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WO2018166937A1 - Procédé et dispositif de préparation d'un flux de gaz contenant du sulfure d'hydrogène - Google Patents

Procédé et dispositif de préparation d'un flux de gaz contenant du sulfure d'hydrogène Download PDF

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Publication number
WO2018166937A1
WO2018166937A1 PCT/EP2018/056003 EP2018056003W WO2018166937A1 WO 2018166937 A1 WO2018166937 A1 WO 2018166937A1 EP 2018056003 W EP2018056003 W EP 2018056003W WO 2018166937 A1 WO2018166937 A1 WO 2018166937A1
Authority
WO
WIPO (PCT)
Prior art keywords
catalyst
washing medium
stage
regeneration
absorber
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/EP2018/056003
Other languages
German (de)
English (en)
Inventor
Stefan Hauke
Ralph Joh
Hans Wolfgang Nickelfeld
Rüdiger Schneider
Michael Schüler
Hatice Gülsah Sönmez
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 WO2018166937A1 publication Critical patent/WO2018166937A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • B01D53/14—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 absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • 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
    • B01D53/14—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 absorption
    • B01D53/1456—Removing acid components
    • B01D53/1468—Removing hydrogen sulfide
    • 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
    • B01D53/14—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 absorption
    • B01D53/1493—Selection of liquid materials for use as absorbents
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/10—Oxidants
    • B01D2251/102—Oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20494—Amino acids, their salts or derivatives
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B01D2256/245—Methane
    • 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
    • C10L2290/24—Mixing, stirring of fuel components
    • 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
    • C10L2290/46—Compressors or pumps
    • 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
    • C10L2290/48—Expanders, e.g. throttles or flash tanks
    • 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

Definitions

  • the invention relates to a process for the treatment of a hydrogen sulfide-containing gas stream, in particular a natural gas stream. Furthermore, the invention relates to a device for the treatment of a hydrogen sulfide-containing gas flow.
  • Natural gas is a fossil fuel with a relatively low emission of carbon dioxide (C0 2 ) and a comparatively low emission of other waste products during combustion. His contribution as one of the most important
  • countercurrent bubble columns are generally used as contact devices.
  • gassing stirrers perforated plates, sintered metal internals or other gassing systems such as membrane aerators, nozzles (for example Venturi nozzles) or gassing rings are used.
  • bubble columns In order for a functioning bubble regime to develop in a bubble column, the gas load must not be too high, since otherwise the gas bubbles coalesce and even then the necessary mass transfer surface for catalyst regeneration is not reached. Therefore, bubble columns must be designed with a comparatively large diameter, which leads to a high space requirement and high investment costs.
  • sour natural gas as part of the local energy supply, however, it is necessary that the plants used here (for example, for offshore applications) take up little space.
  • the weight of liquid hold-up at this point makes operation of direct oxidation processes with bubble columns as contact devices for catalyst regeneration unfavorable.
  • bubble columns during operation are sensitive to the change in the surface tension, which influences the foaming behavior in the respective bubble columns.
  • the alkaline washing media commonly used for the treatment of natural gas show such an increased foaming tendency.
  • the invention is therefore based on the object to provide a way for efficient and cost-effective treatment of a hydrogen sulfide-containing gas stream and in particular a natural gas stream.
  • a hydrogen sulfide-containing gas is used for the treatment of a hydrogen sulfide-containing gas stream and in particular of a natural gas stream
  • a static mixer is used for the regeneration of the catalyst in the regeneration stage.
  • a static mixer as a contact apparatus of the necessary for the regeneration of the catalyst while recovering the regenerated washing medium intensive contact between the two phases, ie the oxygen-containing gas and the liquid is ensured.
  • a static mixer in contrast to the previously used bubble columns in terms of the ratios of the gas and liquid flows are operated much more flexible, since, for example, different bubble regimes play no role. Due to the intensive mixing of the two phases results in a very efficient mass transfer, so that even comparatively short residence times of the two phases in the static are sufficient to ensure the regeneration of the catalyst.
  • a static mixer is understood to mean a mixer which comprises non-movable, flow-influencing mixing elements.
  • the mixing is thus achieved solely by the flow movement of the phases or reactants to be mixed.
  • the mixing elements influencing the flow for example by means of screws, lamellas or even lattices, expediently are arranged one behind the other in a corresponding tube.
  • the loaded washing medium and the oxygen-containing gas flow through the static mixer, preferably in cocurrent.
  • a laden washing medium in the sense of the present invention is understood as meaning a washing medium which (in precipitated form) reduces the catalyst and elemental sulfur reduced in the formation of the sulfur. holds.
  • the mixing elements divide the flowing through the tube stream from the loaded washing medium and the oxygen-containing gas, twist the resulting partial flows and lead them together again.
  • the mixing elements in a static mixer thus ensure a constant renewal of the
  • Phase interfaces which speeds up the mass transfer.
  • the necessary residence time of the two phases in the static mixer can be considerably reduced and, compared to a bubble column, the liquid holdup can also be significantly reduced.
  • the surface tension of the washing medium which is responsible for undesirable foaming, has only a small influence on the process performance in the case of a static mixer.
  • the process can be operated more stable, since unlike the bubble column there is no danger that unwanted liquid with the air flow from the regeneration stage will be discharged (effervescence).
  • the previously reduced catalyst contained in the loaded wash medium is reformed during the passage of the static mixer by the reaction with the oxygen-containing gas.
  • the oxygen-containing gas is expediently flowed into the regeneration stage or into the static mixer for this purpose.
  • Under an oxygen-containing gas in the context of the present invention is basically understood to mean any gas whose oxygen content is high enough to rebuild the catalytic active components.
  • sour Substance-containing gas can be used for example ambient air, oxygen-enriched air or pure oxygen.
  • the oxygen contained in the gas passes from the gas phase into the liquid phase, ie into the washing medium.
  • the oxygen-containing gas depleted of oxygen.
  • the oxidation of the catalyst previously reduced in sulfur formation takes place; the catalyst is regenerated or recovered.
  • the washing medium containing the regenerated catalyst is then again available for the separation of hydrogen sulfide and its subsequent oxidation available.
  • a multiphase mixture of regenerated wash medium, oxygen-depleted gas, and contained solids leaves the membrane contactor.
  • the multiphase mixture is preferably fed to a separation stage in which the two phases are separated from one another.
  • the separation of gas and liquid in this separation stage for example, a gas-liquid separator, is not critical, since the phases here in the DC (on) flow.
  • the oxygen-depleted gas is expediently released into the environment.
  • the regenerated washing medium is expediently fed to the absorber starting from the separating stage and is used there for the reprocessing of a gas stream flowing into the absorber.
  • the catalyst used is a metal salt. In principle, all metal salts of which the metal ions can be present in several oxidation states are suitable here.
  • the salts of the metals iron, manganese or copper are used.
  • the oxidation of the Schweielwasser- substance to elemental sulfur thus takes place with simultaneous reduction of the metal ion.
  • the sulfur precipitates as a solid and the metal ions remain dissolved in the wash medium.
  • a washing medium is used which contains the catalyst, ie the respective metal salt.
  • the laden washing medium flowing out of the absorber can be fed directly from the absorber to the regeneration stage in order to regenerate the reduced catalyst there.
  • methane (CH 4 ) also dissolves in the washing medium, which during the regeneration of the washing medium (within the regeneration stage) can reach the gas used for this purpose which leaves the regeneration stage again.
  • this must be avoided for safety reasons.
  • the loaded washing medium prefferably be depressurized before it is fed to the regeneration stage.
  • a prescribed unwanted enrichment of natural gas components such as methane (CH 4 ) is prevented in the washing medium.
  • the natural gas components absorbed in the washing medium are desorbed from the washing medium and preferably separated before entering the regeneration stage.
  • the separated methane or the methane-containing partial stream is again compressed and the emerging from the absorber, purified from H 2 S.
  • Gas stream sweet gas supplied.
  • the methane can be supplied to a further use.
  • the essentially methane-free washing medium after the expansion is then fed to the regeneration stage as described above.
  • the separation of the elemental sulfur takes place by the removal of a partial flow of the washing medium before it enters the regeneration stage.
  • the partial flow can take place, for example, either before the expansion of the laden washing medium flowing out of the absorber or else afterwards. Preference is given to a removal of the partial flow of the expanded washing medium.
  • the sulfur contained in the partial flow is expediently separated therefrom.
  • the separation is preferably carried out by means of customary separation units, for example by means of a hydrocyclone or by means of filtration units.
  • the sulfur itself is expediently sent for further utilization.
  • the sulfur-purified partial stream of the washing medium can then be recycled at various points in the process.
  • the part-stream purified by sulfur is fed to the expansion stage.
  • the partial flow is metered into the washing medium supplied to the regeneration stage and flows together with it into the regeneration stage.
  • direct dosing into the regeneration stage may also be advantageous.
  • 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.
  • Hydrogen sulfide-containing gas stream in particular a natural gas stream, comprises an absorber for the absorption of
  • Hydrogen sulphide by means of a washing medium and for closing oxidation of the absorbed hydrogen sulfide to elemental sulfur with reduction of a catalyst used for this purpose, as well as a fluidically coupled with the absorber regeneration stage for regeneration of the reduced catalyst by means of an oxygen-containing gas, wherein the regeneration stage is designed for regeneration of the catalyst with a static mixer.
  • the hydrogen sulfide is absorbed by absorption in the washing medium from a gas stream.
  • the washing medium used here is preferably an amino acid salt solution.
  • the absorbed within the absorber in the washing medium hydrogen sulfide reacts within the absorber by means of a catalyst to elemental sulfur and is thereby reduced itself.
  • the catalyst used is preferably a metal salt which is contained in the washing medium.
  • the laden washing medium is supplied to the fluidically coupled with the absorber regeneration stage. Trained with a static mixer regeneration stage is connected downstream of the absorber in the flow direction of the loaded washing medium.
  • the absorber expediently comprises a discharge line, which is fluidically coupled to a supply line of the regeneration stage. In this way, the loaded washing medium, starting from the absorber, can flow into the regeneration stage where the previously reduced catalyst is regenerated as part of the sulfur precipitation.
  • the loaded wash medium flows with an oxygen-containing gas in cocurrent through the regeneration stage.
  • the regeneration stage is expediently connected to a corresponding supply line.
  • the reduced catalyst in the absorber is then recovered in the regeneration stage by oxidation by means of the oxygen-containing gas.
  • the regeneration stage downstream of a separation stage fluidically.
  • the separation stage is used to separate the emerging from the regeneration stage or the static mixer two-phase mixture of regenerated wash medium (low Schweielanteil, regenerated catalyst) and oxygen depleted or depleted gas.
  • the regeneration stage is connected to a discharge line, which is fluidically coupled to a supply line of the separation stage.
  • the separation stage is the regeneration stage thus downstream in the flow direction of the two-phase mixture.
  • the separation stage is suitably connected to a discharge line, via which the depleted gas is removed from the process.
  • the discharge line of the separation stage is expediently coupled to a supply line of a gas turbine.
  • the regenerated washing medium is returned to the absorber starting from the separation stage and used there for the renewed absorption of hydrogen sulphide and for its oxidation to elemental sulfur.
  • the separation stage is expediently coupled fluidically with the absorber.
  • the absorber of the separation stage is downstream in terms of flow in the flow direction of the regenerated washing medium.
  • a discharge line of the separation stage is fluidically coupled to a supply line of the absorber.
  • an expansion stage a so-called flash stage, is fluidically connected between the absorber and the regeneration stage. In the expansion stage, the effluent from the absorber is discharged. mende washing medium containing the precipitated sulfur and the reduced catalyst, relaxed.
  • natural gas components contained in the scrubbing medium in particular methane, are desorbed, thus preventing their undesired enrichment in the scrubbing medium.
  • the expansion stage is expediently connected in the discharge line of the absorber and downstream of the absorber in the flow direction of the loaded washing medium flow. After the expansion, the substantially methane-free washing medium is withdrawn via a discharge line connected to the expansion stage and fed to the regeneration stage. Preferably, the expansion stage is connected to a removal line for removal of at least a partial flow of the washing medium. So part of the oxidation of the
  • Hydrogen sulfide precipitated elemental sulfur are separated from the wash medium.
  • the preferred concentration of the precipitated sulfur remaining in the washing medium after separation is in a range between 1% and 10%.
  • a removal line for removing a partial flow of the loaded washing medium may also be connected elsewhere.
  • a discharge line of the absorber (before the relaxation) or the supply line of Regegenerationstress (after the relaxation) connected discharge line is possible.
  • the separation of the sulfur is preferably carried out in a flow direction of the
  • Partial flow of the extraction line fluidly connected separation unit fluidly connected separation unit.
  • the use of a hydrocyclone or a filtration unit is expedient here.
  • the separated sulfur itself is expediently sent for further utilization.
  • the sulfur-purified partial stream of the washing medium is preferably fed to the expansion stage.
  • a return line of the separation unit fluidly coupled to a supply line of the expansion stage.
  • a return line of the separation unit fluidly coupled to a supply line of the expansion stage.
  • Return line of the separation unit fluidly coupled to a supply line of the regeneration stage, so that the part of the washing medium purified by sulfur is metered to the washing medium supplied to the regeneration stage and is fed together with this (as a combined main stream) of the regeneration stage.
  • a further preferred embodiment is the direct fluidic coupling of the return line of the separation unit with the regeneration stage.
  • the return line of the separation unit is fluidically coupled to a separate supply line of the regeneration stage.
  • the sulfur-purified partial stream of the washing medium is fed to the regeneration stage in this case separately from the main stream.
  • FIG. 1 shows a schematic representation of a device for processing a gas stream with a static mixer, as well
  • FIG 1 a device 1 is shown, which is used for the treatment of a hydrogen sulfide 2 containing gas stream 3.
  • the gas stream 3, in this case a natural gas stream, is fed via a feed line 5 to an absorber 7.
  • the absorber 7 is an aqueous amino acid salt solution as the washing medium 9.
  • the gas stream 3 is contacted in countercurrent with the washing medium 9, wherein the hydrogen sulfide 2 contained in the gas stream 3 is absorbed in the washing medium 9.
  • the purified in this way of hydrogen sulfide 2 gas stream 10 is withdrawn via a discharge line 11 from the absorber 7 and can then be fed to a further use.
  • the hydrogen sulfide 2 absorbed in the washing medium 9 is oxidized by a catalyst 13 contained in the washing medium 9, in the present case a Fe (III) salt, to elemental sulfur 14, which precipitates in the washing medium 9.
  • the catalyst 13 is reduced in this case, the metal ions (Fe (II) ions) remain in solution.
  • the loaded washing medium 15, which now contains the reduced catalyst 17 and elemental sulfur 14, is now supplied to the absorber 7 fluidically downstream expansion stage 21 (flash stage).
  • a discharge line 23 of the absorber 7 is fluidically coupled to a feed line 25 of the expansion stage 21
  • the loaded washing medium 15 is expanded and desorbed in this contained natural gas components such as in particular contained methane.
  • Desorbed natural gas components escape via one of the expansion stage 21 connected to the discharge line 27 from the process.
  • Wash medium 15 removed from the expansion stage 21 via one of these connected extraction line 31 reduces the concentration of precipitated sulfur 14 in the loaded wash medium 15 to a concentration of about 5%.
  • the withdrawn from the washing medium 15 partial stream 29 is supplied via the withdrawal line 31 designed as a hydrocyclone separation unit 33, in which the sulfur 14 is separated from the washing medium 15.
  • the separated from the partial flow 29 sulfur 14 itself is fed to a further utilization 35.
  • the scrubbing medium 15 purified by sulfur 14 is supplied to the expansion stage 21 in the present case.
  • a return line 36 of the separation unit 33 is fluidically coupled to a supply line 38 of the expansion stage 21.
  • the loaded washing medium 15, starting from the expansion stage 21, is supplied to one of these regeneration stages 37 downstream of the latter in the direction of flow of the loaded washing medium 15.
  • a discharge line 39 of the expansion stage 21 is fluidically coupled to a supply line 41 of the regeneration stage 37.
  • the regeneration stage 37 is formed with a static mixer 43, which comprises in a tube 45 static mixing elements 47 arranged one behind the other. A detailed description of the static mixer 43 can be seen in FIG.
  • an oxygen-containing gas 49 in the present case atmospheric oxygen, flows over one
  • Feed line 50 in the regeneration stage 37 a The laden washing medium 15 and the oxygen-containing gas 49 flow through the regeneration stage 37, that is to say the static mixer 43 in the same direction, ie in the same direction.
  • the regeneration stage 37 that is to say the static mixer 43 in the same direction, ie in the same direction.
  • the oxygen-containing gas 49 of the previously reduced catalyst 17 Upon contact of the loaded washing medium 15 with the oxygen-containing gas 49 of the previously reduced catalyst 17 is regenerated by the oxidation of Fe (II) ions to Fe (III) - ions.
  • the catalyst 13 recovered in this way is then available for the renewed oxidation of hydrogen sulfide 2 available.
  • the regeneration stage 37 After the oxidation of the catalyst 17 leaves a mixture 51 of regenerated washing medium 9 and oxygen depleted gas 53, the regeneration stage 37. To separate the mixture 51 in its two phases 9, 53, the mixture 51 of the regeneration stage 37 fluidically downstream separation stage 55 is supplied. For this purpose, the regeneration stage 37, a discharge line 57 is connected, which is fluidically coupled to a feed line 59 of the separation stage 55.
  • the latter is discharged into the environment via a discharge line 61 connected to the separation stage 55.
  • a discharge line 61 connected to the separation stage 55.
  • the regenerated washing medium 9 is supplied to the absorber 7 starting from the separation stage 55.
  • a discharge line 63 of the separation stage 55 is fluidly coupled to a supply line 65 of the absorber 7.
  • the regenerated washing medium 9 is then used again for the treatment of a gas stream 3 fed to the absorber 7.
  • the static mixer 43 used in the device 1 according to FIG. 1 is shown.
  • the static mixer 43 comprises a plurality of static, flow-influencing mixing elements 47 arranged in the tube 45.
  • the static mixing elements 47 When the loaded washing medium 15 and the oxygen-containing gas 49 (starting from the expansion stage 21 or the absorber 7) via the corresponding supply lines 41, 50 in the static mixer 43 and this flow through the DC, the mixing is achieved solely by the flow movement of the two phases 15, 49.
  • the static mixing elements 47 a continuous renewal of the phase interface between the two phases 15, 49 is ensured, so that the necessary mass transfer between them and thus the desired Oxidation and thus regeneration of the catalyst 17 is ensured with only a short residence time within the static mixer 43.
  • the regeneration stage 37 leaving mixture 51 is, as already described for FIG 1, the separation stage 55 and the regenerated washing medium 9 separated there from the oxygen-depleted gas 53.
  • the regenerated washing medium 9 is returned to the absorber 7.

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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)
  • Analytical Chemistry (AREA)
  • Organic Chemistry (AREA)
  • Gas Separation By Absorption (AREA)
  • Industrial Gases (AREA)

Abstract

L'invention concerne un procédé de préparation d'un flux de gaz (3) contenant du sulfure d'hydrogène, en particulier d'un flux de gaz naturel. Un flux de gaz (3) contenant du sulfure d'hydrogène (2) est amené à un absorbeur (7), dans lequel le sulfure d'hydrogène (2) est absorbé dans un agent de lavage (9) et réagit au moyen d'un catalyseur (13) en du soufre élémentaire. Le catalyseur (13) se réduit lors de la réaction du sulfure d'hydrogène (2) absorbé. L'agent de lavage (15) chargé en un soufre (14) élémentaire et en le catalyseur (17) réduit est amené à une colonne de régénération (37), dans laquelle le catalyseur (17) réduit est régénéré par la réaction avec un gaz (49) contenant de l'oxygène. Un mélangeur (43) statique est utilisé aux fins de la régénération du catalyseur (17) dans la colonne de régénération (37). L'invention concerne par ailleurs un dispositif (1), qui comprend une colonne de régénération (37) réalisée avec un mélangeur statique (43) pour préparer un flux de gas (3).
PCT/EP2018/056003 2017-03-14 2018-03-12 Procédé et dispositif de préparation d'un flux de gaz contenant du sulfure d'hydrogène Ceased WO2018166937A1 (fr)

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Application Number Priority Date Filing Date Title
DE102017204190.0 2017-03-14
DE102017204190 2017-03-14

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WO2018166937A1 true WO2018166937A1 (fr) 2018-09-20

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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CN114262635A (zh) * 2021-12-09 2022-04-01 中国石油大学(北京) 一种天然气强化脱硫脱碳系统及方法

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