CN1045927A - The method and apparatus of cleaning flue gases - Google Patents
The method and apparatus of cleaning flue gases Download PDFInfo
- Publication number
- CN1045927A CN1045927A CN 90101425 CN90101425A CN1045927A CN 1045927 A CN1045927 A CN 1045927A CN 90101425 CN90101425 CN 90101425 CN 90101425 A CN90101425 A CN 90101425A CN 1045927 A CN1045927 A CN 1045927A
- Authority
- CN
- China
- Prior art keywords
- cao
- reactor
- flue gas
- separator
- particle
- 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.)
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-
- 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
Abstract
The method and apparatus of cleaning flue gases, the solid that preseparator 8 is told transfer to the activating apparatus 11 of 8 back, therein the material of telling are crushed to more granule, make the CaSO that is wrapping CaO
4Crust is smashed and is disengaged the CaO that is used for hydration reaction.The CaO powder that contains of having crushed is delivered to reactor 16,16 from 11 following currents and is positioned at by the flow of flue gas direction and in 8 back.The CaO particle by a shape district A of jet pipe 14a importing 16, also imports the A district by jet pipe 17a with water in 16, CaO and water are directly reacted, the Ca of generation (OH)
2With 16 in smoke reaction and combine wherein SO
2
Description
The present invention relates to a kind of method and apparatus of cleaning flue gases, this method is that a kind of absorbent is transported to heating furnace, the reaction of Salmon-Saxl that contains in this absorbent and the flue gas.And then flue gas has been transported to along blast pipe from heating furnace and has given separator, this gives separator and separates with the absorbent of reaction of Salmon-Saxl from flue gas and should be transported to a lock out operation unit by unreacted product, here with mechanical means this product is activated.
In early days in the applicant's of Gong Buing the Finnish patent application 76931, known a kind of method is given in the reactor of separator back in flue gas from giving the isolated solid matter of separator by hydration and cause being transferred in the flue-gas flow direction with reaction of Salmon-Saxl and following current and prepare.
The objective of the invention is to improve particularly its hydration operation of said method.Purpose is can strengthen the degree of removing desulfuration from flue gas greatly by apparatus and method of the present invention after heating furnace.
The objective of the invention is to finish the CaO and the CaSO that separate from flue gas by means of solution
4Handle with mechanical means by activating apparatus, for example crushing centers on the CaSO of CaO particle thus
4Crust is broken and discharge the CaO that is used for hydration reaction, and second separator has been used in the activating apparatus back further, from other material, isolate active CaO and with the CaO powder from this second separator by going forward side by side into the reactor of hydration reaction.Hydrated CaO further reacts with the flue gas that enters reactor, and effectively in conjunction with the SO that contains in the flue gas
2
Below whole matting will be described step by step.
In the first step, the very thin lime stone of mill is blown in 900 ℃-1200 ℃ the heating furnace, therefore, calcium carbonate decomposes according to reactional equation (1)
The partial oxidation calcium that generates continues to react by formula (2) with sulfur dioxide thus:
So generated calcium sulfate, the ratio of the sulphur that reacts in heating furnace is the 10-70% of total sulfur content mostly.When using an amount of (that is to say, for the sulphur that contains in the coal, be rational economically) reagent, the sulphur that separates in heating furnace is about SO
2The 30-50% of total amount in order to reach the discharge capacity that is lower than regulation, must continue also that in the later treatment process of heating furnace sulphur is carried out combination and handle.
In second step, unreacted CaO and product are come out with flue gas carrier band from heating furnace and are ended to give separator.Can use various dried dust separators as giving separator.
When the size of the limestone particle that is blown into heating furnace has been done suitable selection with respect to flue dust, have only the part that mainly contains CaO further finishing in the treatment process.But, be covered with one deck CaSO
4The CaO particle also always further finishing in the treatment process, in this case, by the present invention be in activating apparatus (what preferentially select for use is in forcing press) by the CaSO of extruding round CaO
4The top layer makes the CaO activation discharge the CaO that is used for hydration reaction.
In further processing procedure, separated and crushed part in a reactor according to following reactional equation by hydration
In order to make the SO that still is retained in the flue gas
2Can react and can be removed from flue gas by reaction equation (2), hydration is absolutely necessary.
After this reactor, flue dust and product are separated from flue gas.Separator for example can be: electrofilter or flexible pipe filter.When using the flexible pipe filter, the association reaction of sulphur also takes place on the dust layer that hose surface forms.
According to method of the present invention, its feature mainly is, is sent to and is placed on the activating apparatus that gives the separator back from giving separator separated solids matter.In this device, give the material grains crushing or the littler particle that separate earlier.Therefore be wrapped in the CaSO of CaO
4The top layer is broken and discharge the CaO that is used for hydration reaction and being transferred to reactor by the powdered substance of the crushed CaO of containing from the activating apparatus following current.This reactor is placed in flue gas and gives the separator back, on the direction of flue-gas flow.The CaO particle by the hydration fully of following operation quilt, promptly imports the CaO particle by jet pipe a shape district of reactor in reactor.By jet pipe water is imported equally and drip the shape district, therefore, CaO and water droplet are met on the route of being controlled, CaO and water directly react, and the Ca(OH that generates)
2Further with reactor in the flue gas reaction of flowing and combine the SO that contains in the flue gas
2
Therefore the principal character of equipment of the present invention is that this equipment comprises an activating apparatus after giving separator, and the material grains that this activating apparatus is given separation pulverizes littler particle, round the CaSO of CaO
4The top layer is broken and discharge the CaO that is used for hydration reaction, and this equipment comprises a pipeline.The particle that will contain CaO by this pipeline is transferred in the reactor and carries out hydration, and this reactor is placed on the back that flue gas on the flue-gas flow direction is given separator.The said equipment also comprises jet pipe, by jet pipe the CaO particle is transferred in the above-mentioned reactor, and water jet nozzle in fact be placed on above-mentioned jet pipe near.
The embodiment preferred more of the present invention that will explain through diagrams below further describe the present invention, but should not think that the present invention is only limited to these embodiments.
Figure 1A is the forcing press as activating apparatus.
Figure 1B is the schematic diagram that disengages CaO in extrusion process.
Fig. 2 and Fig. 3 are the schematic diagrames of method and apparatus.
In the method for the cleaning flue gases that Figure 1A shows with diagram to Fig. 3, limestone powder is transported in the heating furnace, make it at first roasting and generate calcium oxide (CaO).Then with sulphur compound reaction that in flue gas, comprises and generation calcium sulfate (CaSO
4).
The ratio of participating in the CaO of reaction is 5-30%, normally 15%, and the reason that the utilization rate of calcium is low is the CaSO that generates in reaction
4Can hinder the carrying out of reaction when the top layer reaches certain thickness, so that in 0.5-5 second, reaction has little time to carry out between 2 seconds period of use but normally be not less than.Temperature too high (common＜1150 ℃) can cause caking on the surface of limestone particle, thereby reduces respond.
Product and floating dust are admitted in the sulfur removal unit device that is placed on the heating furnace back with flue gas, and unreacted here CaO is at first given separation.
According to method of the present invention, by smashing the CaSO that surrounds CaO
4The top layer reactivates the CaO particle of calcic.This step is that CaO gives after separating and carries out in activating apparatus (easy to use is forcing press), and crushed fine product is transported to and drips the shape district in the wetting reactor of flue gas in activating apparatus, thereby CaO is generated Ca(OH by hydration)
2, effectively in conjunction with SO
2And generation calcium sulfite CaSO
3The particulate of having crushed produces to be carried, for example: carry by doing carrier with air, so that powdered product is transported to the shape district that flue gas is moistened CaO in the reactor of temperature by jet pipe, so CaO is generated Ca(OH by hydration basically in the wetting reactor of flue gas)
2
The particle that only has the highest oxidation calcium content is transferred to the hydration operation, and for example: floating dust is separated in second separator of activating apparatus back.
Therefore, following reaction takes place the shape district of dripping in the wetting reactor of flue gas: CaO is generated Ca(OH by hydration)
2, Ca(OH)
2With the sulfur dioxide SO that contains in the flue gas
2Reaction also generates calcium sulfite CaSO
3
Except hydration reaction takes place,, also cooled off flue gas simultaneously by water being ejected into the shape district in the wetting reactor of flue gas.
Figure 1A is the activating apparatus 11 of the present invention that explains through diagrams, and the activating apparatus of preferentially selecting for use is a forcing press, give and isolate the material stream J that contains CaO and be admitted to forcing press 11 through giving separator, this material stream by carrier band at forcing press garden dish E
1And E
2Between.Simultaneously, the garden of rotation dish E
1, E
2Material is pulled into garden dish E
1, E
2Between the space, this material is subjected to very strong pressure.
Figure 1B has diagrammatized by CaSO
4The top layer is round a CaO particle, CaSO
4The top layer hinders the hydration of CaO significantly in hydration reaction.According to the present invention is by coil E in the punching machine garden
1, E
2Between push CaO-CaSO
4Particle is this CaSO
4Quilt is played on the top layer.At CaO-CaSO
4The interface has formed failure crack F
1, F
2, F
3, remove CaSO along interfacial separation from the surface of CaO component
4, thereby disengaged the CaO that is used for hydration reaction.
In Fig. 2, hold the bulk container of absorbent (what preferentially select for use is lime stone) and represent with symbol 1.The dosimetry device 2 that absorbent is arranged in the bottom of bulk container.Carry the air blast 3 of air, the carrier gas that is mixed with absorbent is blown in the heating furnace 4.Combustion gas and coal are sent into along pipeline 5.Heating furnace is the heating furnace of combustion powder in preferred embodiments.But the heating furnace in the embodiment preferred also can be the usually said fire grate heating furnace or the heating furnace of fire grate heating furnace/combustion powder to combine.In this case, fire grate is represented (as shown in FIG.) with symbol 6.Slag is discharged from heating furnace along pipeline 7.Flue gas is gone out by heating furnace, enters flue gas along flue gas duct and gives separator 8.Giving separator 8 in preferred embodiments is made up of cyclone separator.The particle of sort out is split in the intermediate receptacle 9.The device 10 of sealing, wherein easy to use is usually said sealing feeder, distinguishes grade, enters intermediate receptacle 9 from giving separator 8, enters preferably forcing press of activating apparatus 11().Flue gas 16 enters powder dust separating device 18 along pipeline 21 from reactor.
Powder dust separating device can comprise electrofilter or the flexible pipe filter device that is used to separate dust.Flue gas blower 19 sucks out flue gas from powder dust separating device 18 and drum (wind) is gone into cigarette fontanel 20 and from then on and then enter open air (atmosphere).The flue gas impurity that separates with 18 devices from cell arrangement 16 (CaSO for example
4) be excluded along discharge line 28.
In activating apparatus 11, handle the CaO that gives separation and the CaSO of sintering with mechanical means
4Particle.By smashing CaSO around CaO
4The top layer.The CaO particle is reactivated so that disengage the CaO that is used for hydration.The particle that has been activated 12 is transported to second separator 13 and enters reactor 16 along pipeline 14 from activating apparatus 11 along pipeline.Air carrier or carrier gas are sent to pipeline 14 by blowing plant 15.Material also can directly enter reactor 16 from activating apparatus 11.At this moment do not use second separator 13.Contain pulverous CaO material that has been activated and drip shape district A by what jet pipe 14a was injected into reactor 16.Water also is sprayed to a shape district A of reactor 16.This water causes that the CaO hydration generates Ca(OH)
2Second purpose of transporting water is cooling stack gas.Hydration CaO is with Ca(OH)
2Form and flue gas in the SO that contains
2React effectively and generate calcium sulfite CaSO
3Water enters reactor 16 along pipeline 17 and the terminal jet pipe 17a by pipeline 17 to drip the spraying of shape form.Terminal jet pipe 17a be placed on just powder jet pipe 14a near, with direct contact and the reaction between the component of guaranteeing to participate in hydration reaction.
The active CaO powder that separates from flue gas stream is sent into the zone of the water smoke A of reactor 16 effectively, to guarantee to have water/affixed touching well.Flue gas is flowed, so that the Ca(OH that flue gas and hydration generate in reactor 16)
2Particle meets each other as far as possible effectively.Thereby guaranteed Ca(OH)
2The SO that contains in particle and the flue gas
2Between good contact.The dust that contains CaO that comes out from jet pipe 14a, 17a and the incoming direction of water are favourable perpendicular to the direction of flue gas stream (S).
The conveying of water and dust can concentrate on the center of reactor 16 and carry out so that the inwall of reactor keeps dry.
By jet pipe 17a transporting water, purpose is to make the heat free (being able to do in time) that contains in the flue gas evaporate whole moisture and not generate wet solid suspension or waste water in any stage.
Fig. 3 method and apparatus of the present invention that explains through diagrams in more detail.Work as CaO-CaSO
4Mixture for example forcing press of activating apparatus 11(, pulverizer, grinder, breaker) when handling with mechanical means.Smashed CaSO around CaO
4The CaO that is used for hydration has been disengaged on the top layer.By method shown in Figure 2, the CaO and the CaSO that handled with mechanical means
4Enter second separator 13 along pipeline 12.In second separator 13, carry out classification and can from the CaO powder stream of activity, separate floating dust or CaSO whereby
4, and therefore can reduce the dust load of reactor 16 and the dust load of the powder dust separating device that reduces reactor 16 back.As shown in Figure 3, the jet pipe 14a of processed reactive powder shape CaO material by pipeline 14 is transported among the flue gas stream S in the reactor 16, and what above-mentioned material entered the flue gas reactor drips shape district A, and water smoke D also enters from jet pipe 17a and drips a shape district A simultaneously.Water smoke D introduces from the jet pipe 17a ejection of pipeline 17.Jet pipe 17a is placed on a shape district A of reactor 16, and near the dust jet pipe, a shape district A is illustrated in a zone in the reactor 16, and the water that atomized in this zone also is not evaporated because of the heat energy transfer of flue S.
Claims (11)
1, the method for cleaning flue gases, comprise absorbent is sent into heating furnace (4), the reaction of Salmon-Saxl that contains in this absorbent and the flue gas, and then flue gas is transferred to along discharge duct (a) from heating furnace and gives separator (8), this give separator separate not with flue gas in the absorbent that reacts of sulphur and with flue gas in reaction of Salmon-Saxl partially absorb the agent particle, it is characterized in that, be placed on the activating apparatus (11) that gives separator (8) back being transferred to by separator (8) separated solids matter, this activating apparatus is given the material that has separated
Therefore particle is crushed to littler particle, round the CaSO of CaO
4The top layer is broken and discharge the CaO that is used for hydration reaction, in this program, the powdered material of the crushed CaO of containing is transferred to from activating apparatus (11) following current and is placed on flue gas and gives the reactor (16) on the flue-gas flow direction of separator (8) back, and in this program the CaO particle in reactor (16) by following operation by fully hydration, promptly the CaO particle is introduced a shape district (A) of reactor (16) by jet pipe (14a), and water is also introduced this shape district by jet pipe (17a), thereby CaO and water droplet are met on the route of being controlled, CaO and water directly react, and the Ca (OH) that generates
2And then with reactor in the flue gas reaction of flowing and combine the SO that contains in the flue gas
2
2, according to the method for claim 1, the material that it is characterized in that the crushed CaO of containing in activating apparatus (11) is transferred to reactor (16) before, and the component with the highest CaO content is separated and be transferred to reactor (16) at second separator (13) that places activating apparatus (11) back.
3,, it is characterized in that the powdered substance that contains calcium oxide brings reactor (16) into carrier gas or vector gas according to the method for claim 1 or 2.
4,, it is characterized in that aquation begins before at reactor (16) by water vapour or water are transported in activating apparatus (11) the material stream that contains CaO afterwards according to the method for aforementioned arbitrary claim.
5, according to the method for aforementioned arbitrary claim.Be characterised in that the powdered substance that contains CaO is admitted to the central area that shape district (A) enters reactor (16) of dripping of reactor (16).Consider to obtain excellent contact between the reactant, (material) that come out from jet pipe flowed so towards flue gas (S), so that the direction of (material) stream and the speed of flue gas and powder are best.
6, according to the method for above-mentioned arbitrary claim, be characterised in that water ejects from the jet pipe (17a) on the next door that exactly is placed on powder jet pipe (14a), therefore may obtain best contact between the reactant, water and to contain the powder of CaO injected with such method so that their flow direction the direction with flue gas stream (S) is opposite substantially.
7,, be characterised in that and use a kind of mechanical activation device (preferably a kind of forcing press) in the method as activating apparatus (11) according to the method for above-mentioned arbitrary claim.
8, the equipment of cleaning flue gases, comprise the flue gas duct (a) of coming out by heating furnace (4), and change over to thus and give separator (8), this give separator separate be admitted to heating furnace (4) but not with flue gas in the absorbent of reaction of Salmon-Saxl, and with flue gas in the sulphur that contains react partially absorb the agent particle, it is characterized in that, giving separator (8) back, this equipment comprises an activating apparatus (11), therefore the material grains that this activating apparatus is given separation is crushed to littler particle, round the CaSO of CaO
4The top layer is broken and disengage the CaO that is used for hydration reaction, and this equipment comprises pipeline 14, through this pipeline the particle that contains CaO is transferred to reactor (16) and carries out hydration.This reactor (16) is placed on flue gas and gives separator (8) back on the direction of flue gas stream, this equipment also comprises jet pipe (14a), by it the CaO particle is transferred to reactor (16), and the playpipe of water (17a) be placed on above-mentioned jet pipe (14a) near.
9, equipment according to Claim 8 is characterised in that this equipment includes one second separator (13) between activating apparatus (11) and reactor (16), and the particle that only contains the highest CaO content in this case is transferred to reactor (16).
10, according to the equipment of one of aforesaid right requirement 8 or 9, be characterised in that this equipment comprises an air blast (15) or its coordinate, produce air carrier stream whereby, enter in the material component along pipeline (14).
11, according to the equipment of one of aforesaid right requirement 8 or 9 or 10, be characterised in that activating apparatus (11) comprises a forcing press.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FI890732 | 1989-02-15 | ||
| FI890732A FI83166B (en) | 1989-02-15 | 1989-02-15 | RENINGSMETOD FOER ROEKGASER OCH ANLAEGGNING FOER RENING AV ROEKGASER. |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1045927A true CN1045927A (en) | 1990-10-10 |
Family
ID=8527901
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 90101425 Pending CN1045927A (en) | 1989-02-15 | 1990-02-15 | The method and apparatus of cleaning flue gases |
Country Status (5)
| Country | Link |
|---|---|
| CN (1) | CN1045927A (en) |
| AU (1) | AU4962790A (en) |
| FI (1) | FI83166B (en) |
| WO (1) | WO1990009226A1 (en) |
| YU (1) | YU29390A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102438941A (en) * | 2008-10-13 | 2012-05-02 | 俄亥俄州立大学研究基金会 | Calcium looping process for high purity hydrogen production intergrated with capture of carbon dioxide, sulfur and halides |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1993003824A1 (en) * | 1991-08-22 | 1993-03-04 | A. Ahlstrom Corporation | Method for purification of waste gases |
| WO1994007591A1 (en) * | 1992-09-25 | 1994-04-14 | Niro A/S | Process of producing calcium hydroxide for absorption |
| FR2698287B1 (en) * | 1992-11-24 | 1995-01-20 | Stein Industrie | Method for reducing pollutant emissions in combustion installations with circulating fluidized bed. |
| SE510535C2 (en) * | 1995-01-30 | 1999-05-31 | Pronea Miljoeteknik Ab | Methods of regenerating used carbonate grains during gas purification |
| SE514592C2 (en) * | 1998-05-18 | 2001-03-19 | Flaekt Ab | Method and apparatus for flue gas purification with extinguishing lime in immediate connection with flue gas purification |
| ITMI20030765A1 (en) * | 2003-04-11 | 2004-10-12 | Gruppo Public Consult S P A | ACID GAS ABATEMENT PROCESS IN GASEOUS EFFLUENTS. |
| EP2011558B1 (en) * | 2007-05-16 | 2011-08-10 | Babcock Noell GmbH | Installation and method for removing contaminants from exhaust gas |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT371371B (en) * | 1981-08-17 | 1983-06-27 | Giesinger Ingo | METHOD FOR DESULFURING SMOKE GASES |
| AT380406B (en) * | 1983-08-16 | 1986-05-26 | Staudinger Gernot | METHOD FOR DESULFURING COMBUSTION EXHAUST GASES |
| FI78845B (en) * | 1984-11-09 | 1989-06-30 | Tampella Oy Ab | FOERFARANDE FOER AVLAEGSNANDE AV GASFORMIGA SVAVELFOERENINGAR, SAOSOM SVAVELDIOXID FRAON ROEKGASERNA FRAON EN PANNA. |
| FI76931B (en) * | 1986-12-12 | 1988-09-30 | Imatran Voima Oy | FOERFARANDE FOER RENING AV ROEKGASER. |
-
1989
- 1989-02-15 FI FI890732A patent/FI83166B/en not_active Application Discontinuation
-
1990
- 1990-02-07 WO PCT/FI1990/000037 patent/WO1990009226A1/en unknown
- 1990-02-07 AU AU49627/90A patent/AU4962790A/en not_active Abandoned
- 1990-02-14 YU YU29390A patent/YU29390A/en unknown
- 1990-02-15 CN CN 90101425 patent/CN1045927A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102438941A (en) * | 2008-10-13 | 2012-05-02 | 俄亥俄州立大学研究基金会 | Calcium looping process for high purity hydrogen production intergrated with capture of carbon dioxide, sulfur and halides |
Also Published As
| Publication number | Publication date |
|---|---|
| YU29390A (en) | 1991-10-31 |
| WO1990009226A1 (en) | 1990-08-23 |
| AU4962790A (en) | 1990-09-05 |
| FI83166B (en) | 1991-02-28 |
| FI890732A (en) | 1990-08-16 |
| FI890732A0 (en) | 1989-02-15 |
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| PB01 | Publication | ||
| C01 | Deemed withdrawal of patent application (patent law 1993) | ||
| WD01 | Invention patent application deemed withdrawn after publication |