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EP0239598A1 - Procede pour diminuer la teneur en matieres deleteres de gaz de fumees ou de procedes contenant des poussieres - Google Patents

Procede pour diminuer la teneur en matieres deleteres de gaz de fumees ou de procedes contenant des poussieres

Info

Publication number
EP0239598A1
EP0239598A1 EP19860905801 EP86905801A EP0239598A1 EP 0239598 A1 EP0239598 A1 EP 0239598A1 EP 19860905801 EP19860905801 EP 19860905801 EP 86905801 A EP86905801 A EP 86905801A EP 0239598 A1 EP0239598 A1 EP 0239598A1
Authority
EP
European Patent Office
Prior art keywords
dust
gases
ammonia
injection cooler
content
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Withdrawn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
EP19860905801
Other languages
German (de)
English (en)
Inventor
Jürgen RITTER
Hans Reye
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.)
Perfluktiv Technik AG
Original Assignee
Perfluktiv Technik AG
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 Perfluktiv Technik AG filed Critical Perfluktiv Technik AG
Publication of EP0239598A1 publication Critical patent/EP0239598A1/fr
Withdrawn legal-status Critical Current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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • 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
    • 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
    • B01D53/68—Halogens or halogen compounds

Definitions

  • the invention relates to a method for reducing the pollutant content of dust-containing smoke or process gases, in which the gases are filtered for dust separation, are cooled by means of an injection cooler by injection and evaporation of water, are fed to an adsorber with an activated coke bed, and for loading the activated coke with pollutants , in particular sulfur dioxide, are conveyed through the activated coke bed, and sulfur dioxide is desorbed from the activated coke bed in the regenerator and fed to further processing.
  • pollutants in particular sulfur dioxide
  • ammonia gas to the flue gases in the course of the method in order to at least partially catalytically decompose the nitrogen oxides contained in the flue gas and also to partially remove these pollutants from the flue gas.
  • the object of the invention is to develop a method of the type mentioned in the introduction in such a way that the disadvantages described are largely avoided and the dew point of the flue gases is reduced when they are transferred to the adsorber, and corrosion-free operation of the adsorber is made possible and the activates before Destruction can be protected by ammonium salts.
  • the method mentioned at the outset is characterized in that the gases with their dust content are conveyed through an at least one injection cooler before filtering, with the simultaneous addition of ammonia as an additive for chemical bonding of the predominant to almost complete proportion of the SO ,, and the halogens the gases as well as for the separation and attachment of the ammonium salts and heavy metals thus formed to the dust, and that the gases are transferred to the adsorber after filtering and the dust loaded with the salts deposited is processed after its discharge to recover the ammonia.
  • the invention is based on the knowledge that the dust particles contained in the flue gas are used as carrier particles before they are discharged through the filtering, to which the ammonium salts formed by the addition of the ammonia can accumulate, so that these together with the dust of the following filters be carried out.
  • the addition of the ammonia as an additive to the injection cooler results in a uniform distribution in the gas volume, and indeed also.
  • ammonia can be introduced into the injection cooler in the form of an aqueous solution, since the evaporation produces the ammonia gas which is rapidly distributed in the mixing chamber.
  • a particularly favorable and faster reaction is achieved if the additive is added at least partially in the form of ammonia gas.
  • the flue dust loaded with ammonium salts has an increased electrical conductivity in the flue gas emerging from the injection cooler compared to unloaded flue dust
  • an improvement in the separation efficiency can be achieved when an electrostatic filter is used to separate the flue dust loaded with the ammonium salts.
  • a better degree of separation of the fine dust is achieved, on which the heavy metals are preferentially attached.
  • the electrostatic filter Due to the reduction in the gas temperature previously carried out in the injection cooler, the electrostatic filter can either be smaller than the previous arrangement in front of the injection cooler. measure or be operated with the same dimensioning with longer dwell time of the gas or reduced gas speed and thus lower pressure losses.
  • filter systems of various types possibly also in combination, can be used for the discharge of the dust with the deposits.
  • the easy solubility of the ammonium salts in water is used in a known manner, so that after the separation of the ammonium salts, the fly dust is present as a moist mass, which makes it easy to handle and transport Airborne dust results.
  • the method described is not only suitable for flue gases from power plants or the like, but can also be used in the same way for gases from other processes, such as for example in glass production and also in waste incineration.
  • the above-mentioned difficulties can be overcome, however, in that the gases are passed through an upstream injection cooler or an upstream injection stage before being introduced into the injection cooler, in which ammonia is added, and thereby by addition of lime milk the SO ,, -, and halogen content of the gases is reduced.
  • the first injection cooler or the upstream injection stage must have good corrosion protection.
  • the exhaust gas temperature is reduced from about 200 to 180 ° C. to about 160 ° C. and not only a reduction in the halogen content is achieved by adding the milk of lime, but at the same time also a part the lime necessary for the subsequent chemical bonding during the preparation is fed to the process gas and thereby partially covers the lime requirement later required for the treatment of the flying dust loaded with the ammonium salts.
  • the salts which form in the first injection cooler or the upstream injection stage increase the dust in the gas. This is advantageous for smoke or press gases with low dust content.
  • the residual separation of the halogens except for traces takes place in the manner described in the second injection cooler or the second stage of the injection cooler using ammonia at temperatures between 160 ° and 120 ° C. or possibly even lower temperatures. A temperature reduction noticeably below 120 ° C is possible. It offers advantages for better deposition of heavy metals, especially mercury.
  • the described pre-separation of the pollutants and the multi-stage injection cooling result in a treatment of the gases in a wide temperature range, which has a favorable effect on the degree of separation which affects pollutants.
  • FIG. 1 shows a flow diagram for the treatment of flue gases from power plants with a flow diagram for the processing of the fly dust for the recovery of the ammonia
  • FIG. 2 shows a flow diagram for the treatment of process gases from a glass tank
  • FIG. 3 shows a flow diagram for the treatment of process gases from a waste incineration plant.
  • Fig. 1 denotes a boiler of a power plant, from which the flue gas is fed to an injection cooler 3 via the flue gas line 2.
  • Temperature of 180 ° to 160 ° C is brought to a process temperature of about 120 ° C or below in the injection cooler 3 by the simultaneous addition of water and ammonia.
  • 4 is the
  • the chemical bonding of the halogens and SO, contained in the flue gas, to ammonium salts and their accumulation as well as the accumulation of the heavy metals on the dust particles of the flue gas takes place.
  • the flue gas with the pollutant-laden dust particles is fed via line 6 to an electric filter 7, in which the fly dust is separated, which is transferred to a bunker 8, while the gas freed from dust and ammonium salts via the further feed line 9 into the an active coke bed receiving adsorber 10 is transferred.
  • the adsorber 10 is preferably equipped as a shaft with planar piles of activated coke which are arranged one above the other and which are conveyed through the adsorber from floor to floor and through which the flue gas flows in countercurrent. In the adsorber there is a further reduction in pollutants in the flue gas, the S0 “being substantially completely removed from the flue gas before the flue gas is passed via line 11 and a blower 12 into the chimney 13.
  • the adsorber works together with an activated coke regenerator, which is not shown in the drawing and which serves to process the activated coke, which is essentially loaded with the SO, by evaporating the sulfur dioxide, the sulfur dioxide in turn can be processed.
  • the dust collected in the electrostatic filter 7 and transferred to the bunker 8 and loaded with ammonium salts is transferred from the bunker 8 into a stirring mixer 14, in which the flying dust is mixed with water which comes from the centrifuge 15 arranged after the stirring mixer 14 and is introduced into the agitating mixer 14 via the return line 16.
  • the pasty moist mass supplied via the line 17 from the stirring mixer 14 is spun off with the addition of water and the moist solid part originating from the centrifuge 15 is fed via line 18 to a spray dryer 19, to which a filter 20 is connected, in which the solids are separated from the gaseous drying medium fed into the spray dryer 19.
  • the solids separated in the filter 20 are passed into the bunker 21 and later deposited there.
  • the gaseous drying medium from the filter 20 is fed via line 22 to the power plant exhaust gases upstream of the injection cooler 3.
  • the return line 16 between the centrifuge 15 and the agitator 14 becomes part of the water and salt existing mixture is transferred via line 23 into a mixer 24, in which the water / salt mixture is mixed with hydrated lime.
  • the liquid portion consisting of water and ammonia is separated, which is fed via line 26 to the water supply 4 to the injection cooler 3.
  • Solids are transferred via a line 27 to a dryer 28- and dried there by means of heated gases at temperatures of approximately 30 ° C. and separated in the downstream filter 29 and transferred via line 30 to the bunker 21, in order later to Landfill.
  • the gaseous heating medium separated from the solids in the filter 29 is in turn admixed via line 31 to the power plant exhaust gases upstream of the injection cooler 3.
  • FIG. 2 shows the i 12 Reduction of the pollutant content according to the invention for process gases from a Glaswa ⁇ e.
  • the flow diagram essentially corresponds to the flow diagram for the flue gases of a power plant, as shown in FIG. 1. Instead of the boiler
  • FIG. 1 is in the flow diagram according to FIG. 1 is in the flow diagram according to FIG. 1
  • FIG. 2 shows a glass tank 33, from which the dust-containing process gas is removed and treated with a slight variation in order to be freed from the pollutants therein, as described earlier in connection with FIG. 1 for the flue gas from a power plant is.
  • the elements corresponding to FIG. 1 are provided with the same reference numbers. An explanation of the path of the flue gases according to FIG. 2 and their treatment should be superfluous with regard to the explanations for FIG. 1.
  • an additional heat exchanger 34 is provided, in which the process gas flowing out of the glass wall is passed through at a temperature of approximately 450 ° C. and cooled to a temperature of approximately 250 ° C.
  • the pollutant-free exhaust gases conveyed into the chimney 13 by the blower 12 are raised to a temperature of approximately 300 ° C., at which they enter the chimney 13.
  • FIG. 3 corresponds, however, without the processing of the dust loaded with the ammonium salts of FIG. 1, so that in FIG. 3 the same parts are again provided with the same reference numerals are as in Fig. l.
  • the injection cooler 3 is designed differently from the flow diagram according to FIG. 1. It is designed for the treatment of the process gases from the garbage disposal in the example shown as a two-stage injection cooler. In the upper part of the desuperheater. is carried out by the arrow 35 a-n indicated the supply of water and indicated by the arrow 32 the supply of lime milk in order to reduce the relatively high proportion of halogens contained in the waste combustion gases by 50% before the process gases treated in this way into the lower stage of the Injection cooler 3 enter, in which the supply of water and ammonia takes place in the same manner as has been described in connection with FIG. 1. In this case, even with the flow chart of FIG.

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

Procédé pour diminuer la teneur en matières délétères de gaz de fumées ou de traitements contenant des poussières au moyen d'un système de refroidissement à injection et en utilisant un adsorbeur coopérant avec un régénérateur et de charges de coke activé passant sur ces derniers, dans lequel les gaz chargés de poussières avant le filtrage sont envoyés à travers au moins un système de refroidissement à injection avec addition simultanée de l'ammoniac comme additif pour réaliser la liaison chimique de la majeure partie sinon la totalité du SO3 et des halogènes, ainsi que pour séparer et précipiter les sels ainsi formés et les métaux lourds sur la poussière. La poussière chargée de sels précipités est retirée par filtrage et préparée pour récupération de l'ammoniac. Après filtrage des matières solides qu'ils contiennent les gas de fumées sont envoyés par la ou les charges de coke activé de l'adsorbeur, de sorte qu'on sépare dans l'adsorbeur essentiellement seulement du SO2, qui est récupéré du coke activé par le traitement de ce dernier dans le régénérateur et est envoyé pour traitement ultérieur.
EP19860905801 1985-10-05 1986-10-04 Procede pour diminuer la teneur en matieres deleteres de gaz de fumees ou de procedes contenant des poussieres Withdrawn EP0239598A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19853535600 DE3535600C1 (de) 1985-10-05 1985-10-05 Verfahren zur Verminderung des Schadstoffgehaltes von staubhaltigen Rauch- oder Prozessgasen
DE3535600 1985-10-05

Publications (1)

Publication Number Publication Date
EP0239598A1 true EP0239598A1 (fr) 1987-10-07

Family

ID=6282848

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19860905801 Withdrawn EP0239598A1 (fr) 1985-10-05 1986-10-04 Procede pour diminuer la teneur en matieres deleteres de gaz de fumees ou de procedes contenant des poussieres

Country Status (5)

Country Link
EP (1) EP0239598A1 (fr)
AU (1) AU6400486A (fr)
DD (1) DD249857A5 (fr)
DE (1) DE3535600C1 (fr)
WO (1) WO1987001963A1 (fr)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FI885299A7 (fi) * 1987-03-18 1988-11-16 Radian Corp Jätekaasun käsittelymenetelmä
DE3732353A1 (de) * 1987-09-25 1989-04-06 Metallgesellschaft Ag Verfahren und vorrichtung zur abscheidung gasfoermiger schadstoffe aus abgasen
AT396655B (de) * 1992-03-26 1993-11-25 Oeko Wien Umweltschutzprojekte Verfahren zur reinigung von rauchgasen
KR950701245A (ko) * 1993-03-05 1995-03-23 파투지 알렉산더 배기가스의 정화방법 및 그 설비(Varfagren und Anlage zur Abgasreinigung, sowie Kombination dieser Abgasreinigung mit einer Abwasserreinigung)
DE4425471A1 (de) * 1994-07-19 1996-01-25 Fpr Holding Ag Verfahren zum Reinigen von Abgasen
CN103028385B (zh) * 2011-09-28 2015-01-07 密西西比国际水务有限公司 一种活性焦再生设备的除尘及冷却方法和装置
CN107185358A (zh) * 2017-06-29 2017-09-22 西安西热锅炉环保工程有限公司 一种干法烟气污染物一体化脱除装置
CN107866142B (zh) * 2017-10-31 2021-05-14 中冶华天工程技术有限公司 用于水泥行业干法脱硫脱硝副产物的处置系统

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4164555A (en) * 1977-09-12 1979-08-14 Foster Wheeler Energy Corporation Pollution control system and method for the removal of sulfur oxides
JPS5543814A (en) * 1978-09-22 1980-03-27 Hitachi Ltd Bipolar semiconductor device's current amplification control method
DE2928526C3 (de) * 1979-07-14 1984-03-29 Buckau-Walther AG, 4048 Grevenbroich Verfahren zum Entfernen saurer Komponenten aus Abgasen
JPS59501579A (ja) * 1982-08-26 1984-09-06 ラデイラ，ニユ−トン・ゴンカルブズ 硫黄を含有する燃料の燃焼から生じる大気汚染物質を除去するための方法
DE3403995A1 (de) * 1984-02-06 1985-08-08 L. & C. Steinmüller GmbH, 5270 Gummersbach Verfahren zur abscheidung von in rauchgasen enthaltenen gasfoermigen schadstoffen

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO8701963A1 *

Also Published As

Publication number Publication date
DD249857A5 (de) 1987-09-23
DE3535600C1 (de) 1987-05-27
AU6400486A (en) 1987-04-24
WO1987001963A1 (fr) 1987-04-09

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