CN101959824A - System and method for treating bleed gas from cement kiln - Google Patents
System and method for treating bleed gas from cement kiln Download PDFInfo
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- CN101959824A CN101959824A CN2009801066215A CN200980106621A CN101959824A CN 101959824 A CN101959824 A CN 101959824A CN 2009801066215 A CN2009801066215 A CN 2009801066215A CN 200980106621 A CN200980106621 A CN 200980106621A CN 101959824 A CN101959824 A CN 101959824A
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- withdrawing gas
- gas
- cement kiln
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- 239000004568 cement Substances 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims description 11
- 239000007789 gas Substances 0.000 claims abstract description 114
- 239000003054 catalyst Substances 0.000 claims abstract description 50
- 239000000428 dust Substances 0.000 claims abstract description 33
- 238000001816 cooling Methods 0.000 claims abstract description 14
- 239000000567 combustion gas Substances 0.000 claims abstract description 11
- 239000000463 material Substances 0.000 claims description 20
- 238000000605 extraction Methods 0.000 claims description 18
- 238000010438 heat treatment Methods 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 6
- 235000003599 food sweetener Nutrition 0.000 claims description 4
- 239000003765 sweetening agent Substances 0.000 claims description 4
- 239000000284 extract Substances 0.000 claims description 2
- 239000002957 persistent organic pollutant Substances 0.000 abstract description 15
- 239000003344 environmental pollutant Substances 0.000 abstract description 3
- 231100000719 pollutant Toxicity 0.000 abstract description 3
- 231100000572 poisoning Toxicity 0.000 abstract description 2
- 230000000607 poisoning effect Effects 0.000 abstract description 2
- 239000000523 sample Substances 0.000 abstract 2
- 230000002378 acidificating effect Effects 0.000 abstract 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 17
- 239000000460 chlorine Substances 0.000 description 16
- 229910052801 chlorine Inorganic materials 0.000 description 16
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 15
- 239000003595 mist Substances 0.000 description 8
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 7
- 238000005260 corrosion Methods 0.000 description 6
- 235000012054 meals Nutrition 0.000 description 5
- 239000010936 titanium Substances 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 4
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- 239000002574 poison Substances 0.000 description 4
- 231100000614 poison Toxicity 0.000 description 4
- 229910052719 titanium Inorganic materials 0.000 description 4
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 4
- 238000004891 communication Methods 0.000 description 3
- 239000000356 contaminant Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000010970 precious metal Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 229910052720 vanadium Inorganic materials 0.000 description 3
- RYHBNJHYFVUHQT-UHFFFAOYSA-N 1,4-Dioxane Chemical class C1COCCO1 RYHBNJHYFVUHQT-UHFFFAOYSA-N 0.000 description 2
- OGBQILNBLMPPDP-UHFFFAOYSA-N 2,3,4,7,8-Pentachlorodibenzofuran Chemical compound O1C2=C(Cl)C(Cl)=C(Cl)C=C2C2=C1C=C(Cl)C(Cl)=C2 OGBQILNBLMPPDP-UHFFFAOYSA-N 0.000 description 2
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 150000001805 chlorine compounds Chemical class 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000005755 formation reaction Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000000292 calcium oxide Substances 0.000 description 1
- 235000012255 calcium oxide Nutrition 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 150000001804 chlorine Chemical class 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 150000002927 oxygen compounds Chemical class 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 239000010948 rhodium Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/36—Manufacture of hydraulic cements in general
- C04B7/364—Avoiding environmental pollution during cement-manufacturing
-
- 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
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8678—Removing components of undefined structure
- B01D53/8687—Organic components
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
- F27B7/20—Details, accessories, or equipment peculiar to rotary-drum furnaces
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/008—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases cleaning gases
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Health & Medical Sciences (AREA)
- Ceramic Engineering (AREA)
- Materials Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental Sciences (AREA)
- Ecology (AREA)
- Structural Engineering (AREA)
- Organic Chemistry (AREA)
- Biodiversity & Conservation Biology (AREA)
- Public Health (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
A bleed gas from a cement kiln is purified with a catalyst by efficiently removing organic pollutants contained in the bleed gas, while minimizing the poisoning of the catalyst by an acidic gas. A system (1) for treating a bleed gas from a cement kiln is provided which includes: a probe (5) which bleeds a kiln discharge gas passage, which extends from the bottom of a cement kiln (4) to a lowermost-stage cyclone, of part of a combustion gas; a first heat exchanger (11) which recovers heat while cooling the bleed gas (G2) taken out by the probe (5); a bag filter (12) which separates dust from the bleed gas (G2) cooled by the first heat exchanger (11); a second heat exchanger (17) by which the bleed gas (G3) from which dust has been separated is heated with the heat recovered by the first heat exchanger (11); and a catalyst device (18) which decomposes organic pollutants contained in the bleed gas (G4) heated by the second heat exchanger (17) and removes the pollutants therefrom.
Description
Technical field
The present invention is the treatment system and the treatment process of relevant cement kiln withdrawing gas, and is particularly relevant to remove the treatment system from the contained organic pollution materials of the withdrawing gas of the kiln exhaust gas stream extraction of the cyclone to hypomere from the kiln tail of cement kiln etc.
Background technology
Past, in cement making equipment, cause among the chlorine, sulphur, alkali etc. of the reason of problems such as preheater obturation, the chlorine that particularly becomes problem is gazed at, relevant kiln exhaust gas stream from the cyclone to hypomere from the kiln tail of cement kiln is extracted the chlorine bypath system of the part of combustion gases with removal chlorine out, is used.
In this chlorine bypath system, for example, such as patent documentation 1 record, because the micro mist side at the dust that combustion gases generate that cools off extraction has chlorine to exist partially, so dust is separated into meal and micro mist by grading machine, meal is recycled to the cement kiln system, reclaims simultaneously and contain separated micro mists such as Repone K (chlorine bypass dust).
As described above all, in the chlorine bypath system,, separated in the withdrawing gas behind the dust, owing to still contain the sulfur oxide (SO that a great deal of is gaseous phase though separate, reclaim chloride dust from the combustion gases of extraction
X), so can't directly emit in atmosphere by the exhaust of chlorine bypass.In the chlorine bypass exhaust, also contain dioxan class (PCDD, PCDF, co-PCB), polychlorobiphenyl (PCB again,
S) waiting the situation of persistent organic pollutant matter (POPs) or volatile organic contaminant matter (VOC), relevant these also have necessity of suitable processing.
[patent documentation 1] international document that discloses No. 97/21638
Summary of the invention
Invent problem to be solved
Remove one of method of organic pollution materials such as POPs, VOC, the known method that the catalyst of utilization disaggregating treatment is arranged; In the chlorine bypath system, also can consider to remove organic pollution materials from chlorine bypass exhaust on exhaust channel by catalyst device is set.
But in chlorine bypass exhaust, there is volume from SO
XSour gas because these make catalyst poison reduce catalyst activity, so catalyst device, inaccessible practicability only are set on exhaust channel.From now on,, worry that then POPs, VOC in the chlorine bypass exhaust become the content increase of branchs if the situation of the recirculation of cement raw materialization by waste or turning sludge into fuel increases day by day again.Therefore, can envision from now on needs the losing activity of catalyst that causes because of sour gas suppressed, and more effectively removes organic pollution materials.
Therefore, the present invention system carries out in view of the problem points of aforementioned prior art, with when utilizing catalyst device to carry out the purifying treatment of cement kiln withdrawing gas, suppress to poison in inferior limit, and to remove the contained organic pollution materials of withdrawing gas effectively be purpose because of the catalyst that sour gas causes.
In order to solve the means of problem
Be to solve aforementioned problems, the present invention is a kind of treatment system of cement kiln withdrawing gas, it is characterized in that, is provided with: extraction sector, the part that it extracts combustion gases out from the kiln exhaust gas stream of the cyclone to hypomere from the kiln tail of cement kiln; The 1st heat exchanger, the withdrawing gas that it simultaneously cools off this extraction sector is extracted out, one side reclaims heat; Separation mechanism, it separates dust from the withdrawing gas that the 1st heat exchanger is cooled off; The 2nd heat exchanger, the heat that it utilizes aforementioned the 1st heat exchanger to be reclaimed, heating has separated the withdrawing gas of this dust; And catalyst device, it removes organic pollution materials from the withdrawing gas that the 2nd heat exchanger is heated.Again, organic substance means dioxan class (PCDD, PCDF, co-PCB), polychlorobiphenyl (PCB
S) wait persistent organic pollutant matter (POPs) or volatile organic contaminant matter (VOC).
According to the present invention, because the withdrawing gas that extraction sector is extracted out can be removed the sour gas in the withdrawing gas with the 1st heat exchanger cooling, so the catalyst poisoning that causes because of sour gas can be suppressed in the scope of hanging down.Because the withdrawing gas that will cool off is carried out reheat by the 2nd heat exchanger, be directed in catalyst device after being adjusted to the temperature that is suitable for decomposing organic pollutant matter, so can remove organic pollution materials effectively again.And then, at this moment, because the heat heating withdrawing gas that utilizes the 1st heat exchanger to be reclaimed so can apply flexibly the heat of recovery effectively and heat withdrawing gas, also can be sought the reduction of operating cost.
In the treatment system of aforementioned cement kiln withdrawing gas, can constitute aforementioned separation mechanism by dry mechanical dust collector, also can between this dry mechanical dust collector and aforementioned the 1st heat exchanger, the interpolation mechanism that sweetening agent is added in the withdrawing gas that the 1st heat exchanger is cooled off be set again.Particularly when interpolation mechanism is set,, suppress in inferior limit so the catalyst that causes because of sour gas can be poisoned owing to the sour gas that can more positively remove in the withdrawing gas.
In the treatment system of aforementioned cement kiln withdrawing gas, can constitute aforementioned separating step, in view of the above, can more positively remove the sour gas in the withdrawing gas, the catalyst that causes because of sour gas can be poisoned and suppress in inferior limit by the wet type precipitron.
In the treatment system of aforementioned cement kiln withdrawing gas, can constitute aforementioned the 1st heat exchanger, also can impose anti-corrosion processing the precipitron after the 1st heat exchanger etc. by the anti-corrosion type heat exchanger of inwall having been implemented anti-corrosion processing.Again, lining such as available fluoro-resin of anti-corrosion processing.
Moreover the treatment process of series cement kiln of the present invention withdrawing gas is characterized in that, comprises following steps: a part of extracting combustion gases out from the kiln exhaust gas stream of the cyclone to hypomere from the kiln tail of cement kiln; Simultaneously cool off the withdrawing gas of this extraction with the 1st heat exchanger, one side reclaims heat; Separate dust from the withdrawing gas of this cooling; The withdrawing gas that will separate this dust is directed into the 2nd heat exchanger, and the heat heating that utilizes aforementioned the 1st heat exchanger to be reclaimed; Withdrawing gas that should heating is directed into catalyst device, removes organic pollution materials from this withdrawing gas.According to the present invention, same with aforementioned invention, the catalyst that causes because of sour gas can be poisoned and suppress, and can remove the organic pollution materials in the chlorine bypass exhaust effectively in inferior limit.
In the treatment process of aforementioned cement kiln withdrawing gas, in aforementioned the 1st heat exchanger, the withdrawing gas of aforementioned extraction can be cooled to below 200 ℃, in view of the above, can remove the oxygen compounds of sulphur in the withdrawing gas effectively, and also can reclaim more heat from the 1st heat exchanger.Limit 20 ℃ that are about normal temperature under the cooling again.
In the treatment process of aforementioned cement kiln withdrawing gas, in aforementioned the 2nd heat exchanger, can be heated to the aforementioned withdrawing gas that has separated dust more than 150 ℃, below 500 ℃, in view of the above, in catalyst device, can decompose, remove the harmful pollutants in the withdrawing gas effectively.Again, when the temperature of withdrawing gas is lower than 150 ℃, the sufficient rate of decomposition of then difficult expectation harmful pollutants; And when being higher than 500 ℃, then have the improper situation that is produced detrimentally affect the catalyst life-span.
The invention effect
As described above all, according to the present invention, when using catalyst device that purifying treatment is carried out in the cement kiln withdrawing gas, the catalyst that causes because of sour gas can be poisoned and suppress, and can remove the organic pollution materials that is contained in withdrawing gas effectively in inferior limit.
Description of drawings
Fig. 1 is the schema of demonstration about the 1st embodiment of the treatment system of the present invention's cement kiln withdrawing gas.
Fig. 2 is the schema of demonstration about the 2nd embodiment of the treatment system of the present invention's cement kiln withdrawing gas.
Nomenclature
1: the treatment system of cement kiln withdrawing gas
2: the gas extraction unit
3: gas processing portion
4: cement kiln
5: air extractor
6: cooling fan
10: cyclone
11: the 1 heat exchangers
11a: pipeline
12: bag filter
13: the dust bucket
14: device for blowing
16: lure fan
17: the 2 heat exchangers
17a: communication pipeline
18: catalyst device
20: the treatment system of cement kiln withdrawing gas
21: the wet type precipitron
22: the circulation liquid layer
23: mist separator
Embodiment
For the optimal way that carries out an invention
Below, one side illustrates relevant the present invention's embodiment with reference to the diagram one side.
Fig. 1 is 1st embodiment of demonstration about the treatment system of cement kiln withdrawing gas of the present invention, and haply, this treatment system 1 is to be made of gas extraction unit 2 and gas processing portion 3.
The 1st heat exchanger 11 is to establish with the sour gas of removing among the withdrawing gas G2 in order to cooling withdrawing gas G2.When cooling withdrawing gas G2, to be cooled to below 200 ℃ to good.In view of the above, owing to promote the calcium component that contains in the withdrawing gas to become the reaction of branch with sulphur, so can remove sulfur oxide (SO
X).Again, when desulfidation is insufficient, also can on the pipeline 11a that links the 1st heat exchanger 11 and bag filter 12, device for blowing 14 be set, correspondingly add sweetening agent with needs.Sweetening agent can use slaked lime, unslaked lime, incinerating cement raw material (cement raw material of getting from the cyclone five equilibrium of the hypomere of preheater), coal ash etc.Again, in the 1st heat exchanger 11, be improving the solidity to corrosion to sour gas, is good with the anti-corrosion type heat exchanger that uses inwall to be coated with fluoro-resin etc.
The 2nd heat exchanger 17 is to be arranged on section before the catalyst device 18, and reheat carries out reheat to exhaust G3, in order to the temperature regulation of exhaust G3 for being suitable for the temperature of catalyst activity.Between the 2nd heat exchanger 17 and the 1st heat exchanger 11, be provided with communication pipeline 17a, and the 2nd heat exchanger 17 utilizes the hot thermal exhaust G3 that is reclaimed in the 1st heat exchanger 11 in order to the heat-transfer medium circulation.When exhaust G3 heats, should be heated to more than 150 ℃, below 500 ℃, in view of the above, can improve the efficient of in catalyst device 18, removing organic pollution materials.When the shortage of heat of the 2nd heat exchanger 17, also can on communication pipeline 17a, well heater (not shown) etc. be set, with the heating of heat-transfer medium supplementary ground again.
Below, one side simultaneously illustrates the action of relevant aforementioned processing system 1 with reference to Fig. 1.
The kiln exhaust gas stream of cyclone from the kiln tail of cement kiln 4 to hypomere, a part of extracting combustion gases out by air extractor 5, simultaneously by from the cold wind quick cooling of cooling fan 6 to as below 600～700 ℃ of chlorine compound melting point.Then, in cyclone 10, the withdrawing gas G1 that air extractor 5 is discharged is separated into the gas G2 that contains meal D1 and micro mist D2, and meal D1 loopback in the cement kiln system, is directed in the 1st heat exchanger with 250～600 ℃ withdrawing gas G2 on the other hand.
And in the 1st heat exchanger, one side is cooled to withdrawing gas G2 below 200 ℃, and one side is removed sulphur content (SOx) and sour gas.Then, in bag filter 12,, will be recovered in dust bucket 13 as chlorine bypass dust with the micro mist D2 control of dust among the gas G2.Secondly, lure the exhaust G3 that draws bag filter 12 by luring fan 16, in the 2nd heat exchanger 17 with more than 150 ℃, be carried out reheat below 500 ℃.After this, the exhaust G4 that will heat is directed in catalyst device 18, and organic pollution materials such as decomposed P OPs, VOC are with purifying exhaust gas G4.Again,, both can emit in atmosphere through vent fan (not shown) by the exhaust G5 of catalyst device 18 purifying treatment, also can be for recovery of heat loopback in the cement step.
As described above all, in the present embodiment,, remove the sour gas among the withdrawing gas G1, so poison among the catalyst device 18 that causes because of sour gas can be suppressed in low scope owing to cool off the withdrawing gas G1 that air extractors 5 are extracted out by the 1st heat exchanger 11.Again, owing to carry out reheat by the 2nd heat exchanger 17, the exhaust G3 that will cool off is directed in catalyst device 18 after being adjusted to the temperature that is suitable for decomposing organic pollutant matter, so can remove organic pollution materials effectively.In addition, when thermal exhaust G3,,, also can seek the reduction of operating cost so can effectively utilize the heat thermal exhaust G3 of recovery owing to utilize the heat that is reclaimed at the 1st heat exchanger 11.
Then, one side simultaneously illustrates the 2nd embodiment of treatment system of relevant the present invention's cement kiln withdrawing gas with reference to Fig. 2.Again, about the integrant identical with the treatment system of Fig. 1, then add same-sign among this figure, it illustrates omission.
All as shown in the drawing, this treatment system 20 in gas processing portion 3, is provided with the 1st heat exchanger 11 with withdrawing gas G2 cooling; The withdrawing gas G2 that the 1st heat exchanger 11 is cooled off carries out the wet type precipitron 21 of wet type control of dust; Lure the luring of exhaust G3 of drawing wet type precipitron 21 to fan 16; Will be by the 2nd heat exchanger 17 of the exhaust G3 heating of luring fan 16 to lure to draw; And the catalyst device 18 of the exhaust G4 that heat from the 2nd heat exchanger 17 removal organic pollution materials.Again, the structure of gas extraction unit 2 is identical with the situation of the treatment system 1 of Fig. 1.
In the aforementioned processing system 20, the withdrawing gas G1 that air extractor 5 is extracted out by system is cooled to below 200 ℃ in the 1st heat exchanger 11, after removing the contained SOx of withdrawing gas G2, and then, in wet type precipitron 21, the SOx that will residue among the withdrawing gas G2 carries out the wet type control of dust.Therefore, can more positively remove the sour gas among the withdrawing gas G2, poison among the catalyst device 18 that causes because of sour gas can be suppressed in inferior limit.
Moreover, after carrying out the wet type control of dust by wet type precipitron 21 and since in the future the exhaust G3 of self-wetted precipitron 21 with more than the 2nd heat exchanger 17 reheat to 150 ℃, below 550 ℃, then, by catalyst device 18, so can decompose, remove organic pollution materials such as POPs, VOC effectively.And then, in the 2nd heat exchanger 17, because the hot thermal exhaust G3 that utilizes the 1st heat exchanger 11 to be reclaimed so also can seek the reduction of operating cost, can obtain the action effect same with the 1st embodiment.
Claims (7)
1. the treatment system of a cement kiln withdrawing gas is characterized in that, is provided with:
Extraction sector, the part that it extracts combustion gases out from the kiln exhaust gas stream of the cyclone to hypomere from the kiln tail of cement kiln;
The 1st heat exchanger, the withdrawing gas that it simultaneously cools off this extraction sector is extracted out, one side reclaims heat;
Separation mechanism, it separates dust from the withdrawing gas that the 1st heat exchanger is cooled off;
The 2nd heat exchanger, the heat that it utilizes aforementioned the 1st heat exchanger to be reclaimed, heating has separated the withdrawing gas of this dust; And
Catalyst device, it removes organic pollution materials from the withdrawing gas that the 2nd heat exchanger is heated.
2. the treatment system of cement kiln withdrawing gas according to claim 1 is characterized in that, aforementioned separation mechanism is a dry mechanical dust collector.
3. as the treatment system of the cement kiln withdrawing gas as described in the claim 2, it is characterized in that, between aforementioned the 1st heat exchanger and aforementioned dry mechanical dust collector, be provided with the interpolation mechanism that sweetening agent is added in the withdrawing gas of being cooled off to the 1st heat exchanger.
4. the treatment system of cement kiln withdrawing gas according to claim 1 is characterized in that, aforementioned separation mechanism is the wet type precipitron.
5. the treatment process of a cement kiln withdrawing gas is characterized in that, comprises following steps:
A part of extracting combustion gases out from the kiln exhaust gas stream of the cyclone to hypomere from the kiln tail of cement kiln;
Simultaneously cool off the withdrawing gas of this extraction with the 1st heat exchanger, one side reclaims heat;
Separate dust from the withdrawing gas of this cooling;
The withdrawing gas that will separate this dust is directed into the 2nd heat exchanger, and the heat heating that utilizes aforementioned the 1st heat exchanger to be reclaimed; And
Withdrawing gas that should heating is directed into catalyst device, removes organic pollution materials from this withdrawing gas.
6. as the treatment process of the cement kiln withdrawing gas as described in the claim 5, it is characterized in that, in aforementioned the 1st heat exchanger, the withdrawing gas of aforementioned extraction is cooled to below 200 ℃.
7. as the treatment process of the cement kiln withdrawing gas as described in claim 5 or 6, it is characterized in that in aforementioned the 2nd heat exchanger, the withdrawing gas that will separate aforementioned dust is heated to more than 150 ℃, below 500 ℃.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2008-057818 | 2008-03-07 | ||
| JP2008057818 | 2008-03-07 | ||
| PCT/JP2009/053323 WO2009110356A1 (en) | 2008-03-07 | 2009-02-25 | System and method for treating bleed gas from cement kiln |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410106360.XA Division CN103933836A (en) | 2008-03-07 | 2009-02-25 | System and method for treating bleed gas from cement kiln |
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| Publication Number | Publication Date |
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| CN101959824A true CN101959824A (en) | 2011-01-26 |
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Family Applications (2)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410106360.XA Pending CN103933836A (en) | 2008-03-07 | 2009-02-25 | System and method for treating bleed gas from cement kiln |
| CN2009801066215A Pending CN101959824A (en) | 2008-03-07 | 2009-02-25 | System and method for treating bleed gas from cement kiln |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201410106360.XA Pending CN103933836A (en) | 2008-03-07 | 2009-02-25 | System and method for treating bleed gas from cement kiln |
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| Country | Link |
|---|---|
| JP (1) | JPWO2009110356A1 (en) |
| KR (1) | KR20110000620A (en) |
| CN (2) | CN103933836A (en) |
| TW (1) | TW200940158A (en) |
| WO (1) | WO2009110356A1 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102620568A (en) * | 2011-01-31 | 2012-08-01 | 太平洋水泥株式会社 | Chlorine bypass system and method for treating extracted gas from chlorine bypass |
| CN103644744A (en) * | 2013-12-25 | 2014-03-19 | 巨石集团有限公司 | Gradient kiln gas waste heat utilization method |
| CN111527363A (en) * | 2017-10-12 | 2020-08-11 | 蒂森克虏伯工业解决方案股份公司 | Method and plant for producing cement clinker or other mineral products |
| WO2024174428A1 (en) * | 2023-02-22 | 2024-08-29 | 中国中材国际工程股份有限公司 | System and method for increasing substitution rate of fossil fuels in cement industry |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JP2009298677A (en) * | 2008-06-17 | 2009-12-24 | Taiheiyo Cement Corp | System and method for treating cement kiln extraction gas |
| CN102102944A (en) * | 2009-09-07 | 2011-06-22 | 厦门热工环保系统工程有限公司 | Flue gas waste heat recovery method for rotary kiln |
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| JP5652950B2 (en) * | 2011-01-06 | 2015-01-14 | 太平洋セメント株式会社 | Chlorine bypass system and chlorine bypass extraction gas processing method |
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| AT14170U1 (en) * | 2014-05-27 | 2015-05-15 | Scheuch Gmbh | Device for producing cement clinker |
| JP6344850B2 (en) * | 2014-07-23 | 2018-06-20 | 太平洋セメント株式会社 | Cement kiln exhaust gas treatment apparatus and treatment method |
| JP2016022439A (en) * | 2014-07-23 | 2016-02-08 | 太平洋セメント株式会社 | Cement kiln exhaust gas treatment apparatus and treatment method |
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| JP2017060905A (en) * | 2015-09-24 | 2017-03-30 | 太平洋セメント株式会社 | Processing apparatus and method of cement kiln exhaust gas |
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| JP2002219335A (en) * | 2001-01-30 | 2002-08-06 | Babcock Hitachi Kk | Exhaust gas treating device |
| KR20060029135A (en) * | 2003-07-10 | 2006-04-04 | 다이헤이요 세멘토 가부시키가이샤 | Device and method for processing combustion exhaust gas |
| CN1255205C (en) * | 2003-10-31 | 2006-05-10 | 中国石油化工股份有限公司 | Method for purifying organic waste gas with high concentration |
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| KR101155844B1 (en) * | 2004-03-03 | 2012-06-21 | 쉘 인터내셔날 리써취 마트샤피지 비.브이. | A process for the high recovery efficiency of sulfur from an acid gas stream |
| KR101207958B1 (en) * | 2005-01-06 | 2012-12-04 | 가부시키가이샤 닛폰 쇼쿠바이 | Cement kiln firing waste gas treating apparatus and treating method |
| JP4664093B2 (en) * | 2005-03-01 | 2011-04-06 | 太平洋セメント株式会社 | Heat recovery device and chlorine bypass facility |
-
2009
- 2009-02-11 TW TW98104315A patent/TW200940158A/en unknown
- 2009-02-25 WO PCT/JP2009/053323 patent/WO2009110356A1/en active Application Filing
- 2009-02-25 KR KR1020107017312A patent/KR20110000620A/en not_active Application Discontinuation
- 2009-02-25 CN CN201410106360.XA patent/CN103933836A/en active Pending
- 2009-02-25 CN CN2009801066215A patent/CN101959824A/en active Pending
- 2009-02-25 JP JP2010501859A patent/JPWO2009110356A1/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102620568A (en) * | 2011-01-31 | 2012-08-01 | 太平洋水泥株式会社 | Chlorine bypass system and method for treating extracted gas from chlorine bypass |
| CN103644744A (en) * | 2013-12-25 | 2014-03-19 | 巨石集团有限公司 | Gradient kiln gas waste heat utilization method |
| CN111527363A (en) * | 2017-10-12 | 2020-08-11 | 蒂森克虏伯工业解决方案股份公司 | Method and plant for producing cement clinker or other mineral products |
| CN111527363B (en) * | 2017-10-12 | 2022-09-13 | 蒂森克虏伯工业解决方案股份公司 | Method and plant for producing cement clinker or other mineral products |
| WO2024174428A1 (en) * | 2023-02-22 | 2024-08-29 | 中国中材国际工程股份有限公司 | System and method for increasing substitution rate of fossil fuels in cement industry |
Also Published As
| Publication number | Publication date |
|---|---|
| KR20110000620A (en) | 2011-01-04 |
| JPWO2009110356A1 (en) | 2011-07-14 |
| CN103933836A (en) | 2014-07-23 |
| TW200940158A (en) | 2009-10-01 |
| WO2009110356A1 (en) | 2009-09-11 |
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