DE3447494A1 - Multiple-stage simultaneous separating out of SO2 and NOx, the untreated gas being first introduced into a co-current stage - Google Patents

Multiple-stage simultaneous separating out of SO2 and NOx, the untreated gas being first introduced into a co-current stage

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Publication number
DE3447494A1
DE3447494A1 DE19843447494 DE3447494A DE3447494A1 DE 3447494 A1 DE3447494 A1 DE 3447494A1 DE 19843447494 DE19843447494 DE 19843447494 DE 3447494 A DE3447494 A DE 3447494A DE 3447494 A1 DE3447494 A1 DE 3447494A1
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Germany
Prior art keywords
redox potential
nozzle
stage
nox
washer
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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
DE19843447494
Other languages
German (de)
Inventor
Heribert Dipl.-Ing. 4390 Gladbeck Dewert
Heinrich Ing.(grad.) 4600 Dortmund Gresch
Heinz Dipl.-Ing. Hölter
Heinrich Dipl.-Ing. 4390 Gladbeck Igelbüscher
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Individual
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Individual
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 Individual filed Critical Individual
Priority to DE19843447494 priority Critical patent/DE3447494A1/en
Priority to PCT/EP1985/000018 priority patent/WO1985003238A2/en
Priority to AU38857/85A priority patent/AU569775B2/en
Priority to EP85900664A priority patent/EP0168453A1/en
Priority to US06/781,235 priority patent/US4670234A/en
Priority to IT19231/85A priority patent/IT1199650B/en
Publication of DE3447494A1 publication Critical patent/DE3447494A1/en
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
    • 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

Abstract

The invention relates to a process for the simultaneous separating out of SO2 and NOx using a co-current scrubber and/or a downstream counter-current scrubber. In order to achieve the largest possible simultaneous separating off of SO2 and NOx, according to the invention it is proposed that the co-current scrubber (2), into which the untreated gas is first introduced, is operated in the first nozzle plane (22) using a scrubbing liquid which, charged with negative redox potential via an iron reactor (3), is first contacted with the gas stream and then in the downstream nozzle planes (23), a cleavage of the bound NO - NO2 from the region of the nozzles (22) to form elemental nitrogen proceeds. A scrubbing liquid is fed to the iron reactor (3) which scrubbing liquid is adjusted to a negative redox potential by reducing agents. <IMAGE>

Description

Beschreibung und Erläuterung zur Zusatzpatent-Description and explanation of the additional patent

anmeldung "Mehrstufige simultane 502 und NO##Abscheidung, wobei das rohgas zuerst in eine Gleichstromstufe eingeführt wird" Zusatz zu P 34 40 782.0 In der Hauptanmeldung P 34 40 782.0 wird beschrieben, daß das Rohgas zuerst einer Gleichstromwaschstufe zugeführt wird, und die Waschflüssigkeit aus dem Ablauf der ersten Waschstufe über einen Eisenreaktor (3) mit einem Minus-Redoxpotential eingestellt, wie aus der Zeichnung ersichtlich, zuerst mit dem Rohgas kontaktiert wird.registration "multi-stage simultaneous 502 and NO ## separation, whereby the Raw gas is first introduced into a cocurrent stage "Addition to P 34 40 782.0 In the main application P 34 40 782.0 it is described that the raw gas is first one Co-current washing stage is supplied, and the washing liquid from the drain of the first washing stage set via an iron reactor (3) with a minus redox potential, As can be seen from the drawing, the raw gas is first contacted.

Die zweite Waschdüsenebene wird mit der Pumpe (8) beschickt mit einem Redoxpotential, das schwächer ist als die oberste Düsenebene.The second washing nozzle level is fed with a pump (8) Redox potential that is weaker than the topmost nozzle level.

Der Gegenstromwäscher (4), der alkalischer betrieben wird, fährt mit der Pumpe (9) im eigenen Kreislauf unter Zugabe von Natriumdithionit oder sonstigen Reduktionsmitteln aus dem Behälter (11).The countercurrent washer (4), which is operated more alkaline, also moves the pump (9) in its own circuit with the addition of sodium dithionite or other Reducing agents from the container (11).

Erfindungsgemäß wird durch weitere Verfahrensschritte der simultane S02- und NO##Abscheider#?rozeß entsprechend den nachstehenden und in der beiliegenden Zeichnung dargestellten Merkmalen verbessert.According to the invention, the simultaneous S02 and NO ## separator process according to the following and the enclosed Characteristics shown in the drawing improved.

In der beiliegenden Zeichnung ist dargestellt: mit (1) der sogenannte Vorwäscher, der zur Chlorabscheidung dient bei chlorreicher Kohle; mit (2) die Waschstufe, die sauer betrieben wird vorzugsweise im Bereich zwischen pH 3 und pH 4; mit (3) ein Eisenreaktor über den die Flüssigkeit aus dem sauren Waschkreislauf gefördert wird; mit (4) die zweite Waschstufe, die vorzugsweise alkalischer, d.h. mit einem etwas höheren pH-Rert größer 5 betrieben wird als die Waschstufe eins, die mit (2) bezeichnet ist; mit (5) ein Tropfenabscheider hinter der zweiten Waschstufe (4); mit (6) ein Dekanter, der einen Teil der Waschflüssigkeit aus der zweiten Waschkreislaufstufe (4) reinigt, um sie dem Tropfenabscheider zur Spülung zuzuführen; mit (7) die Waschflüssigkeitsabgabe zur Gipsentwässerung (Zentrifuge oder Bandfilter); mit (8) eine Kreislaufpumpe für den Waschkreislauf (2); mit (9) die Waschflüssigkeitspumpe für den Wäscher (4), zweite Waschstufe für den Kreislauf mit einem pH-Wert größer pH 5, wobei eine Teilmenge über den Dekanter (6) geführt wird, um den Feststoff (Gips) auszutragen; mit (10) der Kalkstein- oder der Kalkhydratanmischbehälter; mit (11) der Behälter für Natriumdithionit, Ascorbinsäure oder ein gleichwertiges Reduktionsmittel; mit (12) ist dargestellt die Zugabe von Natriumdithionit bzw. Ascorbinsäure oder ein gleichwertiges Reduktionsmittel, das der Waschflüssigkeit vor dem Eisenreaktor (3) zugegeben wird, wobei vorzugsweise diese Zugabe nur für die Anfahrphase erfolgt bis daß der Reaktor (3) das vorgegebene Redoxpotential ohne Reduktionsmittel aufrechterhält.The attached drawing shows: with (1) the so-called Pre-scrubber, which is used to separate chlorine from chlorine-rich coal; with (2) the washing level, the acidic operation is preferably carried out in the range between pH 3 and pH 4; with (3) an iron reactor through which the liquid is pumped out of the acidic washing cycle will; with (4) the second washing stage, which is preferably more alkaline, i.e. it is operated with a slightly higher pH value greater than 5 than the washing stage one indicated by (2); with (5) a mist eliminator behind the second Washing stage (4); with (6) a decanter that removes part of the washing liquid from the second washing cycle stage (4) cleans it to the droplet separator for rinsing to feed; with (7) the washing liquid delivery for gypsum drainage (centrifuge or band filter); with (8) a circulation pump for the washing circuit (2); with (9) the washing liquid pump for the washer (4), second washing stage for the circuit with a pH value greater than pH 5, a portion of which is passed through the decanter (6) is to discharge the solid (gypsum); with (10) the limestone or the hydrated lime mixing tank; with (11) the container for sodium dithionite, Ascorbic acid or an equivalent reducing agent; with (12) is shown the addition of sodium dithionite or ascorbic acid or an equivalent reducing agent, which is added to the washing liquid upstream of the iron reactor (3), preferably this addition takes place only for the start-up phase until the reactor (3) has reached the specified level Maintains redox potential without reducing agents.

Weiterhin wird eine Teilmenge der Pumpe (9) in den Bereich der Pumpe (14) zugegeben.Furthermore, a subset of the pump (9) is in the area of the pump (14) added.

Mit (15) ist die Waschflüssigkeitsmenge bezeichnet.The amount of washing liquid is denoted by (15).

Eine Teilmenge der Waschflüssigkeit aus dem Kalksteinanmischbehälter (10) wird einer Elektrolysestation (13) zugegeben.Part of the washing liquid from the limestone mixing tank (10) is added to an electrolysis station (13).

Von der Elektrolysestation (13) wird eine mit entsprechendem negativen Redoxpotential aufgearbeitete Waschflüssigkeit (16) in den Bereich des Eisenreaktors (3) - Leitung mit (17) bezeichnet - und/oder in den Bereich des Gegenstromwäschers (4) - mit (18) bezeichnet -zugeführt.The electrolysis station (13) has a corresponding negative Redox potential processed Washing liquid (16) in the area of the iron reactor (3) - line denoted by (17) - and / or in the area of the Countercurrent scrubber (4) - labeled (18) - supplied.

Es ist durchaus möglich, daß auch aus dem Behälter (11), der mit Reduktionsmitteln angefüllt ist, Teilmengen zur Elektrolysestation (13) übergeben werden können, so daß durch Reduktionsmittel und Elektrolyse eine sehr schnelle Reaktion zum Einstellen des Reduktionspotentials geleistet werden kann und über eine weitere Pumpe (19) das konzentrierte negative Redoxpotential in der Waschflüssigkeit der Düsenebene (20) zugeführt wird.It is entirely possible that from the container (11) that with reducing agents is filled, partial quantities can be transferred to the electrolysis station (13), so that by reducing agents and electrolysis a very fast response to setting of the reduction potential can be achieved and another pump (19) the concentrated negative redox potential in the washing liquid of the nozzle level (20) is supplied.

Diese Düsenebene ist die letzte im Waschsystem, um hier das noch nicht abgeschiedene NO und S02 an die Waschflüssigkeit anzulagern, um sie der darunterliegenden Düsenebene (21) zuzuleiten und hier elementaren Stickstoff N2 freizusetzen.This nozzle level is the last one in the washing system, so that's not the case here deposited NO and SO2 to attach to the scrubbing liquid to make them the underlying To supply nozzle level (21) and to release elemental nitrogen N2 here.

Durch die oben beschriebenen erfindunffsemäßen Anordnungen ist eine größtmögliche simultane Ausscheidung von S02 und NOx gewährleistet.With the above-described arrangements according to the invention, a greatest possible simultaneous elimination guaranteed by S02 and NOx.

Mit (22) ist die Düsenebene im Gleichstromwäscher dargestellt; mit (23) die nachgeschalteten Düsenebenen.With (22) the nozzle plane is shown in the direct current washer; with (23) the downstream nozzle levels.

Zusatz-Patentansprüche:Additional claims:

Claims (1)

Zusatz-Patentansprüche: Anspruch 1 Verfahren zur simultanen S02- 2und NO##Abscheidung mit einem Gleichstromwäscher und/oder nachgeschaltetem Gegenstromwäscher dadurch gekennzeichnet, daß der Gleichstromwäscher, in den das Rohgas zuerst hineingeführt wird, in der ersten Düsenebene (22) mit einer Waschflüssigkeit betrieben wird, die über einen Eisenreaktor mit negativem Redoxpotential aufgeladen dem Gasstrom zuerst kontaktiert wird, und dann in den nachgeschalteten Düsenebenen (23) eine Abspaltung des gebundenen NO - NO, aus dem Bereich der Düsen (22) zu elementaren Stickstoff erfolgt.Additional claims: Claim 1 method for simultaneous S02-2und NO ## Separation with a cocurrent washer and / or downstream countercurrent washer characterized in that the direct current scrubber into which the raw gas is first introduced is operated in the first nozzle level (22) with a washing liquid which The gas flow is charged first via an iron reactor with negative redox potential is contacted, and then in the downstream nozzle levels (23) a cleavage of the bound NO - NO, from the area of the nozzles (22) to elemental nitrogen he follows. Anspruch 2 Verfahren nach Anspruch 1 dadurch gekennzeichnet, daß dem Eisenreaktor (3) eine Waschflüssigkeit zugeführt wird, die durch Reduktionsmittel aus dem Behälter (11) auf ein negatives Redoxpotential eingestellt wird.Claim 2 The method according to claim 1, characterized in that the Iron reactor (3) is supplied with a washing liquid, which is reduced by reducing agents is set to a negative redox potential from the container (11). Anspruch 3 Verfahren nach Anspruch 1 - 2 dadurch gekennzeichnet, daß die Düsenebene, die als letzte im Waschprozeß eingesetzt wird, mit einer Waschflüssigkeit beaufschlagt wird, die ein negatives Redoxpotential hat, das vorzugsweise über Reduktionsmittel aus dem Behälter (11) und/oder aus der Elektrolysestation (13) gesteuert ist.Claim 3 Method according to Claim 1 - 2, characterized in that the nozzle level, which is used last in the washing process, with a washing liquid is applied, which has a negative redox potential, which is preferably via reducing agent is controlled from the container (11) and / or from the electrolysis station (13). Anspruch 4 Verfahren nach Anspruch 1 - 3 dadurch gekennzeichnet, daß die Düsenebenen (21) im Gegenstromwäscher und die Düsen (23) im Gleichstromwäscher ein kleineres Minus-Redoxpotential aufweisen als die Düsenebenen (20) und (22).Claim 4, method according to claims 1-3, characterized in that the nozzle levels (21) in the countercurrent washer and the nozzles (23) in the cocurrent washer have a lower minus redox potential than the nozzle planes (20) and (22). Anspruch 5 Verfahren nach Anspruch 1 - 4 dadurch gekennzeichnet, daß die Einstellung des Redoxpotentials über den. Eisenreaktor (3) und wahlweisen Einsatz von Reduktionsmitteln (11) wie Natriumdithionit und/oder Elektrolyse (13) erfolgt.Claim 5, method according to claims 1-4, characterized in that the setting of the redox potential via the. Iron reactor (3) and optional insert of reducing agents (11) such as sodium dithionite and / or electrolysis (13) takes place.
DE19843447494 1984-01-25 1984-12-27 Multiple-stage simultaneous separating out of SO2 and NOx, the untreated gas being first introduced into a co-current stage Ceased DE3447494A1 (en)

Priority Applications (6)

Application Number Priority Date Filing Date Title
DE19843447494 DE3447494A1 (en) 1984-12-27 1984-12-27 Multiple-stage simultaneous separating out of SO2 and NOx, the untreated gas being first introduced into a co-current stage
PCT/EP1985/000018 WO1985003238A2 (en) 1984-01-25 1985-01-23 Process for stripping nitrogen oxides and sulphur oxides as well as optionally other noxious elements of flue gas from combustion plants
AU38857/85A AU569775B2 (en) 1984-01-25 1985-01-23 Stripping nox and sox from flue gases discharged from combustion plants
EP85900664A EP0168453A1 (en) 1984-01-25 1985-01-23 Process for stripping nitrogen oxides and sulphur oxides as well as optionally other noxious elements of flue gas from combustion plants
US06/781,235 US4670234A (en) 1984-01-25 1985-01-23 Process for stripping nitrogen oxides and sulphur oxides as well as optionally other noxious elements of flue gas from combustion plants
IT19231/85A IT1199650B (en) 1984-01-25 1985-01-25 PROCEDURE FOR THE SEPARATION OF NITROGEN OXIDES AND SULFUR OXIDS AND EVENTUALLY OF OTHER HARMFUL SUBSTANCES FROM THE COMBUSTION GASES OF COMBUSTION PLANTS

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Application Number Priority Date Filing Date Title
DE19843447494 DE3447494A1 (en) 1984-12-27 1984-12-27 Multiple-stage simultaneous separating out of SO2 and NOx, the untreated gas being first introduced into a co-current stage

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DE3447494A1 true DE3447494A1 (en) 1986-07-10

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3703766A1 (en) * 1987-02-07 1988-08-18 Hoelter Heinz Process for treating the clean gases of a flue gas desulphurisation plant

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2353528A1 (en) * 1972-10-25 1974-05-16 Hitachi Ltd Treating waste gases to remove nitrogen- and sulphur oxides - without the formation of nitric acid derivs
DE2416660A1 (en) * 1973-04-09 1974-10-24 Mitsui Petrochemical Ind PROCEDURE FOR THE REMOVAL OF NITROGEN OXYDE FROM A GAS
DE2445567A1 (en) * 1973-09-24 1975-04-03 Asahi Chemical Ind PROCEDURE FOR REMOVING NITROGEN MONOXIDE FROM A GAS CONTAINING NITROGEN MONOXIDE

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2353528A1 (en) * 1972-10-25 1974-05-16 Hitachi Ltd Treating waste gases to remove nitrogen- and sulphur oxides - without the formation of nitric acid derivs
DE2416660A1 (en) * 1973-04-09 1974-10-24 Mitsui Petrochemical Ind PROCEDURE FOR THE REMOVAL OF NITROGEN OXYDE FROM A GAS
DE2445567A1 (en) * 1973-09-24 1975-04-03 Asahi Chemical Ind PROCEDURE FOR REMOVING NITROGEN MONOXIDE FROM A GAS CONTAINING NITROGEN MONOXIDE

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3703766A1 (en) * 1987-02-07 1988-08-18 Hoelter Heinz Process for treating the clean gases of a flue gas desulphurisation plant

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