenerated.
  • the regeneration of the catalyst within the regeneration stage is carried out according to the invention by means of separated from an air stream of a gas turbine, pure oxygen.
  • pure oxygen is purposely obtained from the air flow of a turbine, which is then used in the regeneration stage for the regeneration of the catalyst and thus for the regeneration of the washing medium.
  • pure oxygen instead of compressed air has clear advantages over conventional liquid redox processes. Due to the high partial pressure when using pure oxygen, the mass transport into the washing medium and thus the speed of regeneration are increased. As a result, smaller Christsverweil Stamm initiatives and lower Umpumpmengen the wash medium can be realized. The latter, in turn, leads to structurally smaller device components, such as contact devices, separators and pumps, whereby investment and operating costs can be saved. Reduction of the equipment is also an important precondition.
  • Catalyst and the precipitated elemental sulfur is then contacted starting from the absorber of the regeneration stage and there with pure oxygen.
  • Pure oxygen in the context of the present invention is understood in particular to mean oxygen having a purity in a range between 90% and 99%.
  • Air separation module used.
  • an air flow of the gas turbine is fed to such a Luftzerlegungsmodul, in which pure oxygen is separated from the air flow.
  • the air flow in particular a partial flow of the compressed combustion air of the gas turbine, is preferably taken from a suitable compressor stage (compressor stage) of the gas turbine at a high pressure level adapted to the process control.
  • the air separation module used is a high-temperature air separation module with a membrane which, in the environment of a gas turbine, provides a comparatively cost-effective possibility for the production of oxygen.
  • the gas turbine hot compressed air is removed and passed into the high-temperature Heilzerlegungsmodul.
  • the membrane removes oxygen from the air ström separated, it results - in addition to the oxygen flow - an oxygen-depleted exhaust air flow.
  • the recovered oxygen is then preferably fed to the regeneration stage and used there for the regeneration of the washing medium and the catalyst contained therein.
  • the gas turbine produces the hot air stream necessary for the air separation. Additional investments for compression and / or air heating are not necessary.
  • the amount of pure oxygen fed to the regeneration stage is preferably metered such that the stoichiometric ratio of the amount of oxygen fed to the amount of hydrogen sulfide to be separated off is> 1.
  • the dosage of pure oxygen is done with a small excess, so as to achieve the necessary equilibrium.
  • the gas flow needed for the regeneration ie the pure oxygen supplied to the regeneration stage, can be reduced by up to 98% compared to a "classic" air flow.
  • the required lines and compressors could be designed much smaller and more cost-effectively.
  • Liquid separators which are used after the regeneration to separate the regenerated washing medium and the remaining exhaust air, can be structurally made significantly smaller or may even be dispensed with.
  • the separated within the air separation module from the air flow pure oxygen is suitably fed to the regeneration stage.
  • the pure oxygen is cooled before entering the regeneration stage.
  • the released during the cooling of the oxygen heat can be fed in particular at a suitable point in the process and use there.
  • the air stream depleted of oxygen or depleted of oxygen when the pure oxygen is separated off is fed to the gas turbine.
  • the airflow has a high pressure level as it leaves the air separation module, allowing it to be fed to the gas turbine without loss of volume work.
  • the supply takes place directly into the combustion chamber of the gas turbine.
  • the supply to the cooling system of the turbine blades of the gas turbine is fed to the gas turbine.
  • the separation of elemental sulfur from this is necessary. Accordingly, at least a partial stream of the washing medium containing the sulfur and the reduced catalyst is expediently removed before it is fed to the regeneration stage.
  • the partial flow is preferably withdrawn from the absorber leaving the flow of the washing medium and the sulfur contained in the partial flow separated from this.
  • the separation is expedient to remove so much sulfur that a steady state value of about 5% by weight is established in the sweat fraction in the washing medium.
  • the separation is preferably carried out by means of customary separation units, for example by means of a cyclone or by means of appropriately designed filtration units.
  • the sulfur itself is expediently sent for further utilization.
  • the cleaned of sulfur partial stream of the washing medium is preferably fed to a plant part in which the operating pressure is possible low, so as to reduce the necessary pump power and thus to keep the operating costs low.
  • the regenerated wash medium is then conveniently fed to an absorber in which it is used to re-absorb hydrogen sulfide from a gas stream and to oxidize the absorbed hydrogen sulfide to elemental sulfur.
  • an amino acid salt solution is preferably used as the washing medium.
  • An aqueous amino acid salt solution is useful here.
  • the use of mixtures of different amino acid salts as a washing medium is also possible.
  • Metal salts are particularly suitable as catalyst.
  • all such metal salts are conceivable here, the metal ions of which may be present in a plurality of oxidation states.
  • the salts of the metals iron, manganese or copper are used.
  • These metal salts are inexpensive to acquire and have the desired catalytic properties.
  • metal chelate complexes are advantageous which have a sufficiently high solubility in the aqueous formulation.
  • the wash medium is suitably a complexing agent such as EDTA (ethylenediaminetetra acetate), HEDTA (hydroxyethyl-ethylenediaminetetraacetate), DTPA (Diethylentriaminpentaacetat) and / or NTA (nitrile triacetate) was added.
  • EDTA ethylenediaminetetra acetate
  • HEDTA hydroxyethyl-ethylenediaminetetraacetate
  • DTPA Diethylentriaminpentaacetat
  • NTA nitrile triacetate
  • the device according to the invention for the desulfurization of a gas stream containing hydrogen sulfide, in particular a fuel gas stream which can be used for combustion in a gas turbine comprises an absorber for absorbing hydrogen sulfide from the gas stream to form elemental
  • the regeneration stage is designed to regenerate the catalyst by means of pure oxygen separated from an air stream of a gas turbine.
  • Hydrogen sulfide removed by absorption in the washing medium from a gas stream is an amino acid salt solution.
  • the absorbed hydrogen sulfide reacts within the absorber by means of a catalyst contained in the washing medium to elemental sulfur and is thereby reduced itself.
  • the catalyst used is preferably a metal salt which is used in the
  • Washing medium is included. Particularly preferred is the use of metal-chelate complexes as a catalyst.
  • the washing medium is supplied to the regeneration stage downstream of the absorber in the direction of flow of the washing medium.
  • the absorber expediently comprises a discharge line, which is fluidically coupled to a supply line of the regeneration stage.
  • the regeneration stage itself is expediently coupled fluidically with a gas turbine.
  • the regeneration stage is connected in an expedient embodiment, a supply line connected to a discharge line of the gas turbine is fluidically coupled.
  • the discharge line of the gas turbine is particularly preferred one
  • Compressor stage of the gas turbine connected. About the fluidic coupling of the discharge line of the gas turbine and the supply line of the regeneration stage of the regeneration stage is fed pure oxygen.
  • an air separation module is interposed fluidically.
  • the air separation module is thus downstream in terms of flow in the direction of flow of an air stream taken from the gas turbine.
  • the air separation module is supplied with compressed air from the gas turbine.
  • a discharge line of the gas turbine and, in particular, a discharge line connected to a compressor stage of the gas turbine are expediently coupled to a supply line of the air separation module.
  • the air separation module of the regeneration stage is upstream in terms of flow in the flow direction of the air flow taken from the gas turbine.
  • a discharge line of the air separation module is expediently coupled fluidically to a supply line of the regeneration stage.
  • the air separation module in particular a high-temperature air separation module with a membrane designed to separate oxygen
  • oxygen is separated off from an air partial stream taken from the gas turbine.
  • This oxygen is fed to the regeneration stage and used there for the regeneration of the washing medium and the catalyst.
  • the stoichiometric ratio of the amount of pure oxygen fed to the regeneration stage to the amount of hydrogen sulfide to be separated off is preferably at a value 1. 1. This results in a reduction in the rate of regeneration. required gas flow up to 98% possible.
  • the equipment used and lines can be made significantly smaller compared to previous devices.
  • the regeneration stage is preferably fluidically coupled to the gas turbine.
  • the exhaust air stream leaving the regeneration stage after regeneration of the washing medium and depleted of oxygen can thus be supplied to the gas turbine.
  • the supply preferably takes place at a high pressure level. This ensures that the volume work from the compression is not lost.
  • the regeneration stage is fluidically coupled to the combustion chamber of the gas turbine.
  • the supply of the oxygen-depleted exhaust air flow then takes place to the combustion chamber of the gas turbine.
  • Through a supply to the combustion chamber in particular secondary components formed in the process are burned, thus avoiding additional emissions.
  • the exhaust air flow can be fed in the context of the invention in a relaxation stage of the gas turbine.
  • the regeneration stage is expediently coupled fluidically with the expansion stage of the gas turbine.
  • the exhaust air can be used in the invention in particular for cooling the turbine blades of the gas turbine.
  • the air separation module is capable of removing the flow of air which is depleted of oxygen during the separation of the pure oxygen from oxygen.
  • a discharge line of the air separation module is expediently coupled to a supply line of the gas turbine.
  • the air separation module is fluidically coupled to the combustion chamber of the gas turbine.
  • the air separation module is coupled to the cooling system of the turbine blades of the gas turbine.
  • a removal line for removing a partial flow of the washing medium is preferably included.
  • the extraction line can in principle be connected to different positions of the device.
  • the separation of sulfur takes place before the entry of the washing medium in the regeneration stage.
  • Suction line is suitably connected to the discharge line of the absorber. In this way, a part of the precipitated in the oxidation of the hydrogen sulfide elemental sulfur can be separated from the washing medium.
  • the preferred concentration of solid sulfur remaining in the wash medium after separation is about 5%.
  • the separation of the sulfur from the washing medium is preferably carried out in a flow-connected in the flow direction of the withdrawn partial flow of the extraction line separation unit.
  • a separation unit common devices such as cyclones or filtration devices are suitable.
  • FIG. 1 shows a device 1 for the desulfurization of a gas stream 3 and in particular for the desulfurization of a fuel gas stream for a gas turbine.
  • the gas stream 3 is fed via a feed line 5 to an absorber 7 and contacted within the absorber 7 with a washing medium 9.
  • a washing medium 9 As the washing medium 9, an aqueous amino acid salt solution containing a catalyst 11 is used.
  • Hydrogen sulfide 13 contained in the gas stream 3 is absorbed in the washing medium 9 and oxidized to elemental sulfur 15 by means of the catalyst 11, in this case complexed Fe (III) ions.
  • the catalyst 11 is reduced in the oxidation of the hydrogen sulfide 13 to Fe (II) ions.
  • the sulfur 15 forms as a solid phase (particles), the Fe (II) ions formed by the reduction remain in solution and are masked by EDTA as the complexing agent added to the washing medium 9.
  • the purified from hydrogen sulfide 13 (sweet) gas 17 is removed from the absorber 7 via a discharge line 19 and fed to a gas turbine 21.
  • the discharge line 19 is fluidically coupled to a supply line 23 of the gas turbine 21.
  • the washing medium 25 which contains the now reduced catalyst 27 and the elemental sulfur 15
  • a the absorber 7 fluidly downstream regeneration stage 29 is supplied to the head 31.
  • a discharge line 33 of the absorber 7 is fluidically coupled to a supply line 35 of the regeneration stage 29.
  • a partial flow 37 of the washing medium 25 is removed via a withdrawal line 39 connected to the discharge line 33 of the absorber.
  • the withdrawn from the washing medium 25 partial flow 37 is a filter as unit formed separation unit 41, in which the sulfur 15 is separated from the washing medium 25.
  • Sulfur 15 itself is sent for further use.
  • the cleaned of sulfur 15 washing medium 25 is in the
  • a return line 43 of the separation unit 41 is also fluidically coupled to the discharge line 33 of the absorber 7.
  • the scrubbing medium 25 freed of sulfur 15 is combined with the main flow 45 of the scrubbing medium 25.
  • the washing medium 25 is then fed to the regeneration stage 29 and contacted here with pure oxygen 47.
  • the pure oxygen 47 is provided by means of an air separation module 53.
  • a hot, compressed, oxygen-containing air stream 57 is taken from a compressor stage 55, that is to say a compressor stage of the gas turbine 21, and passed into the air separation module 53 downstream of the gas turbine 21 in the flow direction of the air stream 57.
  • the gas turbine 21 is coupled via a connected discharge line 59 to a supply line 61 of the air separation module 53.
  • the oxygen 47 is separated from the airflow 57 taken from the gas turbine 21 by means of a membrane 63.
  • the depleted of oxygen 47 air flow 65 is again fed to the gas turbine 21, wherein the supply to a compressor stage 55 in the flow direction of the combustion air downstream turbine stage 67, in this case the combustion chamber 69 is carried out.
  • the oxygen 47 separated within the air separation module 53 is fed to the regeneration stage 29 downstream of the air separation module 53.
  • the regeneration stage 29 is connected to the bottom 71 of a supply line 73, which is fluidically coupled to a discharge line 75 of the air separation module 53.
  • the air separation module 53 is therefore switched fluidly between the gas turbine 21 and the regeneration stage 29.
  • a heat exchanger 77 is arranged, which cools the oxygen 47 before entering the regeneration stage 29.
  • the resulting heat can be fed into the process at a suitable point. Further, the cooled oxygen 47 is compressed.
  • the reduced catalyst 27 contained in the washing medium 25 is oxidized by means of the oxygen 47 (oxidation of the previously reduced Fe (II) ions to Fe (III) ions) and thus the unconsumed catalyst 11 is recovered with simultaneous regeneration of the washing medium 9 ,
  • the regenerated in the regeneration stage 29 washing medium 9 is then used to re-separation of hydrogen sulfide 13 from a gas stream 3.
  • the regenerated washing medium 9 is withdrawn via a discharge line 79 connected to the bottom 71 of the regeneration stage 29 and supplied via a fluidic coupling of the discharge line 79 with a supply line 81 of the absorber 7.
  • the exhaust air stream 83 can then be used further. There are various options that can be selected depending on the process management and the composition of the exhaust air stream 83. It is particularly advantageous if the
  • Exhaust air stream 83 of the gas turbine 21 and in particular the combustion chamber 69 of the gas turbine 21 is supplied.
  • a discharge of the exhaust air 83 in a relaxation stage of the gas turbine 21 is possible. If a return of the exhaust air flow in the process is not desired or due to a high methane content in the exhaust air 83 and an associated increased risk of explosion not lent be borrowed, the exhaust air can be removed via the discharge line 85 also from the process.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

L'invention concerne un procédé de désulfuration d'un flux de gaz (3) contenant de l'hydrogène sulfuré (13), en particulier d'un flux de gaz combustible pouvant s'utiliser pour la combustion dans une turbine à gaz (21), le flux de gaz (3) étant mis en contact, pour assurer l'absorption de l'hydrogène sulfuré et par formation de soufre élémentaire (15), avec un milieu de lavage (9) contenant un catalyseur (11), ledit catalyseur (11) étant réduit lors de la formation du soufre élémentaire (15), le milieu de lavage (25) et le catalyseur réduit (27) qu'il contient étant acheminés jusqu'à un étage de régénération (29) dans lequel le catalyseur réduit (27) est régénéré, et la régénération du catalyseur (27) intervenant à l'intérieur de l'étage de régénération (29) au moyen d'oxygène pur (47) séparé d'un flux d'air (57) d'une turbine à gaz (21). L'invention concerne en outre un dispositif (1) de désulfuration d'un flux de gaz (3) contenant de l'hydrogène sulfuré.
PCT/EP2018/059616 2017-05-02 2018-04-16 Procédé et dispositif de désulfuration d'un flux de gaz contenant de l'hydrogène sulfuré Ceased WO2018202406A1 (fr)

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Application Number Priority Date Filing Date Title
DE102017207328.4 2017-05-02
DE102017207328 2017-05-02

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WO2018202406A1 true WO2018202406A1 (fr) 2018-11-08

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111440646A (zh) * 2020-04-21 2020-07-24 武汉国力通能源环保股份有限公司 一种油气田井口酸气自循环硫回收橇装装置及回收方法

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014170047A1 (fr) * 2013-04-15 2014-10-23 Siemens Aktiengesellschaft Agent absorbant, procédé pour le fabriquer, ainsi que procédé et dispositif de séparation de sulfure d'hydrogène d'avec un gaz acide
WO2016180555A1 (fr) * 2015-05-12 2016-11-17 Siemens Aktiengesellschaft Procédé et dispositif de désulfuration d'un flux de gaz

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014170047A1 (fr) * 2013-04-15 2014-10-23 Siemens Aktiengesellschaft Agent absorbant, procédé pour le fabriquer, ainsi que procédé et dispositif de séparation de sulfure d'hydrogène d'avec un gaz acide
WO2016180555A1 (fr) * 2015-05-12 2016-11-17 Siemens Aktiengesellschaft Procédé et dispositif de désulfuration d'un flux de gaz

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111440646A (zh) * 2020-04-21 2020-07-24 武汉国力通能源环保股份有限公司 一种油气田井口酸气自循环硫回收橇装装置及回收方法

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