WO1992015390A1 - Method for cleaning process gases containing gaseous impurities - Google Patents

Method for cleaning process gases containing gaseous impurities Download PDF

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Publication number
WO1992015390A1
WO1992015390A1 PCT/SE1992/000119 SE9200119W WO9215390A1 WO 1992015390 A1 WO1992015390 A1 WO 1992015390A1 SE 9200119 W SE9200119 W SE 9200119W WO 9215390 A1 WO9215390 A1 WO 9215390A1
Authority
WO
WIPO (PCT)
Prior art keywords
site
absorbent
gas passage
dust separator
gaseous impurities
Prior art date
Application number
PCT/SE1992/000119
Other languages
French (fr)
Inventor
Stefan Åhman
Jens Gertner Hansen
Original Assignee
ABB Fläkt AB
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 ABB Fläkt AB filed Critical ABB Fläkt AB
Publication of WO1992015390A1 publication Critical patent/WO1992015390A1/en

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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
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/508—Sulfur oxides by treating the gases with solids

Definitions

  • the present invention relates to a method for clean- ing process gases, such as flue gases, containing gaseous impurities, such as sulphur dioxide, wherein the process gases are conducted along a process-gas passage running through a reactor plant, and through a dust separator communicating with the process-gas passage, an absorbent, such as Ca(0H) 2 and/or CaO, that reacts with the gaseous impurities being injected in finely divided form into the process-gas passage in order to react with the gaseous impurities and form particles which are separated in the reactor plant and the dust separator, use being made of a fresh absorbent as well as a portion of the particles separated in the reactor plant and the dust separator as absorbent, said portion of particles separated in the reactor plant and the dust separator being re-injected together with water into the process-gas passage at a first site.
  • an absorbent such as Ca(0H) 2 and/or CaO
  • the flue gases are conducted through a reactor into which an absorbent suspended or dissolved in water is injected in order to react with gaseous impurities, e.g. acid compo ⁇ nents such as sulphur dioxide, in the flue gases. Then, the flue gases are conducted through a dust separator, such as a bag filter or an electrostatic filter. Residual products or reaction products, such as calcium sulphite and calcium sulphate, are separated in the form of dry particles in the reactor and the dust separator.
  • gaseous impurities e.g. acid compo ⁇ nents
  • a dust separator such as a bag filter or an electrostatic filter. Residual products or reaction products, such as calcium sulphite and calcium sulphate, are separated in the form of dry particles in the reactor and the dust separator.
  • the object of the present invention is to provide a cleaning method in which some of the residual or reaction products separated in the reactor and the dust separator are recycled in such a manner that the separation of the gaseous impurities is improved, i.e. in such a manner that one and the same amount of fresh absorbent gives a higher degree of separation in the method according to the inven ⁇ tion than in the prior-art method described above.
  • this object is achieved by a method which is of the type stated in the introduc ⁇ tion to this specification and which is characterised by injecting at least the main part of the fresh absorbent into the process-gas passage at a second site which is separate from said first site.
  • the second site is located downstream from the first site.
  • Fresh absorbent is then preferably injected together with water at the second site.
  • water is supplied in such an amount that the relative humidity of the pro- cess gases is increased to 20-50% after the first site and to 30-60% after the second site.
  • Use is suitably made of Ca(0H) 2 as fresh absorbent.
  • the second site is located upstream from the first site.
  • Fresh absorbent is then preferably injected in dry state at the second site.
  • water is supplied in such an amount at the first site that the relative humidity of the process gases is increased to 30-60%.
  • Use is suitably made of CaO as fresh absorbent.
  • a contact reactor 1 is connected to a coal-fired boiler house (not shown) by a flue duct 2.
  • This duct 2 ends in the upper part of the reactor 1.
  • the reactor 1 is connected to a dust separator 4 with hoppers 5 for intercepting the separated dust.
  • the dust separator 4 is a bag filter, but it may also be an eletrostatic filter.
  • the dust sepa ⁇ rator 4 is connected to a chimney 7 by a flue duct 6.
  • a fan 8 is provided in the flue duct 6.
  • Hot flue gases from the boiler house are conducted through the duct 2, the contact reactor 1, the duct 3 and the dust separator 4 in order to be cleaned. Then, the thus-cleaned flue gases are discharged into the atmospher through the chimney 7.
  • An absorbent such as Ca(0H) 2 , that reacts with the gaseous impurities of the flue gases, such as sulphur dioxide, is injected in powder form into the flue duct 3 between the contact reactor 1 and the dust separator 4.
  • the absorbent is injected by means of an injector (not shown) which is provided in the flue duct 3 at A and which conveniently is a venturi device of the type described in Swedish Patent Application 8904106-5.
  • the absorbent is injected together with water which is supplied to the injector through a line 9. The water is supplied in such a small amount that the powder state of the absorbent is retained.
  • the absorbent is obtained from a fresh-absorbent container 11 equipped with a valve device 10, and is fed via a supply line 12 to the injector by means of a fan 13.
  • the particles of absorbent are reacted with the gaseous impurities of the flue gases, and these impurities are thus transformed into particulate impurities, e.g. consisting of calcium sulphite and calcium sulphate, and a surplus of absor- bent.
  • particulate impurities are separated in the dust separator 4 and intercepted by the hoppers 5. If no preseparator is provided before the contact reactor 1, also fly ash may form part of the separated, particulate impurities.
  • the absorbent is injected by means of a nozzle (not shown) which is provided in the upper part of the contact reactor 1 at B and which conveniently is of the type described in EP-B1-0,198,810 or EP-B1-0,185,630 (SE-C-8501851-3 and SE-C-8406144-9, respectively).
  • the particles of absorbent are reacted with the gaseous impur ⁇ ities, which thus are transformed into particulate impur ⁇ ities of which a minor amount is separated in the contact reactor 1 and collected in the lower part thereof, and of which the main part is separated in the dust separator 4 and intercepted by the hoppers 5.
  • the lower part of the contact reactor 1 and the hoppers 5 of the dust separator 4 are connected, by a conveying line 15, to a device 16 where the separated particles are deposited.
  • the conveying line 15 is connect ⁇ ed to a tank 18 by a branch line 17.
  • the line 17 starts from a point on the conveying line 15 located between the two hoppers 5 of the dust separator 4.
  • An amount of fresh absorbent which is but slight compared with the amount of fresh absorbent introduced into the flue duct 3 via the supply line 12, can be fed to the tank 18 via a line 21 in order to be suspended or dis ⁇ solved in water and pumped further via the line 14.
  • the fresh absorbent e.g. consists of CaO
  • it may be supplied at a site A' upstream from site B through a line 12', instead of at site A downstream from site B.
  • the fresh absorbent is preferably supplied in dry form. Since the main part of the fresh absorbent is in ⁇ jected into the flue-gas passage made up of the flue duct 2, the contact reactor 1 and the flue duct 3 at a site A or A' which is separate from site B where the recycled absorbent is injected into the flue-gas passage, and not, as in the prior-art method described by way of introduc ⁇ tion, at the same site as the recycled absorbent, there i obtained an improved separation of the gaseous impurities with one and the same amount of fresh absorbent.
  • Ca(0H) 2 and CaO have been given as examples of suitable absorbents.
  • Other suitable absorbent are found in a group made up of oxides, hydroxides and carbonates of alkali metals and alkali earth metals.

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

Abstract

In a method for cleaning process gases containing gaseous impurities, the process gases are conducted along a process-gas passage running through a reactor plant (1, 2, 3), and through a dust separator (4) communicating with the process-gas passage. An absorbent that reacts with the gaseous impurities is injected in finely divided form into the process-gas passage in order to react with the gaseous impurities and form particles which are separated in the reactor plant (1, 2, 3) and the dust separator (4). The absorbent used comprises both fresh absorbent and a portion of the particles separated in the reactor plant and the dust separator. This portion of particles separated in the reactor plant and the dust separator are re-injected together with water into the process-gas passage at a first site (B). At least the main part of the fresh absorbent is injected into the process-gas passage at a second site (A; A') which is separate from the first site (B).

Description

METHOD FOR CLEANING PROCESS GASES CONTAINING GASEOUS
IMPURITIES
The present invention relates to a method for clean- ing process gases, such as flue gases, containing gaseous impurities, such as sulphur dioxide, wherein the process gases are conducted along a process-gas passage running through a reactor plant, and through a dust separator communicating with the process-gas passage, an absorbent, such as Ca(0H)2 and/or CaO, that reacts with the gaseous impurities being injected in finely divided form into the process-gas passage in order to react with the gaseous impurities and form particles which are separated in the reactor plant and the dust separator, use being made of a fresh absorbent as well as a portion of the particles separated in the reactor plant and the dust separator as absorbent, said portion of particles separated in the reactor plant and the dust separator being re-injected together with water into the process-gas passage at a first site.
In a prior-art method of this type, used for cleaning the flue gases from e.g. a coal-fired boiler house, the flue gases are conducted through a reactor into which an absorbent suspended or dissolved in water is injected in order to react with gaseous impurities, e.g. acid compo¬ nents such as sulphur dioxide, in the flue gases. Then, the flue gases are conducted through a dust separator, such as a bag filter or an electrostatic filter. Residual products or reaction products, such as calcium sulphite and calcium sulphate, are separated in the form of dry particles in the reactor and the dust separator. To use the absorbent more efficiently, some of the residual or reaction products separated in the reactor and the dust separator are, in this prior-art method, recycled and re- used as absorbent by being suspended or dissolved in water together with fresh absorbent, and then re-injected into the reactor. The object of the present invention is to provide a cleaning method in which some of the residual or reaction products separated in the reactor and the dust separator are recycled in such a manner that the separation of the gaseous impurities is improved, i.e. in such a manner that one and the same amount of fresh absorbent gives a higher degree of separation in the method according to the inven¬ tion than in the prior-art method described above.
According to the invention, this object is achieved by a method which is of the type stated in the introduc¬ tion to this specification and which is characterised by injecting at least the main part of the fresh absorbent into the process-gas passage at a second site which is separate from said first site. In a preferred embodiment of the invention, the second site is located downstream from the first site. Fresh absorbent is then preferably injected together with water at the second site. Conveniently, water is supplied in such an amount that the relative humidity of the pro- cess gases is increased to 20-50% after the first site and to 30-60% after the second site. Use is suitably made of Ca(0H)2 as fresh absorbent.
In another preferred embodiment of the invention, the second site is located upstream from the first site. Fresh absorbent is then preferably injected in dry state at the second site. Conveniently, water is supplied in such an amount at the first site that the relative humidity of the process gases is increased to 30-60%. Use is suitably made of CaO as fresh absorbent. The invention will be described in more detail below with reference to the accompanying drawing which schemati¬ cally illustrates a plant for implementing the method according to the invention.
A contact reactor 1 is connected to a coal-fired boiler house (not shown) by a flue duct 2. This duct 2 ends in the upper part of the reactor 1. By a flue duct 3, the reactor 1 is connected to a dust separator 4 with hoppers 5 for intercepting the separated dust. In the embodiment shown, the dust separator 4 is a bag filter, but it may also be an eletrostatic filter. The dust sepa¬ rator 4 is connected to a chimney 7 by a flue duct 6. A fan 8 is provided in the flue duct 6.
Hot flue gases from the boiler house are conducted through the duct 2, the contact reactor 1, the duct 3 and the dust separator 4 in order to be cleaned. Then, the thus-cleaned flue gases are discharged into the atmospher through the chimney 7.
An absorbent, such as Ca(0H)2, that reacts with the gaseous impurities of the flue gases, such as sulphur dioxide, is injected in powder form into the flue duct 3 between the contact reactor 1 and the dust separator 4. The absorbent is injected by means of an injector (not shown) which is provided in the flue duct 3 at A and which conveniently is a venturi device of the type described in Swedish Patent Application 8904106-5. Pre¬ ferably, the absorbent is injected together with water which is supplied to the injector through a line 9. The water is supplied in such a small amount that the powder state of the absorbent is retained. The absorbent is obtained from a fresh-absorbent container 11 equipped with a valve device 10, and is fed via a supply line 12 to the injector by means of a fan 13. The particles of absorbent are reacted with the gaseous impurities of the flue gases, and these impurities are thus transformed into particulate impurities, e.g. consisting of calcium sulphite and calcium sulphate, and a surplus of absor- bent. These particulate impurities are separated in the dust separator 4 and intercepted by the hoppers 5. If no preseparator is provided before the contact reactor 1, also fly ash may form part of the separated, particulate impurities. An absorbent that reacts with the gaseous impurities of the flue gases and is suspended or dissolved in water, is supplied to the contact reactor 1 via a supply line 14 and injected into the upper part of the reactor in the form of droplets. The absorbent is injected by means of a nozzle (not shown) which is provided in the upper part of the contact reactor 1 at B and which conveniently is of the type described in EP-B1-0,198,810 or EP-B1-0,185,630 (SE-C-8501851-3 and SE-C-8406144-9, respectively). The particles of absorbent are reacted with the gaseous impur¬ ities, which thus are transformed into particulate impur¬ ities of which a minor amount is separated in the contact reactor 1 and collected in the lower part thereof, and of which the main part is separated in the dust separator 4 and intercepted by the hoppers 5.
The lower part of the contact reactor 1 and the hoppers 5 of the dust separator 4 are connected, by a conveying line 15, to a device 16 where the separated particles are deposited. The conveying line 15 is connect¬ ed to a tank 18 by a branch line 17. The line 17 starts from a point on the conveying line 15 located between the two hoppers 5 of the dust separator 4. Some of the par- tides collected in the lower part of the contact reactor 1 and the first hopper 5 of the dust separator 4 are conducted, via the branch line 17, to the tank 18 to be re-used as absorbent. Water is supplied to the tank 18 through a line 19. An absorbent suspended or dissolved in water is fed, with the aid of a pump 20, through the line 14 to the contact reactor 1, as described above.
An amount of fresh absorbent, which is but slight compared with the amount of fresh absorbent introduced into the flue duct 3 via the supply line 12, can be fed to the tank 18 via a line 21 in order to be suspended or dis¬ solved in water and pumped further via the line 14.
When the fresh absorbent e.g. consists of CaO, it may be supplied at a site A' upstream from site B through a line 12', instead of at site A downstream from site B. If so, the fresh absorbent is preferably supplied in dry form. Since the main part of the fresh absorbent is in¬ jected into the flue-gas passage made up of the flue duct 2, the contact reactor 1 and the flue duct 3 at a site A or A' which is separate from site B where the recycled absorbent is injected into the flue-gas passage, and not, as in the prior-art method described by way of introduc¬ tion, at the same site as the recycled absorbent, there i obtained an improved separation of the gaseous impurities with one and the same amount of fresh absorbent. In the foregoing, Ca(0H)2 and CaO have been given as exemples of suitable absorbents. Other suitable absorbent are found in a group made up of oxides, hydroxides and carbonates of alkali metals and alkali earth metals.
The following tests were performed in a pilot plant. I) All fresh absorbent was supplied together with the recycled absorbent at site B (the prior-art method described by way of introduction).
II) All fresh absorbent was supplied in dry state at site A. III) All fresh absorbent was supplied together with minor amount of water at site A.
IV) All fresh absorbent was supplied in dry form at site A' .
The operational parameters measured are stated in th Table below.
Figure imgf000008_0001

Claims

1. A method for cleaning process gases, such as flue gases, containing gaseous impurities, such as sulphur dioxide, wherein the process gases are conducted along a process-gas passage running through a reactor plant (1, 2 3), and through a dust separator (4) communicating with the process-gas passage, an absorbent, such as Ca(0H)2 and/or CaO, that reacts with the gaseous impurities being injected in finely divided form into the process-gas passage in order to react with the gaseous impurities and form particles which are separated in the reactor plant (1, 2, 3) and the dust separator (4), use being made of a fresh absorbent as well as a portion of the particles separated in the reactor plant and the dust separator as absorbent, said portion of particles separated in the reactor plant and the dust separator being re-injected together with water into the process-gas passage at a first site (B), c h a r a c t e r i s e d by injecting at least the main part of the fresh absorbent into the process-gas passage at a second site (A; A' ) which is separate from said first site (B).
2. A method as claimed in claim 1, c h a r a c - t e r i s e d in that the second site (A) is located downstream from the first site (B).
3. A method as claimed in claim 2, c h a r a c ¬ t e r i s e d by injecting fresh absorbent together with water at the second site (A).
4. A method as claimed in claim 3, c h a r a c ¬ t e r i s e d by supplying water in such an amount that the relative humidity of the process-gases is increased t 20-50% after the first site (B) and to 30-60% after the second site (A).
5. A method as claimed in any one of claims 2-4, c h a r a c t e r i s e d by using Ca(0H)2 as fresh absorbent.
6. A method as claimed in claim 1, c h a r a c ¬ t e r i s e d in that the second site (A' ) is located upstream from the first site (B).
7. A method as claimed in claim 6, c h a r a c - t e r i s e d by injecting fresh absorbent in dry state at the second site (A').
8. A method as claimed in claim 7, c h a r a c ¬ t e r i s e d by supplying water in such an amount at the first site (B) that the relative humidity of the process gases is increased to 30-60%.
9. A method as claimed in any one of claims 6-8, c h a r a c t e r i s e d by using CaO as fresh absor¬ bent.
PCT/SE1992/000119 1991-02-28 1992-02-27 Method for cleaning process gases containing gaseous impurities WO1992015390A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE9100584-3 1991-02-28
SE9100584A SE9100584D0 (en) 1991-02-28 1991-02-28 SETTING TO CLEAN PROCESS GASES CONTAINING GAS GAS POLLUTANTS

Publications (1)

Publication Number Publication Date
WO1992015390A1 true WO1992015390A1 (en) 1992-09-17

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SE (1) SE9100584D0 (en)
WO (1) WO1992015390A1 (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2714303A1 (en) * 1993-12-29 1995-06-30 Hamon Ind Thermique Installation for the neutralisation and filtration of acid fumes
FR2957528A1 (en) * 2010-03-22 2011-09-23 Lab Sa METHOD AND INSTALLATION FOR PURIFYING SMOKE CONTAINING ACIDIC POLLUTANTS

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2723958A1 (en) * 1977-05-27 1978-12-07 Heinz Hoelter Dry contact process to purify gases, for e.g. sulphur di:oxide removal - using radial horizontal contact zones for solids and gas with longitudinal slots and screw conveyors below to collect and recycle solids
DE2910537C2 (en) * 1979-03-17 1982-10-21 L. & C. Steinmüller GmbH, 5270 Gummersbach Process for regenerating the dry and fine-grain additives from an exhaust gas purification device
EP0273508A1 (en) * 1986-12-23 1988-07-06 Metallgesellschaft Ag Waste gas purification process
SE460642B (en) * 1987-03-06 1989-11-06 Flaekt Ab PROCEDURES FOR ABSORPING GAS GAS COMPONENTS FROM FORECURATED SMOKE GASES
SE462551B (en) * 1988-03-03 1990-07-16 Flaekt Ab PROCEDURES FOR PURIFICATION OF COB GAS FORMED GAS

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2723958A1 (en) * 1977-05-27 1978-12-07 Heinz Hoelter Dry contact process to purify gases, for e.g. sulphur di:oxide removal - using radial horizontal contact zones for solids and gas with longitudinal slots and screw conveyors below to collect and recycle solids
DE2910537C2 (en) * 1979-03-17 1982-10-21 L. & C. Steinmüller GmbH, 5270 Gummersbach Process for regenerating the dry and fine-grain additives from an exhaust gas purification device
EP0273508A1 (en) * 1986-12-23 1988-07-06 Metallgesellschaft Ag Waste gas purification process
SE460642B (en) * 1987-03-06 1989-11-06 Flaekt Ab PROCEDURES FOR ABSORPING GAS GAS COMPONENTS FROM FORECURATED SMOKE GASES
SE462551B (en) * 1988-03-03 1990-07-16 Flaekt Ab PROCEDURES FOR PURIFICATION OF COB GAS FORMED GAS

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2714303A1 (en) * 1993-12-29 1995-06-30 Hamon Ind Thermique Installation for the neutralisation and filtration of acid fumes
FR2957528A1 (en) * 2010-03-22 2011-09-23 Lab Sa METHOD AND INSTALLATION FOR PURIFYING SMOKE CONTAINING ACIDIC POLLUTANTS
EP2371444A1 (en) * 2010-03-22 2011-10-05 Lab Sa Process and device for the purification of fumes containing acidic pollutants

Also Published As

Publication number Publication date
SE9100584D0 (en) 1991-02-28
AU1341692A (en) 1992-10-06

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