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EP2430213A1 - Procédé permettant la séparation électrolytique d'hydrogène sulfuré - Google Patents

Procédé permettant la séparation électrolytique d'hydrogène sulfuré

Info

Publication number
EP2430213A1
EP2430213A1 EP10721455A EP10721455A EP2430213A1 EP 2430213 A1 EP2430213 A1 EP 2430213A1 EP 10721455 A EP10721455 A EP 10721455A EP 10721455 A EP10721455 A EP 10721455A EP 2430213 A1 EP2430213 A1 EP 2430213A1
Authority
EP
European Patent Office
Prior art keywords
solution
hydrogen sulfide
amine
amine scrubber
acid
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.)
Withdrawn
Application number
EP10721455A
Other languages
German (de)
English (en)
Inventor
Marc Martin
Guenther Huber
Ruediger Schmidt
Martin Scholtissek
Heinrich Driever
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.)
BASF SE
Original Assignee
BASF SE
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 BASF SE filed Critical BASF SE
Priority to EP10721455A priority Critical patent/EP2430213A1/fr
Publication of EP2430213A1 publication Critical patent/EP2430213A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • 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
    • B01D53/32—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 electrical effects other than those provided for in group B01D61/00
    • B01D53/326—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 electrical effects other than those provided for in group B01D61/00 in electrochemical cells
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/21—Organic compounds not provided for in groups B01D2251/206 or B01D2251/208
    • 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

Definitions

  • the invention relates to a process for the electrolytic cleavage of hydrogen sulfide dissolved in a liquid in an electrolysis cell which has an anode space and a cathode space, wherein the anode space and the cathode space are separated by a membrane.
  • Oil, natural gas, coal and biomass are widely used as raw materials for energy production and for the production of chemical products. These raw materials generally contain a proportion of organo-sulfur compounds. During combustion or work-up, the sulfur remains in the form of climate-damaging sulfur oxides in the exhaust gases. For this reason, great efforts have been made to remove sulfur from the raw materials mentioned before they are put into incineration or further processing. The most commonly used process for the elimination of sulfur is hydrogenation. Sulfur-containing compounds split thereby hydrogen sulfide gas. A further major challenge today is the separation of the recovered hydrogen sulphide from the desired product and the conversion of the toxic hydrogen sulphide gas into non-toxic, disposable sulfur.
  • Gas scrubber solutions contain, as an essential ingredient, low-volatility amines, for example methyldiethanolamine (MDEA), diethanolamine (DEA), etc., which dissolve acid hydrogen sulfide from the hydrocarbon-containing gas mixture by physisorption and chemisorption and at the same time do not affect the hydrocarbon.
  • MDEA methyldiethanolamine
  • DEA diethanolamine
  • Large-scale gas scrubbers generally simultaneously dissolve other acidic gases such as CO 2 from the gas mixture.
  • the gas scrubber solutions are heated in a second step and thereby desorbing the dissolved gases again.
  • the hydrocarbon-free waste gas mixture is then reacted in a third step by the Claus method with air or oxygen at temperatures around 300 0 C to elemental sulfur and water vapor.
  • the Claus process has been continuously improved in recent decades, but still suffers from high energy consumption, poor controllability and associated high emissions, as well as costly safety technology due to the handling of toxic gases at high temperature and pressure.
  • a further disadvantage is that the required hydrogen is lost for the hydrogenation of the organosulfur compounds by the reaction in the Claus process as a raw material. Because hydrogen is usually made from hydrocarbons Reforming is generated, a not to be underestimated share of valuable product in sulfur removal is lost.
  • ammonium hydroxide as the electrolyte for the electrolysis of hydrogen sulfide is also known from US 4,765,873.
  • Organic amine compounds which form ammonium ions in aqueous solution are described as the electrolyte for the electrolysis of hydrogen sulfide in US 5,908,545.
  • the object of the present invention is to provide a process which allows an e-lektrolytician cleavage of dissolved in an amine scrubber solution hydrogen sulfide in an electrolytic cell.
  • the object is achieved by a process for the electrolytic cleavage of dissolved in an amine scrubber solution hydrogen sulfide in an electrolytic cell having an anode compartment and a cathode compartment, wherein the anode compartment and the cathode compartment are separated by a membrane.
  • the process embodies at least one of the following features:
  • the amine scrubber solution in which the hydrogen sulfide is dissolved contains at least 10% by volume of potassium N, N-dimethylaminoacetic acid.
  • the electrolysis for the cleavage of the hydrogen sulfide can also be carried out with large-scale amine scrubber solutions.
  • a cation-conducting membrane is used as the membrane which separates the anode space and the cathode space.
  • Amine scrubbers are used to remove hydrogen sulphide from exhaust gases, such as hydrocarbons refining, coal gasification, refining and desulfurization of renewable resources, and biogas production. Also amine scrubbers are used to remove hydrogen sulfide from natural gas.
  • the gas streams generally also contain carbon dioxide, carbon monoxide, carbon monoxide, carbon monoxide and carbon dioxide. sulfide, mercaptans, thiols and ammonia.
  • the carbon dioxide can be contained in large quantities in the gas stream. In the known processes based on alkali or NH 4 solutions, the carbon dioxide causes difficulties, since this reacts in aqueous hydroxide liquor to form carbonates.
  • hydrocarbons are used as the gas.
  • the impurities such as hydrogen sulfide and carbon dioxide are dissolved in the amine solutions. These contaminated with amine solutions are currently heated in a second reactor and hydrogen sulfide, carbon dioxide and the remaining impurities desorbed again.
  • the amine scrubber solutions used generally have only a very low specific conductivity and are therefore not suitable for electrochemical processes.
  • a hydrogen ion of the hydrogen sulfide becomes attached to the nitrogen of the amine, thereby producing an amine cation.
  • the corresponding salts of the amine with hydrogen sulfide form as a counterion.
  • This increases the conductivity of the solution so that it would be sufficient to carry out an electrolysis.
  • this electrolysis does not work because the cations are too large to pass through the cation-conducting membranes used.
  • the cell resistance of the membrane is too large and only low currents can be driven. Therefore, a large-scale electrolysis is not possible. At a higher load on the cell, the membrane ruptures due to the size of the ions.
  • the addition of the at least one conducting salt to the liquid gives a sufficiently high conductivity in order to be able to carry out an electrolysis; moreover, with the conducting salt it is also possible to carry out an electrolysis since the added cations of the conducting salt form the membrane can happen. Furthermore, it has been shown that the absorption capacity of the amine scrubber solution for hydrogen sulfide is not due to the addition of the conductive salt to the liquid is impaired. Surprisingly, the selectivity between Leitsalzkation and Aminkation is so high that the membrane is not damaged even at high current densities. Furthermore, it has been shown that the absorption of carbon dioxide, which is weakly bound in the amine scrubber solution by physisorption, does not interfere with the electrolysis.
  • Another technically significant problem of the prior art methods is the passivation of the anode of the electrolytic cell with sulfur.
  • sulfur does not precipitate until it falls below a pH which depends on the amine of the amine scrubber solution.
  • the pH can be monitored in a simple manner and allows a targeted setting of the electrolysis. It is possible to maintain the pH of the amine scrubber solution, for example by selective addition of acid or alkali, at a level at which the sulfur remains dissolved in the amine scrubber solution.
  • Suitable acids or bases for adjusting the pH are, for example, mineral acids, for example sulfuric acid, nitric acid, hydrochloric acid or phosphoric acid, and / or hydroxides of the alkali metals, in particular sodium hydroxide, potassium hydroxide or lithium hydroxide.
  • Suitable conductive salts which can be added to the amine scrubber solution are, in particular, salts of an alkali metal.
  • Suitable alkali metals are in particular lithium, sodium and potassium.
  • the anion of the conductive salt is preferably selected from the group consisting of sulfate, sulfide, phosphate, hydroxide, halide, carbonate and hydrogen sulfide.
  • a chloride is particularly preferred.
  • Very particularly preferred as conductive salts are alkali metal chlorides and of these very particularly sodium chloride.
  • the conductive salt may alternatively also be an organic salt of an alkali metal or alkaline earth metal.
  • Suitable organic salts of the alkali or alkaline earth metals are, for example, typical organic conducting salts, for example smaller water-soluble carboxylates, in particular formates, acetates and oxalates, and all types of deprotonated amino acids.
  • the proportion of conductive salt in the hydrogen sulfide-containing amine scrubber solution is preferably in the range of 1 to 13.8 wt .-%.
  • the proportion of conductive salt is close to the saturation limit.
  • the molar ratio of conductive salt to dissolved hydrogen sulfide is preferably between 1 and 2.
  • the resulting solution in the electrolysis is preferably removed from the anode compartment prior to the formation of trisulfides.
  • the solution removed from the anode compartment is acidified outside the electrolysis cell.
  • decompose the disulfides in sulfur and sulfides the sulfur precipitates.
  • the sulfur formed is easily filterable and is separated from the remaining solution.
  • the solution is passed into the cathode compartment.
  • the salt formed from the amine cation and the anion of the conducting salt is deprotonated in the cathode space by the hydroxide ions formed there, so that again the conducting salt and a free amine are formed.
  • the solution can thus be used again for gas scrubbing.
  • Electroneutrality means that as much base is produced as sulfide is oxidized.
  • the acid required to precipitate the sulfur from the disulfide solution can be added separately. However, it is also possible to produce this acid electrochemically. If, for example, a part of the solution is returned to the anode compartment of an electrolytic cell of the same structure after precipitation of the sulfur, water is not oxidized at the prevailing pH value. While caustic and hydrogen are formed in the cathode compartment as in the electrolysis of the hydrogen sulfide, an acid forms on the anode side. This can be used to initiate sulfur precipitation.
  • sodium chloride When sodium chloride is used as conductive salt, it is thus possible, for example, to first dissolve it in the amine scrubber solution.
  • the sodium ions are very suitable for passing through the cation-conducting membrane used.
  • sulfide ions are oxidized to disulfide ions, without a failure of sulfur is observed.
  • two sodium ions pass through the membrane into the cathode compartment. Water is reduced in the cathode compartment and forms hydrogen and hydroxide ions.
  • the chloride ions remain in the anode compartment and form an ammonium chloride with the ammonium cations. As a result, the pH of the solution decreases.
  • the hydroxide ions formed there deprotonate the chloride of the ammonium cations and form again sodium chloride and free amine, which can be used again for gas scrubbing.
  • Electroneutrality means that as much base is produced as sulfide is oxidized. Thus, just as much chloride of the cation of the amine is produced.
  • the pH at which the formation of sulfur can be suppressed is preferably in the range of 7.5 to 8.5
  • a conducting salt can be dispensed with if the membrane used is not a cation-conducting membrane but an anion-conducting membrane.
  • the membrane is migrated by the sulfide ions contained in the amine scrubber solution.
  • the sulfide ions have a sufficiently good conductivity through the anion-conducting membrane, so that the addition of a conducting salt is not required.
  • Suitable anion-conducting membranes are, for example, membranes which contain a polymer having quaternary ammonium groups or phosphonium groups.
  • a suitable anion-conducting membrane is, for example, FUMASEP FAA® from FuMach Tech GmbH.
  • At least one conductive salt is added and an anion-conducting membrane is used.
  • Suitable electrolyte salts are the same salts which have been described above.
  • Particularly preferred salts are here also salts of the alkali metals, in particular halides of the alkali metals and very particularly sodium chloride.
  • the amine scrubber solution used to remove hydrogen sulfide from the gas stream is preferably an aqueous solution containing at least 10% by volume of methyldiethanolamine (MDEA), diethanolamine (DEA), aminoethoxyethanol (ADEG), di-isopropanolamine (DIPA). or potassium N, N-dimethylamioacetic acid.
  • MDEA methyldiethanolamine
  • DEA aminoethoxyethanol
  • DIPA di-isopropanolamine
  • potassium N, N-dimethylamioacetic acid is especially preferred.
  • Aminoethoxyethanol (ADEG), diisopropanolamine (DIPA) or potassium N, N-dimethylaminoacetic acid in the amine scrubber solution in the range of 30 to 50% by volume.
  • potassium N, N-dimethylaminoacetic acid is particularly preferred.
  • Advantage of the use of potassium N, N-dimethylaminoacetic acid is that even when using a cation-conducting membrane, it is not necessary to additionally add a conductive salt. During electrolysis, the potassium ion can pass through the cation-conducting membrane.
  • the amine scrubber solution is an aqueous solution containing potassium N, N-dimethylaminoacetic acid, it preferably contains at least 10% by volume of potassium N, N-dimethylaminoacetic acid.
  • the proportion of potassium N, N-dimethylaminoacetic acid in the amine scrubber solution is in the range of 30 to 48% by volume.
  • the conductivity of a solution containing potassium N, N-dimethylaminoacetic acid is initially very low, but increases with saturation with hydrogen sulfide, the conductivity to a sufficiently high value.
  • the conductivity in a 40% aqueous solution with potassium N, N-dimethylaminoacetic acid after saturation with hydrogen sulfide to 100 mS / cm rise. This value is sufficient to carry out the electrolysis.
  • a further improvement of the electrolysis is possible by adding a conductive salt.
  • Figure 1 is a flow diagram of an exhaust gas purification with an electrolytic cell for the separation of hydrogen sulfide
  • Figure 2 is a flow diagram of an exhaust gas purification with an electrolytic cell for the separation of hydrogen sulfide and an acid electrolysis.
  • FIG. 1 shows a flow diagram of an exhaust gas purification with electrolysis cell for the separation of hydrogen sulfide is shown.
  • An amine scrubber 1 is fed via an inlet 3 to be cleaned, containing hydrogen sulfide exhaust gas.
  • the exhaust gas comes, for example, from the oil or gas processing industry.
  • natural gas containing hydrogen sulfide can be supplied to the amine scrubber 1, the hydrogen sulfide being removed from the natural gas in the amine scrubber 1.
  • this can be Mine scrubber 1 supplied, for example, any other refinery gas obtained in the petroleum or natural gas processing industry, be.
  • Any other exhaust gas containing any other hydrogen sulfide can be supplied to the amine scrubber 1.
  • Suitable amine scrubber 1 is any gas scrubber known to the person skilled in the art.
  • gas scrubbers are used, for example, as washing columns, in which the gas to be purified is passed through a scrubbing liquid contained therein or in which a scrubbing liquid is injected into a column.
  • Further suitable scrubbers are, for example, venturi scrubbers, jet scrubbers or washing columns.
  • the purified exhaust gas that is, the exhaust gas from which the hydrogen sulfide has been removed, is removed from the amine scrubber 1 via a trigger 5.
  • the washing liquid used in the amine scrubber 1 is an aqueous solution of an amine.
  • amines are, for example, methyldiethanolamine, diethanolamine, aminoethoxyethanol, diisopropanolamine or potassium N, N-dimethylamioacetic acid.
  • the hydrogen sulfide dissolves to form hydrosulfide ions and amine cations by protonation of the nitrogen atom in the amine in the scrubber solution.
  • the amine scrubber solution in which the hydrogen sulfide is dissolved is fed via a feed line 7 to an anode chamber 9 of an electrolytic cell 11.
  • sulfide ions contained in the amine scrubber solution form a disulfide with the release of two electrons.
  • the necessary charge balance is achieved by transporting cations through a cation-conducting membrane 13 into a cathode compartment 15.
  • the cations are the cations of a conductive salt which is added to the amine scrubber solution.
  • the cations of the amine contained in the amine scrubber solution are generally too large for transport through the pores of the cation-conducting membrane 13.
  • the electrolyte from the anode chamber 9 is fed to a device for sulfur precipitation 17.
  • acid is added to reduce the pH of the apparatus for sulfur precipitation 17 via an acid feed 19 acid is added.
  • the acid addition decomposes the disulfide into sulfur and sulfide.
  • the precipitated sulfur is removed via a sulfur removal 21 from the device for sulfur precipitation 17.
  • FIG. 2 shows a flow diagram of an exhaust gas purification with electrolysis cell for the separation of hydrogen sulfide and an acid electrolysis.
  • the embodiment shown in FIG. 2 differs from the embodiment shown in FIG. 1 in that the acid required for sulfur precipitation is produced in an acid electrolysis cell 29.
  • the acid passes from the acid electrolysis cell 29 via an acid line 31 into the apparatus for sulfur precipitation 17.
  • a filter element 33 is provided in the apparatus for sulfur precipitation 17 to remove solids, for example precipitated sulfur, from the solution.
  • any filter element known to the person skilled in the art is suitable as the filter element 33.
  • a corresponding filter element 33 can of course also be provided in the device for sulfur precipitation 17 shown in FIG.
  • Suitable filter elements 33 are, for example, filter presses, centrifugal cleaning filters, plate filters, decanter centrifuges and belt filters. However, it is also possible to use any other suitable filter element known to the person skilled in the art.
  • the solution is fed to the acid electrolysis cell 29.
  • the solution is uniformly added to the anode compartment 35 and the cathode compartment 37 of the acid electrolyte cell 29.
  • the acid electrolysis cell 29 preferably corresponds to the electrolytic cell 1 1.
  • the anode chamber 35 and the cathode chamber 37 of the acid electrolysis cell 29 are likewise separated from one another by a membrane 39.
  • the membrane is preferably made of the same material as the membrane 13 of the electrolytic cell 1 1.
  • the acid electrolysis cell 29 In the acid electrolysis cell 29, a water electrolysis takes place, 29 hydrogen and the base of the cation of the conductive salt is formed in the cathode compartment 37 of the acid electrolysis cell and in the anode compartment 35 of Acid electrolyte cell 29 the acid of the anion of the conductive salt. This acid is then passed via the acid line 31 into the apparatus for sulfur precipitation 17. From the cathode compartment 37 of the acid electrolysis cell 29, the solution is passed further into the cathode compartment 15 of the electrolytic cell 11.
  • Sodium chloride is preferably used as conductive salt.
  • the acid electrolyte cell 29 forms hydrochloric acid in the anode compartment 35 and sodium hydroxide solution and hydrogen in the cathode compartment 37 of the acid electrolyte cell 29.
  • the advantage of using the acid electrolysis cell 29 is that in each case exactly as much acid is produced as is produced in the cathode space 37 of the acid electrolysis cell 29 base. This preserves the acid-base balance.
  • it has been found in the use of sodium chloride as conductive salt that no oxygen formation occurs at the anode. Also, no by-products such as sulfites, thiosulfates or sulfates are formed.
  • Another advantage of using the conducting salt, especially sodium chloride is that the conductivity of the solution remains largely constant throughout the course of the electrolysis.
  • the potassium ions When using potassium N, N-dimethylamioacetic acid, the potassium ions can be transported through the cation-conducting membrane 13. The use of an additional conductive salt is therefore not necessary.
  • an electrolysis cell for the electrolytic cleavage of hydrogen sulfide, an electrolysis cell is used, in which the anode space and the cathode space are protected by a cation-conducting
  • the cation-conducting membrane used is a NafionO membrane.
  • the electrolysis was carried out at room temperature and without pressure. The electrolyte warmed up during the experiment due to ohmic heat loss.
  • the anode loop is filled with 532 g of an amine scrubber solution in which hydrogen sulfide is absorbed.
  • an amine scrubber solution in which hydrogen sulfide is absorbed.
  • 200 g of methyldiethanolamine and 300 g of water are added to a scrubbing tower.
  • 80 g of NaCl are dissolved.
  • An empty wash bottle and a wash bottle filled with NaOH solution to absorb excess hydrogen sulfide are connected to the wash tower.
  • Hydrogen sulphide is passed into the solution until the solution is saturated and hydrogen sulphide is no longer absorbed. From the solution, 35 g of hydrogen sulfide are absorbed.
  • the specific conductivity of the solution is 72 mS / cm.
  • the cathode circuit of the electrolysis cell is filled with 500 g of 1 N NaOH solution.
  • the exhaust gas of the anode circuit is checked for the formation of oxygen by means of an oxygen sensor. Both circuits are superimposed with 40 l /
  • an electrolytic cell as in Example 1, an electrolytic cell is performed. However, the anode cycle is now filled with 537 g of an amine scrubber solution based on potassium N, N-dimethylamioacetic acid.
  • an amine scrubber solution based on potassium N, N-dimethylamioacetic acid.
  • 200 g of potassium N, N-dimethylaminoacetic acid and 300 g of water are placed in a scrubbing tower.
  • the washing tower is connected to an empty wash bottle and a wash bottle filled with sodium hydroxide solution to take up excess hydrogen sulfide. Hydrogen sulphide is then passed into the wash solution until the solution is saturated. From the solution 49 g of hydrogen sulfide are absorbed.
  • the specific conductivity of the solution is 118 mS / cm.
  • the cathode circuit of the electrolysis cell is filled with 500 g of 1 N KOH solution.
  • the exhaust gas of the anode circuit is tested by means of oxygen sensor for the formation of oxygen. Both circuits are superimposed with 40 l / h of nitrogen.
  • a constant current of 20 A (2000 A / m 2 ) is applied. After about 34 Ah (44% conversion) and a pH of 8.5 in the anode loop, the sulfur outage is observed. If the electrolysis is stopped at pH 8.5, no sulfur will precipitate. Already precipitated sulfur dissolves again to pH> 8.5.
  • An electrolysis cell is used in which the anode compartment and the cathode compartment are separated by a cation-conducting membrane made of Nafion®. Graphite rods with a diameter of 12 mm are used as anodes and cathodes, respectively.
  • the electrolysis was carried out at room temperature and without pressure. The electrolyte warmed up during the experiment due to ohmic heat loss.
  • the anode circuit of the electrolysis cell is 44 g and the cathode circuit with
  • Example 3 An electrolytic cell is used as in Example 3. However, the cation-conducting membrane is used by an anion-conducting membrane (FUMASEP FAA®). The electrolysis is also carried out at room temperature and without pressure. Due to ohmic heat loss, the electrolyte heats up during the experiment.
  • the anode circuit is filled with 35 g and the cathode circuit with 33 g of an amine scrubber solution.
  • the amine scrubber solution is prepared as described in Example 1.
  • a constant electric current of 0.7 A about 620 mA / cm 2
  • After about 1.4 Ah (44% conversion) and a pH of 8 in the anode compartment the loss of sulfur is observed. If the electrolysis is stopped at pH 8, no sulfur precipitates. Already precipitated sulfur dissolves again at pH> 8.

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  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Electrochemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Treating Waste Gases (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
  • Gas Separation By Absorption (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)

Abstract

L'invention concerne un procédé permettant la séparation électrolytique d'hydrogène sulfuré dissous dans une solution de lavage aux amines dans une cellule d'électrolyse (11) comprenant un compartiment anodique (9) et un compartiment cathodique (15) séparés l'un de l'autre par une membrane (13). Selon le procédé, au moins un sel conducteur est ajouté à la solution de lavage aux amines, une membrane perméable aux anions est utilisée pour séparer le compartiment anodique (9) du compartiment cathodique (15) et/ou la solution de lavage aux amines, dans laquelle est dissous l'hydrogène sulfuré, contient au moins 10% en volume de N,N-diméthylaminoacétate de potassium. L'invention concerne en outre une utilisation de ce procédé.
EP10721455A 2009-05-14 2010-05-12 Procédé permettant la séparation électrolytique d'hydrogène sulfuré Withdrawn EP2430213A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP10721455A EP2430213A1 (fr) 2009-05-14 2010-05-12 Procédé permettant la séparation électrolytique d'hydrogène sulfuré

Applications Claiming Priority (3)

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EP09160208 2009-05-14
PCT/EP2010/056565 WO2010130791A1 (fr) 2009-05-14 2010-05-12 Procédé permettant la séparation électrolytique d'hydrogène sulfuré
EP10721455A EP2430213A1 (fr) 2009-05-14 2010-05-12 Procédé permettant la séparation électrolytique d'hydrogène sulfuré

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EP2430213A1 true EP2430213A1 (fr) 2012-03-21

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NL2035307B1 (en) * 2023-07-07 2025-01-14 Stichting Wetsus European Centre Of Excellence For Sustainable Water Tech Method for solvent regeneration used in carbon capture and/or sulphur capture, membrane device, membrane stack, and system to perform said method
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