WO2015018796A1 - Procédé et dispositif de traitement d'un flux de gaz, en particulier de traitement d'un flux de gaz de fumée - Google Patents

Procédé et dispositif de traitement d'un flux de gaz, en particulier de traitement d'un flux de gaz de fumée Download PDF

Info

Publication number
WO2015018796A1
WO2015018796A1 PCT/EP2014/066740 EP2014066740W WO2015018796A1 WO 2015018796 A1 WO2015018796 A1 WO 2015018796A1 EP 2014066740 W EP2014066740 W EP 2014066740W WO 2015018796 A1 WO2015018796 A1 WO 2015018796A1
Authority
WO
WIPO (PCT)
Prior art keywords
activator
washing medium
carbon dioxide
gas stream
washing
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/EP2014/066740
Other languages
German (de)
English (en)
Inventor
Markus Kinzl
Diego Andres Kuettel
Ralph Joh
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 WO2015018796A1 publication Critical patent/WO2015018796A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—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
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • 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
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/60—Additives
    • B01D2252/602—Activators, promoting agents, catalytic agents or enzymes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • the invention relates to a process for the treatment of a gas stream, in particular for the treatment of a flue gas stream. Furthermore, the invention relates to a device for the treatment of a gas flow, in particular for the treatment of a flue gas flow.
  • the flue gas is fed to an absorber as part of a conventional treatment device for separating carbon dioxide (C0 2 separation device), wherein gaseous carbon dioxide contained in the flue gas is dissolved in the washing medium or absorbed in a chemical sense.
  • C0 2 separation device for separating carbon dioxide
  • the exempt from carbon dioxide Exhaust gas will eventually release to the atmosphere.
  • the carbon dioxide-laden wash medium can be regenerated by desorbing the absorbed carbon dioxide and reused to absorb carbon dioxide from the flue gas.
  • activators can be used.
  • an activator such as monoethanolamine or
  • Diethanolamine lead to an improvement in the reaction rate.
  • activators run the risk of being emitted into the atmosphere due to their vapor pressure with the scrubbing flue gas leaving the absorber.
  • the associated loss of activator requires a continuous replenishment of new activator material in the washing medium used in the preparation process, which is associated with increased operating costs.
  • discharge of the activator together with the carbon dioxide-purified flue gas contributes to undesirable environmental impact.
  • a second object of the invention is to provide a device with which a corresponding method can be carried out economically.
  • the first object of the invention is achieved by a process for the treatment of a gas stream, in particular for the treatment of a flue gas stream, in which a
  • Absorber is supplied to a gas stream, carbon dioxide contained in the gas stream is deposited in the absorber by means of a washing medium, the loaded with carbon dioxide washing medium an Nem desorber is fed, the carbon dioxide contained in the scrubbing medium is released from the scrubbing medium in the desorber, which is supplied in the desorber freed from carbon dioxide scrubbing medium a treatment stage, in which contained in the scrubbing medium sulfur oxides are separated as potassium sulfate, and purified in the treatment stage Washing medium is returned to the absorber.
  • a regenerable activator is used in the washing medium, which increases the absorption rate of the carbon dioxide in the washing medium and / or the desorption of carbon dioxide from the washing medium.
  • the invention takes into account that in order to accelerate the absorption and / or the desorption of carbon dioxide in the treatment of a gas stream, the use of an activator is possible.
  • an activator By means of an activator both the absorption process and the desorption process can be accelerated and in this way the effectiveness of the treatment of a
  • Total flue gas flow can be increased.
  • an activated activator is discharged into the atmosphere.
  • an activator loss is to be avoided due to the required efficiency of the treatment process. This is not satisfactorily possible with the use of activators.
  • the invention recognizes that it is then possible to meet the requirements for a cost-effective and environmentally friendly treatment of a gas stream, if a regenerable activator is used in the washing medium, the rate of absorption of the carbon dioxide in the washing medium and / or increases the rate of desorption of carbon dioxide from the washing medium.
  • activators are understood as regenerable activators, which are not or only insignificantly in the context of the treatment process of a gas stream be consumed and thus in the process can be recovered substantially completely.
  • the regenerability of the activator used gives two advantages at the same time. On the one hand, by increasing the absorption rate of carbon dioxide in the washing medium and the desorption rate of carbon dioxide from the washing medium, the entire treatment process is accelerated. On the other hand, a subsequent dosing of the activator (activator-refill) used in the process is not or only to a very small extent necessary, whereby possible additional costs in the
  • Implementation of the treatment process can be saved.
  • a solid is used as the activator.
  • a solid activator is particularly suitable because it has no appreciable vapor pressure, so that discharge from the deposition process is avoided.
  • the activator can preferably be regenerated or recovered by precipitation in the treatment process. The regeneration of the activator takes place here in particular in the treatment stage, in which also contained in the scrubbing medium sulfur oxides (S0 X ) are separated by reaction with potassium hydroxide solution (KOH) as potassium sulfate (K 2 S0 4 ) from the washing medium.
  • KOH potassium hydroxide solution
  • the activator is dissolved in a solvent and the solution is fed to the washing medium.
  • the activator used does not dissolve instantaneously.
  • the activator is pre-dissolved in an alkaline solvent and this solution is fed to the washing medium.
  • an aqueous KOH solution potassium hydroxide solution
  • the pre-dissolution in an alkaline solvent has the further advantage that the solubility of the activator therein is relatively high, so that only small amounts of solvent must be used.
  • the pre-dissolution of the activator is basically associated with little effort, since the solvents used (water, an alkaline solution or the washing medium) are already present in the deposition process and this must be added regularly during the treatment of the gas stream to the continuously occurring Compensate for water and KOH losses and thus maintain the overall mass balance of the treatment process. Furthermore, by using existing water and KOH streams, for example, it is possible to dispense with an additional supply of solvents in order to pre-dissolve the activator before it enters the processing device or the corresponding preparation process.
  • solvents used water, an alkaline solution or the washing medium
  • the activator used is an oxide of at least one element which is selected from the group consisting of the elements from the third main group (boron group), the fourth main group
  • Carbon group the fifth main group (nitrogen group), the fourth subgroup (titanium group), the fifth subgroup (vanadium group), the sixth subgroup (chromium group) and / or the seventh subgroup (manganese group) of the periodic table.
  • activator B 2 0 3 A1 2 0 3 , Si0 2 , Ge0 2 , P 2 0 3 , As 2 0 3 , Sb 2 0 3 , Se0 2 , Te0 2 , Ti0 2 , V 2 0 5 , Mo0 3 , W0 3 and / or Ge0 2 used.
  • Germanium dioxide (GeO 2 ) is used in particular, which reacts with alkaline solutions, such as with KOH solution used for pre-dissolution of the activator to germanate.
  • the activator is continuously supplied to the washing medium.
  • small amounts of the activator expediently as a solution by predissolving in an alkaline solution, in water or in the washing medium used in the process, flow into the washing medium in the deposition process.
  • the continuous supply of the solution can take place for example by means of a pump in flowing from the absorber sump, loaded with carbon dioxide washing medium.
  • a discontinuous supply of the activator also pre-dissolved in an appropriate solvent, is possible.
  • the solid so the activator prior to dissolution, for example, externally at a
  • Service providers be pre-dissolved. At the processing device itself, only the dosing of the pre-dissolved activator takes place in the washing medium present in the preparation process.
  • the pre-dissolved activator is preferably fed into a discharge line connected to the absorber, through which washing medium laden with carbon dioxide flows into the desorber.
  • the preparation stage for this purpose comprises a reclaimer (SO x - reclaimer), in which a solid mixture of activator and potassium sulfate is precipitated from the washing medium. Potassium sulphate precipitates in the treatment stage or in the SO x reclaimer by the reaction of the sulfur oxides and potassium hydroxide solution contained in the washing medium.
  • the stream entering the reclaimer from the desorber is cooled to temperatures between 10 and 15 ° C.
  • a co-crystallization of the activator used occurs.
  • Ge0 2 crystallizes in the alkaline solvent in the form of germanate.
  • the activator concentration is adjusted to the solubility at the lowest temperature prevailing in the deposition process, which is usually present in the absorber.
  • the absorber temperature is higher than the temperature in the reclaimer and the activator solubility decreases with decreasing temperature falls in the SO x -Reclaimer the fixed-described mixture of activator and potassium sulfate from.
  • the mass ratio of the two crystallized solids is in the range of 1: 1.
  • a separating device In order to separate the precipitated or crystallized solid mixture, ie the mixture of potassium sulfate and the activator to be regenerated from the washing medium, a separating device is expediently used.
  • a separation device for example, is a centrifuge, which allows a simple and effective separation of the solid mixture from the washing medium.
  • the activator regeneration is carried out by means of a method which is based on the utilization of the significantly lower activity compared to potassium sulfate. Tor solubility in water or in dilute aqueous solution is based.
  • the activator is separated from the potassium sulfate by means of a washing process.
  • the washing process is followed by the separation of the solid mixture from the washing medium.
  • the solid mixture of potassium sulfate and activator is preferably washed with washing water to separate the components from one another, wherein the potassium sulfate is essentially completely dissolved in the washing water used.
  • Germanium dioxide (Ge0 2 ) dissolve from this only about 0.4% by weight.
  • a small amount of sulfuric acid is additionally added to the washing water used for the washing process.
  • the amount of washing water used is expediently chosen so that the ratio of the amount of washing water added, based on the amount of potassium sulfate contained in the solid mixture 10: 1, is. Due to the solubility of potassium sulfate of about 10% by weight in water, the entire potassium sulfate contained in the solid mixture dissolves accordingly, while the major part of the activator remains undissolved.
  • germanium dioxide as an activated activator.
  • 1 solid mixture (share K 2 S0 4 and Ge0 2 each 1 kg) is added based on the potassium sulfate, the 10-fold amount of wash water (10 kg), so that due to the solubility of potassium sulfate, the total K 2 S0 4 content of the solid mixture in the washing water dissolves.
  • the germanium dioxide dissolve in the wash water, so that about 960 g of GeO 2 remain as undissolved solid.
  • This low-cost method for recovery or regeneration of the activator can in principle be transferred to all - in particular poorly soluble - activators.
  • the washing medium regenerated in the treatment stage after the precipitation and the subsequent separation of the solid mixture is preferably recycled from the treatment stage or from a reclaimer of the treatment stage into the deposition process.
  • the solid activator not dissolved in the washing water is preferably separated from the washing water in a separation unit. This can be done for example by filtration, wherein the activator is recovered substantially completely.
  • the separated activator is returned to the washing medium - in the deposition process - and is there again to accelerate the treatment of a gas stream available.
  • a post-dosing of activator material is hardly or only to a small extent necessary.
  • a regeneration yield of about 96% of the activator germanium dioxide for example, a subsequent dosing of only about 4% of the activator used is necessary.
  • the regeneration process is also possible with an external service provider if required.
  • the solid mixture precipitated in the preparation stage consisting of potassium sulfate and the activator, can be removed from the process and separated and processed in an external device.
  • the regenerated activator can then be returned to the process.
  • the wash water containing the dissolved potassium sulfate is preferably supplied to a utilization device, where the potassium sulfate is separated from the wash water. Subsequently, the potassium sulfate can be further processed and made available for use, for example, in fertilizers or specialty chemicals.
  • an amino acid salt is used as the washing medium.
  • An aqueous amino acid salt solution is useful here.
  • an amino acid salt having a carbon substituent selected from the group consisting of hydrogen, an alkyl, a hydroxyalkyl and an aminoalkyl More preferably, an amino acid salt having a nitrogen substituent selected from the group consisting of hydrogen, an alkyl, a hydroxyalkyl and a haloalkyl is used.
  • a single amino acid salt such as a potassium salt of glycine or other amino acids, may be employed.
  • mixtures of different amino acid salts can be used as the absorbent.
  • washing medium flows from the desorber into a reboiler.
  • the reboiler supplies the necessary heat of regeneration for the separation of absorbed C0 2 from Washing medium.
  • the loaded washing medium is in this case regenerated by steam, which is generated in the reboiler. To generate the steam within the reboiler this is usually heated with imported steam, for example from a connected steam power plant.
  • the second object of the invention is achieved by a device for the treatment of a gas stream, in particular for the treatment of a flue gas stream comprising an absorber for the separation of carbon dioxide from the
  • a regenerable activator is used to increase the absorption rate of the carbon dioxide in the washing medium and / or the desorption of carbon dioxide from the washing medium.
  • a solid is particularly preferably used as the activator since a solid activator has no appreciable vapor pressure and thus its discharge from the deposition process can be prevented.
  • the activator is expediently used in the form of a solution.
  • the activator is in an alkaline
  • the activator used is an oxide of at least one element which is selected from the group consisting of the elements from the third main group, the fourth main group, the fifth main group, the fourth subsidiary group, the fifth subgroup, the sixth subgroup
  • Such oxides allow effective acceleration of a separation process carried out in the apparatus.
  • the device comprises a metering device for supplying the activator to the deposition process.
  • the supply takes place here preferably continuously.
  • a discontinuous feed of the activator is expedient. Regardless of the type of feed, the activator is pre-dissolved and then fed to the separation process.
  • the preparation stage particularly preferably comprises a reclaimer for precipitating a solid mixture of the activator and potassium sulfate from the washing medium.
  • a separation device is preferably used, wherein, for example, a centrifuge is suitable.
  • the treatment stage comprises a washing device.
  • a washing of the solid mixture can be carried out with a detergent which is only suitable for dissolving potassium sulfate, but not for dissolving the activator used. In this way, a simple and effective separation of the two components from each other can be achieved.
  • Reclaimer is fluidly connected to a supply line of the absorber.
  • the washing medium can be used in the process for the re-absorption and desorption of carbon dioxide.
  • the reclaimer is preferably fluidically connected to a metering device for the activator.
  • the metering device is fluidically connected to a discharge line of the absorber.
  • the activator - either at the beginning of the process or after the regeneration - can thus be added to the washing medium flowing out of the absorber sump and flow together with this into the desorber.
  • an amino acid salt is preferably used as the washing medium.
  • An aqueous potassium-containing amino acid salt solution is useful here.
  • the desorber is expediently connected to a reboiler which, as a bottom evaporator, supplies the necessary regeneration heat for the separation of absorbed CO 2 from the washing medium.
  • 1 shows a device for carrying out a method for the separation of carbon dioxide from a flue gas Ström.
  • the separating device 1 shows a device 1 for separating carbon dioxide from a flue gas stream.
  • the separating device 1 comprises an absorber 3 and a desorber 5 fluidically coupled thereto.
  • the flue gas is introduced into the CO 2 separator 1.
  • the flue gas is supplied to the absorber 3 via a flue gas line 7.
  • a potassium-containing aqueous amino acid salt solution which is used to separate the carbon dioxide contained in the flue gas. This is the
  • the cleaned of carbon dioxide gas stream is discharged from the absorber 3 at the absorber head 11.
  • the absorber 3 is fluidly coupled to a feed line 15 of the desorber 5, so that the laden with carbon dioxide washing medium 9 can be pumped via these two lines 13, 15 with temperature increase by means of a pump 17 in the desorber 5.
  • the loaded washing medium 9 passes through a heat exchanger 19 in which the heat of the regenerated washing medium 9 flowing from the desorber 5 to the absorber 3 is transferred to the laden washing medium 9 flowing out of the absorber 3.
  • the heat exchanger 19 thus uses the waste heat of the desorber 5 to preheat the washing medium 9 from the absorber 3 before entering the desorber 5.
  • the carbon dioxide absorbed in the washing medium 9 is thermally desorbed.
  • the desorber 5 is connected to a discharge line 21, which opens into a recycling device 23.
  • the desorbed C0 2 -rich gas stream can be compressed to allow, for example, the transport to a storage site.
  • a regenerable activator 24 is used.
  • the activator 24 is pre-dissolved in a metering device 25 in potassium hydroxide solution and introduced continuously from the metering device 25 via a metering line 27 into the discharge line 13 of the absorber 3.
  • the pre-dissolved activator 24 thus passes together with the emerging from the absorber 3, loaded with carbon dioxide washing medium 9 in the desorber 5 and is available to accelerate the deposition process available.
  • this also applies that a discontinuous dosage of the pre-dissolved activator 24 in the process is possible.
  • the preliminary resolution then takes place, for example, with an external service provider.
  • only the metering of the pre-dissolved activator 24 into the washing medium 9 used in the process or the device 1 takes place on the device 1 itself.
  • the regeneration or the recovery of the activator 24 takes place in a treatment stage 29, which is fluidically connected to the desorber 5.
  • a return line 31 of the desorber 5 is coupled to a feed line 33 of the treatment stage 25.
  • the feed line 33 is part of a bypass 35.
  • the scrubber 9 freed of carbon dioxide in the desorber 5, in which the dissolved activator 24 is located is fed to the treatment stage 29 via the fluidic coupling of the return line 31 to the feed line 33.
  • the treatment stage 29 comprises a reclaimer 37 in which sulfur oxides contained on the one hand in the washing medium 9 are precipitated out of the washing medium 9 by a drop in temperature and by reaction with potassium hydroxide solution as potassium sulfate. Furthermore, the activator 24 contained in the washing medium 9 is precipitated. The recovery of the activator 24 thus takes place in one process step together with the separation of potassium sulfate formed in the process.
  • the washing medium 9 flowing into the reclaimer 37 from the desorber 5 is cooled to 10 ° C. to 15 ° C., with co-crystallization of the germanium dioxide activator 24 taking place in addition to the crystallization of potassium sulfate. This crystallizes in the form of germanate.
  • the activator 24 and the potassium sulfate are present in a mass ratio of about 1: 1.
  • the solid mixture is then separated from the washing medium 9 by a separating device 39 designed as a centrifuge and finally washed in a corresponding washing device 41 with detergent or washing water.
  • a separating device 39 designed as a centrifuge and finally washed in a corresponding washing device 41 with detergent or washing water.
  • the K 2 S0 4 solubility in water at room temperature about 10 -g. %
  • only a small proportion of activator 24 dissolves in the wash water. With the use of germanium dioxide of this dissolve only about 0.4 wt.%.
  • the amount of washing water used is expediently chosen so that the ratio of the amount of the added wash water, based on the amount of potassium sulfate contained in the solid mixture is 10: 1. Due to the K 2 S0 4 solubility of about 10% in water accordingly dissolves all the potassium sulfate contained in the solid mixture, while most of the activator 24 remains undissolved.
  • the activator 24 is then separated from the washing water in the treatment stage 29 in a further separation process and returned via a discharge line 43 from the processing stage 29 and the reclaimer 37 into the metering device 25.
  • the activator 24 can be returned to the deposition process.
  • the washing medium 9 itself which has been regenerated in the preparation stage 29 after the precipitation and the subsequent separation of the solid mixture, is likewise returned to the preparation process via a return line 45 which is part of the bypass 35.
  • the reclaimer 37 is fluidically connected to a supply line 47 of the absorber 3.
  • the potassium sulfate dissolved in the washing water is preferably fed to a utilization device 49 and there correspondingly separated from the washing water. Subsequently, the potassium sulfate can be further processed and made available for further use, such as in fertilizers or specialty chemicals.
  • a reboiler 51 is connected, which serves to provide the necessary heat of regeneration for the separation of carbon dioxide from the washing medium 9.
  • the loaded washing medium 9 is in this case regenerated by steam, which is generated in the reboiler 51.
  • the reboiler 51 is heated with imported steam, for example from a connected steam power plant, which is not shown here.

Landscapes

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

Abstract

L'invention concerne un procédé de traitement d'un flux de gaz, en particulier de traitement d'un flux de gaz de fumée, selon lequel un flux de gaz est amené dans un absorbeur (3), du dioxyde de carbone contenu dans le flux de gaz est séparé dans l'absorbeur (3) au moyen d'un agent de lavage (9), l'agent de lavage (9) chargé de dioxyde de carbone est amené dans un désorbeur (5), le dioxyde de carbone contenu dans l'agent de lavage (9) est libéré de l'agent de lavage (9) dans le désorbeur (5), l'agent de lavage (9) libéré du dioxyde de carbone dans le désorbeur (5) est amené vers une étape de traitement (29) dans laquelle l'oxyde de soufre contenu dans l'agent de lavage (9) est séparé comme sulfate de potassium et l'agent de lavage (9) épuré à l'étape de traitement (29) est ramené dans l'absorbeur (3). Selon l'invention, un activateur (24) régénérable qui accroît le taux d'absorption du dioxyde de carbone dans l'agent de lavage (9) et/ou le taux de désorption du dioxyde de carbone de l'agent de lavage (9) est introduit dans l'agent de lavage (9). L'invention concerne également un dispositif (1) pour mettre en œuvre un tel procédé.
PCT/EP2014/066740 2013-08-08 2014-08-04 Procédé et dispositif de traitement d'un flux de gaz, en particulier de traitement d'un flux de gaz de fumée Ceased WO2015018796A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102013215677.4 2013-08-08
DE102013215677 2013-08-08

Publications (1)

Publication Number Publication Date
WO2015018796A1 true WO2015018796A1 (fr) 2015-02-12

Family

ID=51266335

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2014/066740 Ceased WO2015018796A1 (fr) 2013-08-08 2014-08-04 Procédé et dispositif de traitement d'un flux de gaz, en particulier de traitement d'un flux de gaz de fumée

Country Status (1)

Country Link
WO (1) WO2015018796A1 (fr)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011120138A1 (fr) * 2010-03-30 2011-10-06 University Of Regina Procédé catalytique et appareil pour séparer un composant gazeux d'un flux de gaz entrant
WO2012062724A2 (fr) * 2010-11-10 2012-05-18 Siemens Aktiengesellschaft Traitement d'un solvant à base amine contaminé par l'introduction d'oxydes de soufre
EP2481469A1 (fr) * 2011-01-31 2012-08-01 Siemens Aktiengesellschaft Solvant, procédé de préparation d'un liquide d'absorption, utilisation du solvant et procédé d'activation d'un solvant
EP2551007A1 (fr) * 2011-07-29 2013-01-30 Siemens Aktiengesellschaft Liquide d'absorption, procédé de fabrication d'un liquide d'absorption, procédé d'activation d'un solvant et utilisation du liquide d'absorption
US20130139695A1 (en) * 2010-09-02 2013-06-06 The Regents Of The University Of California Method and system for capturing carbon dioxide and/or sulfur dioxide from gas stream

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011120138A1 (fr) * 2010-03-30 2011-10-06 University Of Regina Procédé catalytique et appareil pour séparer un composant gazeux d'un flux de gaz entrant
US20130139695A1 (en) * 2010-09-02 2013-06-06 The Regents Of The University Of California Method and system for capturing carbon dioxide and/or sulfur dioxide from gas stream
WO2012062724A2 (fr) * 2010-11-10 2012-05-18 Siemens Aktiengesellschaft Traitement d'un solvant à base amine contaminé par l'introduction d'oxydes de soufre
EP2481469A1 (fr) * 2011-01-31 2012-08-01 Siemens Aktiengesellschaft Solvant, procédé de préparation d'un liquide d'absorption, utilisation du solvant et procédé d'activation d'un solvant
EP2551007A1 (fr) * 2011-07-29 2013-01-30 Siemens Aktiengesellschaft Liquide d'absorption, procédé de fabrication d'un liquide d'absorption, procédé d'activation d'un solvant et utilisation du liquide d'absorption

Similar Documents

Publication Publication Date Title
EP2174700A1 (fr) Absorbant, procédé de fabrication d'un absorbant et utilisation d'un moyen d'absorbant
JP6071838B2 (ja) Ｃｏ２又はｈ２ｓ又はその双方の回収装置及び方法
KR101519900B1 (ko) 육상 플랜트용 탈황 탈질 시스템
EP2145667A1 (fr) Procédé et dispositif de séparation de dioxyde de carbone d'un gaz d'échappement d'une centrale à combustible fossile
EP2964364A1 (fr) Agent absorbant, procédé pour le fabriquer, ainsi que procédé et dispositif de séparation de sulfure d'hydrogène d'avec un gaz acide
CN104338418A (zh) 用于减少能量消耗的碳捕获系统的氨汽提塔
EP2595730B1 (fr) Procédé et dispositif pour préparer une solution de sels d'acides aminés alcaline contaminée
WO2014202448A1 (fr) Procédé pour séparer du dioxyde de carbone d'un courant de gaz, en particulier d'un courant de gaz de combustion, ainsi que dispositif pour séparer du dioxyde de carbone d'un courant de gaz, en particulier d'un courant de gaz de combustion
EP3720815A1 (fr) Procédé pour la fourniture de co2 pour la synthèse de l'urée à partir de fumées et de gaz de synthèse
EP3271046B1 (fr) Procédé et dispositif de désulfuration d'un flux de gaz
EP3104956A1 (fr) Dispositif et procédé de séparation du dioxyde de carbone d'un flux de gaz, en particulier d'un flux de gaz de combustion, comprenant un circuit d'eau de refroidissement
EP3134198B1 (fr) Unité de traitement d'un agent de lavage liquide pollué par des oxydes de soufre et/ou des oxydes d'azote
EP3132840A1 (fr) Procede et dispositif de separation de substances toxiques gazeuses d'un flux gazeux
EP3107637B1 (fr) Procédé et dispositif de séparation du dioxyde de carbone d'un flux de gaz et d'élimination de produits de dégradation dans l'agent de lavage par décomposition par photolyse
EP2941315B1 (fr) Procédé et dispositif servant à la préparation d'un flux de gaz, en particulier d'un flux de gaz naturel
WO2014127980A1 (fr) Dispositif et procédé servant à la préparation d'un flux de gaz, en particulier d'un flux de gaz de fumées
EP2653209A1 (fr) Dispositif de séparation du dioxyde de carbone et son procédé de fonctionnement ainsi qu'unité de séparation
EP2228117B1 (fr) Liquide absorbeur, procédé de fabrication d'un liquide absorbeur, ainsi qu'utilisation d'un liquide absorbeur
WO2018206228A1 (fr) Procédé et dispositif de désulfuration d'un flux gazeux contenant de l'hydrogène sulfuré
EP2640491B1 (fr) Solvant, procédé de préparation d'un liquide d'absorption, utilisation du solvant et procédé d'activation d'un solvant
EP2653210A1 (fr) Installation de combustion avec lavage des fumés et éloignement de CO2 et son procédé de fonctionnement
CN203281225U (zh) 湿式喷淋吸收塔添加有机催化剂烟气脱硫脱汞系统
KR102177534B1 (ko) 이산화탄소로 오염된 아미노산염 용액의 처리를 위한 방법 및 장치
DE102014207851A1 (de) Verfahren sowie Vorrichtungen, insbesondere zur Durchführung des Verfahrens
WO2018202406A1 (fr) Procédé et dispositif de désulfuration d'un flux de gaz contenant de l'hydrogène sulfuré

Legal Events

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

Ref document number: 14747641

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 14747641

Country of ref document: EP

Kind code of ref document: A1