WO2015161978A1 - Procédé et dispositif de traitement d'un milieu de lavage contenant des cations de potassium et/ou des oxydes de soufre - Google Patents

Procédé et dispositif de traitement d'un milieu de lavage contenant des cations de potassium et/ou des oxydes de soufre Download PDF

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Publication number
WO2015161978A1
WO2015161978A1 PCT/EP2015/056362 EP2015056362W WO2015161978A1 WO 2015161978 A1 WO2015161978 A1 WO 2015161978A1 EP 2015056362 W EP2015056362 W EP 2015056362W WO 2015161978 A1 WO2015161978 A1 WO 2015161978A1
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Prior art keywords
potassium
crystallizer
sulfate
container
sulfuric acid
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PCT/EP2015/056362
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German (de)
English (en)
Inventor
Ralph Joh
Markus Kinzl
Ansgar Kursawe
Rüdiger Schneider
Original Assignee
Siemens Aktiengesellschaft
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Publication of WO2015161978A1 publication Critical patent/WO2015161978A1/fr

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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
    • B01D53/1418—Recovery of products
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0004—Crystallisation cooling by heat exchange
    • B01D9/0013—Crystallisation cooling by heat exchange by indirect heat exchange
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0018—Evaporation of components of the mixture to be separated
    • B01D9/0022—Evaporation of components of the mixture to be separated by reducing pressure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/306—Alkali metal compounds of potassium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/50—Inorganic acids
    • B01D2251/506—Sulfuric acid
    • 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 method for processing an aqueous washing medium containing potassium cations and / or dissolved sulfur oxides from a carbon dioxide deposition process of a fossil-fired power plant process.
  • a carbon dioxide-containing flue gas Especially in fossil-fired power plants for the production of electrical energy or heat by combustion of a fossil fuel, a carbon dioxide-containing flue gas.
  • the carbon dioxide must be separated from the flue gas.
  • insbeson ⁇ particular are discussed appropriate measures to existing fossil fired power plants in order to separate after the combustion, the resulting carbon dioxide from the flue gas (post-combustion capture).
  • the carbon dioxide contained in the flue gas With regardwa ⁇ rule by an absorption-desorption process by means of a washing medium or a Ab ⁇ sorption medium from the respective flue gas stream.
  • condition a so-called reclaimer (conditioner) with an SO x recycling stage for removing SO x or sulfates, as well as with a NO x recycling stage for removing NO x , nitrite, nitrate and corresponding secondary products is used.
  • condition a so-called reclaimer
  • the sO x -Reclaimingr in ⁇ play, potassium sulfate in crystalline form, in quirat ⁇ rod, preferably by a cooling crystallization, is deposited.
  • the soluble components are in the
  • the NO x - Reclaimingr ie the NO x -claimer
  • the NO x - Reclaimingr is used for the recovery of the active component of the washing medium, so for example an amino acid salt.
  • the washing medium is thickened in egg ⁇ ner evaporation stage and pumped from there into a crystallizer of the NO x -claimer.
  • the Aminoklaresalzanion is crystallized out as a solid. Soluble secondary constituents are separated off as waste and fed to appropriate disposal.
  • the first object of the invention is to provide an improved process for preparing a washing solution containing potassium cations for an absorption desorption process as described above.
  • the second object is to provide a device which especially since ⁇ is suitable to perform the method described above.
  • the first object is achieved by the indication of a method for preparing a potassium cations and / or dissolved sulfur oxides-containing aqueous wash medium from a carbon deposition process of a fossil-fired power ⁇ plant process, wherein a generator operated as a cooling or Verdampfungskris ⁇ tallisator container for the separation of Potassium sulfate is provided, and wherein in the cooling or evaporation crystallizer operated container
  • Potassium sulfate is provided. According to the invention, it was recognized that the ion equilibrium of the amino acid salt washing solutions used can be shifted in the direction of potassium cations. This can be caused by the following reasons: On the one hand, gas power plant fumes lead to increased degradation of the amino acid salt due to increased oxygen and NOx concentrations, eg via oxidative mechanisms. This degradation always affects only the amino acid salt anion, but not the potassium cation. Since the NOx reclaimer emits some of the degradation products to a greater extent than the Ka ⁇ liumkationen potassium cations, while both ions are added via the refill stream in the preferred stoichiometric ratio, it comes over time to a potassium cation excess. These relationships were experimentally confirmed by experiments with a gas burner exhaust gas.
  • the invention can be carried out without additional apparatus with the existing equipment.
  • the method is like potassium surpluses and potassium lower wefts by conversion to a commercially viable product from by an as cooling or Ver ⁇ dampfungskristallisator operated container for the deposition is provided by potassium sulphate, and in which operated as a cooling or evaporative crystallizer vessel a classifier for retaining the formed Potassium sulfate is provided.
  • Sulfur oxides have a very limited solubility in aqueous amino acid salt solutions with a few grams per kilogram.
  • the container operated as a cooling or evaporating crystallizer determines the solubility limit of the lowered and exceeded medium dissolved sulfate. Therefore, crystal growth takes place on the potassium sulfate crystals retained by the classifier, and dissolved potassium sulfate is depleted of the washing medium in the form of solid.
  • the separation of the potassium sulfate particles formed is carried out according to their particle size. This classifier offers several advantages.
  • particle-free wash medium is discharged from the Kristallisati ⁇ ons livinger for further processing, thus only small amounts of potassium sulfate get back into the process.
  • the container is introduced into the container at a step stöchiomet ⁇ potassium cation excess sulfuric acid.
  • the sulfuric acid is configured as dilute sulfuric acid.
  • the washing solution preferably contains
  • Amino acid salt anions wherein the addition rate of sulfuric acid on the basis of the ratio of the potassium cations to the amino acid salt ⁇ anions takes place.
  • dilute sulfuric acid solid potassium sulfate is produced in the crystallization vessel, which is a valuable product for the fertilizer and specialty chemical industries.
  • the invention has as a further advantage that the high selectivity of the SOx reclaimer, ie the elimination of potassium sulfate of high purity and the recycling of the regenerated solvent in the main process, is not affected by the proposed method.
  • the educt costs are compared with the yields that can be achieved for the potassium sulphate obtained, there is another advantage: the yields which can be achieved for a given amount of K 2 SO 4 exceed the costs which have to be borne for the corresponding amount of sulfuric acid. by a factor of about five. Also, the inventive method is characterized by good controllability.
  • potassium hydroxide is introduced into the crystallization vessel at a stoichiometric potassium deficiency.
  • the Ka is designed liumhydroxid as aqueous potassium hydroxide diluted from ⁇ .
  • the washing solution also contains amino acid salt anions and the addition rate of potassium hydroxide he ⁇ follows on the basis of the ratio of potassium cations to the amino acid salt anions. The ratio of potassium cations-potassium cations is preferred to Aminoklaresalz- anions by ion chromatography in conjunction with egg ⁇ ner titration with hydrogen chloride (HCl) was determined.
  • the inventive method is characterized by good controllability.
  • Preference in the classifier sulfate crystals passerge- is where the potassium sulfate in solution grows ⁇ .
  • potassium cation excesses or SOx collected in the washing medium can be converted into the commercially utilizable potassium sulfate in the form of dissolved sulfate, it being necessary to add only the inexpensive sulfuric acid or the aqueous dilute potassium hydroxide solution as educt.
  • an evaporation crystallizer is provided as the crystallizer, and the lowering and exceeding of the solubility limit of the sulfate is accomplished in the washing solution by lowering the water content.
  • ⁇ if a cooling crystallizer is provided as a crystallizer and the reduction and exceeding the solubility limit of the sulfate in the washing solution is effected by lowering the temperature.
  • the concentration of the dissolved Sulfate by addition of dilute sulfuric acid with the simultaneous presence of sulfate crystals increases. Gleichzei ⁇ tig the solubility limit of the sulfate is reduced by the procedural ⁇ ren and exceeded.
  • the cooling crystallizer this is done by lowering the temperature in the evaporation crystallizer by lowering the water content.
  • the potassium sulfate crystals already present as solids grow.
  • the innovative, inventive method is characterized by good controllability.
  • the rate at which potassium hydroxide must be added with the sulfur acid ⁇ / can be calculated using the present process in the main ratio of potassium cations and Aminoklaesalzanionen.
  • the concentrations of both ions can be monitored analytically. Due to the slow change in the ion ratio, the analyzes can be carried out offline or online.
  • the second object is achieved by specifying a forward direction for preparing a potassium cations and / or dissolved sulfur oxides-containing aqueous washing medium from egg ⁇ nem carbon deposition process of a fossil-fired power plant process, whereby a cooling or evaporative ⁇ crystallizer operated container for the separation of Kali is provided umsulfat, wherein the cooling or evaporating crystallizer operated container via a
  • the container is provided in a first apparatus comprising an evaporation stage for Aufkonzen ⁇ tration of the active component of the washing medium with a Ver ⁇ steamer and / or with a heat exchanger, and a the evaporator and / or the heat exchanger connected collecting container as a container, wherein the Collecting container over the Evaporator and / or via the heat exchanger, the potassium cations and / or dissolved sulfur oxides containing aqueous Waschme ⁇ dium is fed, and wherein in the liquor operated as Verdampfungskristal- lisator at a stoichiometric excess calsium sulfuric acid and stoichiometric Kali ⁇ deficiency potassium hydroxide can be supplied, whereby crystallized out at least Ka ⁇ liumsulfat.
  • a first apparatus comprising an evaporation stage for Aufkonzen ⁇ tration of the active component of the washing medium with a Ver ⁇ steamer and / or with a
  • the washing medium for concentrating its active component of an evaporation stage with an evaporator and / or with a heat exchanger, as well as with a fluidically connected to the evaporator and / or the heat exchanger is supplied to the collecting vessel via the evaporator and / or via the heat exchanger, the potassium cations and / or sulfur-containing aqueous washing ⁇ medium is supplied and wherein the potassium sulfate is fed from a collecting container of a separation unit.
  • the separation ⁇ unit is the solid-liquid separation, the withdrawn from the collecting container or the crystallizer suspension.
  • the device is particularly suitable for carrying out the method as described above.
  • the container is provided in a second device for processing a potassium cations and / or sulfur oxides-containing aqueous wash medium consists of a carbon dioxide-deposition process of a fossil fuel-fired Krafttechnikpro ⁇ zesses comprising a condenser, a crystallizer as a container, wherein the crystallizer on the one hand via the cooler the washing medium containing potassium cations or dissolved sulfur oxides can be supplied, and in the container operated as a cooling crystallizer, sulfuric acid can be fed in at a stoichiometric excess of potassium and potassium hydroxide can be fed in the case of stoichiometric potassium deficiency, as a result of which at least potassium sulfate crystallizes out.
  • a second device for processing a potassium cations and / or sulfur oxides-containing aqueous wash medium consists of a carbon dioxide-deposition process of a fossil fuel-fired Krafttechnikpro ⁇ zesses comprising a condenser
  • a filter is provided, said crystals from the crystallizer ⁇ sationsreaktor potassium sulfate, especially potassium sulfate, in the filter is ausleitbar / are, and a recycled washing medium of the potassium sulphate is separated by the filter.
  • the second device is also particularly suitable for carrying out the method as described above.
  • FIG. 2 shows the second apparatus for processing a potassium cation or sulfur oxide-containing washing solution.
  • the apparatus for processing comprises an evaporation stage 2 with an evaporator 3 designed as a thin-film evaporator for thickening the washing medium contained by concentrating the active component of the washing medium, and with a collecting container 7 connected to the evaporator 3.
  • Such a collecting container 7 is basically used in the treatment of washing medium in a NO x recyclable in which it serves as a reservoir or as a pump template for a washing medium which can be fed to a crystallizer of the NO x reclaimer.
  • the collecting container 7 of the processing apparatus is formed as a crystallizer 9 for removing sulfur oxides from the washing medium by crystallization of potassium sulfate.
  • the crystallizer 9 is defined against ⁇ dimensioned larger than previously used collection vessels, and optionally, but not necessarily equipped with a stirrer 10th
  • the supply of the washing medium in the crystallizer 9 from ⁇ formed collecting container 7 is carried out starting from a desorption unit, not shown, a separator for carbon dioxide. Starting from the desorption unit, a sulfate-rich input stream 11 containing about 30% by weight of an active component of the washing medium is used
  • the input current 11 has an inlet temperature between 30 ° C and 40 ° C, whereas ⁇ gen the temperature in the collecting container 7 is between 60 ° C and 65 ° C.
  • ⁇ gen the temperature in the collecting container 7 is between 60 ° C and 65 ° C.
  • potassium excesses are now compensated by conversion into a commercially utilizable product.
  • a supply line 100 is also connected for the supply of sulfuric acid.
  • the concentration of the dissolved sulfate by the addition of dilute sulfuric acid with the simultaneous presence of Sulfate crystals increased.
  • the solubility limit of the sulfate ⁇ is lowered by the method and ⁇ steps. In the evaporation crystallizer this is done by lowering the water content. Exceeding the solubility limit causes the potassium sulfate crystals already present as solids to grow.
  • potassium sulfate formed grows after the addition of sulfuric acid to existing K 2 SO 4 crystals.
  • the suitable place for the addition is the crystallizer 9, in which suspended K 2 S0 4 crystals are present.
  • potassium cation excesses can be converted into the commercially utilizable potassium sulfate, wherein only the kos ⁇ ten réellee sulfuric acid must be added as starting material.
  • potassium hydroxide can also be added via a feed line 101.
  • the crystallizer 9 comprises a
  • Classifying device 13 which allows separation of the crystallized in the crystallization chamber 12 potassium sulfate particles according to their particle size.
  • the classifier 13 is formed inside the crystallizer 9 in the form of a classification zone 14 with a first Klas ⁇ sier Colour 15 and a second Klassier Scheme sixteenth In the first classifier ⁇ area 15 accumulate substantially medium and small size potassium sulfate particles, the large potassium sulphate particles are preferably discharged.
  • the collecting container 7 and the evaporator 3 thus represent an evaporative crystallizer with internal classification function.
  • a first partial flow 17 is supplied with the wash medium ⁇ means of a pump 19 from the holding tank 7 as a hy- rozyklon formed separation unit 21st
  • the first Klassier Scheme 15 is gekop pelt ⁇ via the outlet 22 of the collecting container 7 with an inlet 23 of the separation unit 21st
  • the first substream 17 essentially comprises the medium and small potassium sulfate particles which are present in the
  • Classifying zone 15 of the crystallizer 9 have been separated from the heavy Parti ⁇ cle.
  • the invention is characterized by good controllability.
  • the rate must be added with the H 2 SO 4 / KOH can be calculated using the present process in the main relationship between Kaliumka ⁇ functions and amino acid salt anions.
  • the concentrations of both ions can be followed analytically. Due to the slow change in the ion ratio, the analyzes can be carried out offline or online.
  • the supersaturation of the washing medium then breaks down by the crystallization of potassium sulfate in the crystallizer 9.
  • the crystallizer 9 is formed with a crystallization ⁇ chamber 12.
  • a second partial stream 25 enriched with potassium sulphate particles from the second classifying area 16 is supplied from the collecting container 7 to a recycling device 29 by means of a pump 27 designed as a sump pump.
  • a pump 27 designed as a sump pump.
  • the medium and small particles of potassium sulfate contained in the first partial flow 17 are separated from the washing medium.
  • Underflow 30, which is Liquid separation is formed containing the separated from the wash medium potassium sulfate particles, which are then fed via a Kopp ⁇ treatment of the outlet 31 of the separation unit 21 with an inlet 32 of the collecting container 7 as crystal nuclei again the crystallization process.
  • a first substream 33 of the resulting in this solid-liquid separation upper run 34, ie a low-particle clear flow is then from an outlet 35 of the separation unit 21 by means of a pump 36 an additional crystallizer 37 for recovering the active component of the washing medium supplied ⁇ leads.
  • the crystallizer 37 is formed as a crystallizer for the NO x recycling process.
  • the separation unit 21 gekop ⁇ pelt with the evaporator 3.
  • the coupling takes place via the outlet 35 of the separation unit with an inlet 38 of the evaporator 3.
  • a second partial stream 39 of the upper run 34, the main stream, can be returned to the evaporator 3 and there for the purpose of concentration of the active component of the washing medium water from this discharging.
  • a third partial flow 41 of the upper run 34 of the separation unit 21 is supplied by means of a pump 43 to an absorber unit, not shown, of a carbon dioxide separation device.
  • the outlet 35 of the separation unit 21 with egg ⁇ nem not shown inlet of the absorber unit is coupled.
  • a metering device 45 is connected to the collecting container 7 designed as a crystallizer 9.
  • the metering device 45 comprises two pumps 47, 49, by means of which additional reactants (sulfuric acid / potassium hydroxide) are fed to the system to prevent undesirable potassium cations concentration, for example, in gas power plant applications, or alternatively unwanted potassium cation depletion, for example, in coal power plant applications.
  • the device shows a second apparatus for processing a contaminated solvent 51 for carbon dioxide.
  • the device essentially comprises a crystallizer 60, a filter 61, a cooler 62, and a heat exchanger 63.
  • the crystallizer 60 has a contaminated solvent supply line 57. In the supply line 57, the heat exchanger 63 and the radiator 62 are connected. To the crystallizer 60, there is also connected a supply pipe 100 for supplying the sulfuric acid and a supply pipe 101 for supplying potassium hydroxide.
  • a metering apparatus having two pumps 47, connected 49 by means of which the additional reactant sulfuric acid / potassium hydroxide is added to the system Kgs ⁇ nen to an undesirable concentration of Kaliumka ⁇ functions, for example in low-sulfur flue gases (Gas power plant application) or alternatively to prevent unwanted depletion of potassium cations, for example, in sulfur-rich flue gases (coal power plant application).
  • the concentration of the dissolved sulfate is increased by adding dilute sulfuric acid or aqueous potassium hydroxide solution with the simultaneous presence of sulfate crystals.
  • the solubility limit of the sulfate is lowered and exceeded by the process. In the cooling crystallizer this is done by lowering the temperature. Exceeding the solubility limit increases the potassium sulfate crystals already present as solids, which are provided by the classifier for the retention of the potassium sulfate particles formed.
  • Ausurgid the crystallizer 60 is connected via a suspension ⁇ line 80 with the filter 61st
  • the filter For discharging a crystalline solid, the filter is followed by a container 90.
  • a line 56 is connected to the filter 61, which is connected to the heat exchanger 63rd
  • heat from the contaminated solvent 51 to the treated solvent 53 is transferable through the heat exchanger 63.
  • the heat exchanger 63 is optional, and in particular in di rect ⁇ integration of the device in a carbon dioxide separation apparatus is advantageous.
  • the invention has the following advantages: The potassium excesses are not converted into a waste stream, but into the commercially utilizable product potassium sulfate. Furthermore, the high selectivity of the crystallizer 60 (FIG. 2), 9 (FIG. 1), in particular the discharge of potassium sulfate with high purity and the recycling of the regenerated solvent into the main process, are not impaired by the invention. If the educt costs are compared with the recoverable for the product Ka ⁇ liumsulfat achievable, so there is another advantage: The achievable for a given amount of K 2 SO 4 revenues exceed the costs that are incurred for the appropriate amount of sulfuric acid by a factor of five.
  • the ge ⁇ suitable place for the addition of the sulfuric acid is the crystallization Lizer 60 (FIG 2), 9 ( Figure 1), in which suspended K 2 S0 4 - crystals are present at which the secreting potassium sulfate can grow.
  • the separation of the potassium sulfate is carried out with the aid of the separation apparatuses present in the crystallizer 60 (FIG. 2), 9 (FIG. 1).
  • the proposed process variant is characterized by good controllability.
  • the rate of addition must be added to ⁇ with the H 2 SO 4 can be calculated through the process in the main tillen- de ratio of potassium cations and anions Aminoklaresalz-.
  • the concentrations of both ions can be monitored by standard analytical techniques. Due to the slow change of the ion ratio , these analyzes can be carried out offline or online.
  • KOH potassium hydroxide
  • KOH potassium hydroxide

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Treating Waste Gases (AREA)

Abstract

L'invention concerne un procédé de traitement d'un milieu de lavage aqueux, contenant des cations de potassium et/ou des oxydes de soufre dissous, issu d'un processus de séparation de dioxyde de carbone lors du fonctionnement d'une centrale utilisant des combustibles fossiles. Pour séparer le sulfate de potassium, on utilise une cuve faisant office de cristalliseur par refroidissement ou par évaporation et, pour retenir les particules de sulfate de potassium formées, on utilise un équipement classeur disposé dans la cuve faisant office de cristalliseur par refroidissement ou par évaporation. L'invention concerne en outre un dispositif correspondant.
PCT/EP2015/056362 2014-04-25 2015-03-25 Procédé et dispositif de traitement d'un milieu de lavage contenant des cations de potassium et/ou des oxydes de soufre WO2015161978A1 (fr)

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DE102014207851.2 2014-04-25
DE102014207851.2A DE102014207851A1 (de) 2014-04-25 2014-04-25 Verfahren sowie Vorrichtungen, insbesondere zur Durchführung des Verfahrens

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113144660A (zh) * 2021-02-05 2021-07-23 成都思达能环保设备有限公司 一种结晶方法及系统
CN117427365A (zh) * 2023-12-20 2024-01-23 福建铭麟科技有限公司 一种过硫酸钾制备工艺及制备装置

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US3208834A (en) * 1960-01-26 1965-09-28 Hertha M Schulze Method and apparatus for crystallizing and classifying
US4389383A (en) * 1980-05-27 1983-06-21 Union Carbide Corporation Regenerable process for the selective removal of sulfur dioxide from effluent gases
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
EP2653209A1 (fr) * 2012-04-18 2013-10-23 Siemens Aktiengesellschaft Dispositif de séparation du dioxyde de carbone et son procédé de fonctionnement ainsi qu'unité de séparation

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3485581A (en) * 1966-11-15 1969-12-23 Wellman Lord Inc Process for recovering sulfur dioxide from gases containing same
WO2012030630A1 (fr) * 2010-09-02 2012-03-08 The Regents Of The University Of California Procédé et système pour capturer le dioxyde de carbone et/ou le dioxyde de soufre contenus dans un flux gazeux

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3208834A (en) * 1960-01-26 1965-09-28 Hertha M Schulze Method and apparatus for crystallizing and classifying
US4389383A (en) * 1980-05-27 1983-06-21 Union Carbide Corporation Regenerable process for the selective removal of sulfur dioxide from effluent gases
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
EP2653209A1 (fr) * 2012-04-18 2013-10-23 Siemens Aktiengesellschaft Dispositif de séparation du dioxyde de carbone et son procédé de fonctionnement ainsi qu'unité de séparation

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113144660A (zh) * 2021-02-05 2021-07-23 成都思达能环保设备有限公司 一种结晶方法及系统
CN117427365A (zh) * 2023-12-20 2024-01-23 福建铭麟科技有限公司 一种过硫酸钾制备工艺及制备装置
CN117427365B (zh) * 2023-12-20 2024-03-15 福建铭麟科技有限公司 一种过硫酸钾制备工艺及制备装置

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