Treatment device and treatment method for chlorine bypass dust

Abstract

In accordance with the present invention, there is provided a treat chlorine bypass dust while preventing increases in chemical cost and concentrations of heavy metals in clinker, and ensuring stability in quality of cement. In a chlorine bypass facility 1 extracting a part G of combustion gas, while cooling it, from a kiln exhaust gas passage, which runs from an inlet end of a cement kiln to a bottom cyclone, and recovering a high chlorine concentration chlorine bypass dust D5 from the extracted gas G1, a slurry S containing chlorine bypass dust and SO2 gas or/and CO2 gas are contacted with each other to obtain solid content. The slurry containing chlorine bypass dust and an exhaust gas from the chlorine bypass facility or/and the exhaust gas from the cement kiln can be contacted with each other, and the solid content can be fed to a cement finishing process, which allows cement with low CaO and Ca(OH)2 contents and with stable property such as setting time to be produced.

Claims

1. A method of treating chlorine bypass dust in a chlorine bypass facility, the method comprising extracting a part of combustion gas, while cooling it, from a kiln exhaust gas passage, which runs from an inlet end of a cement kiln to a bottom cyclone, and recovering a chlorine bypass dust including compounds of calcium from the extracted gas, obtaining solid content by contacting a slurry including the chlorine bypass dust and a calcium compound with SO.sub.2 gas or/and CO.sub.2 gas, the SO.sub.2 gas being received from a bag filter disposed between the kiln exhaust gas passage and a dissolution tank including the slurry, the CO.sub.2 gas being exhaust gas from the cement kiln, added to the slurry via a gas introduction device separate from the kiln exhaust passage such that the SO.sub.2 or/and CO.sub.2 gas being added to the slurry separate from the chlorine bypass dust, and determining time for reacting the slurry containing the chlorine bypass dust to the SO.sub.2 gas or/and the CO.sub.2 gas by at least one selected from the group consisting of: rate of decrease in the SO.sub.2 gas or/and the CO.sub.2 gas when obtaining the solid content; pH of the slurry after being reacted with the SO.sub.2 gas or/and the CO.sub.2 gas, and chemical analysis of a concentration of calcium compounds in the chlorine bypass dust.

2. The method of treating chlorine bypass dust as claimed in claim 1, wherein said slurry containing chlorine bypass dust and an exhaust gas from the chlorine bypass facility or/and the exhaust gas from the cement kiln are contacted with each other.

3. The method of treating chlorine bypass dust as claimed in claim 1, wherein said solid content is fed to a cement finishing process.

4. The method of treating chlorine bypass dust as claimed in claim 1, wherein said solid content is obtained after controlling pH of said slurry containing the chlorine bypass dust after contacted with the SO.sub.2 gas or/and the CO.sub.2 gas.

5. The method of treating chlorine bypass dust as claimed in claim 4, wherein said pH of the slurry after being contacted with the SO.sub.2 gas or/and the CO.sub.2 gas is between 7.0 and 10.5.

6. The method of treating chlorine bypass dust as claimed in claim 2, wherein said solid content is fed to a cement finishing process.

7. The method of treating chlorine bypass dust as claimed in claim 2, wherein said solid content is obtained after controlling pH of said slurry containing the chlorine bypass dust after contacted with the SO.sub.2 gas or/and the CO.sub.2 gas.

8. The method of treating chlorine bypass dust as claimed in claim 7, wherein said pH of the slurry after being contacted with the SO.sub.2 gas or/and the CO.sub.2 gas is between 7.0 and 10.5.

9. The method of treating chlorine bypass dust as claimed in claim 3, wherein said solid content is obtained after controlling pH of said slurry containing the chlorine bypass dust after being contacted with the SO.sub.2 gas or/and the CO.sub.2 gas.

10. The method of treating chlorine bypass dust as claimed in claim 9, wherein said pH of the slurry after contacted with the SO.sub.2 gas or/and the CO.sub.2 gas is controlled 7.0 or more and 10.5 or less.

11. The method of treating chlorine bypass dust as claimed in claim 1, wherein SO.sub.2 gas and CO.sub.2 gas are added to the slurry.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

(1) FIG. 1 is a schematic view showing the first embodiment of a chlorine bypass dust treatment apparatus according to the present invention.

(2) FIG. 2 is a schematic view showing the second embodiment of a chlorine bypass dust treatment apparatus according to the present invention.

DETAILED DESCRIPTION OF THE INVENTION

(3) Next, embodiments to carry out of the present invention will be explained in detail with reference to drawings.

(4) FIG. 1 shows a chlorine bypass facility with an apparatus for treating chlorine bypass dust according to the first embodiment of the present invention, and this chlorine bypass facility 1 comprises: a probe 3 for extracting a part G of combustion gas from a kiln exhaust gas passage, which runs from an inlet end of a cement kiln 2 to a bottom cyclone (not shown); a cyclone 4 for separating coarse powder D1 from dust included in an extracted gas G1 extracted by the probe 3; a heat exchanger 5 for cooling an extracted combustion gas G2 including fine powder D2 discharged from the cyclone 4; a bag filter 6 for collecting dust contained in an extracted gas G3 from the heat exchanger 5; a dust tank 7 for temporarily storing dusts (D3+D4) discharged from the heat exchanger 5 and bag filter 6; a dissolution reaction tank 8 for dissolving the dust (chlorine bypass dust) D5 discharged from the dust tank 7 with water and reacting the dust D5 with SO.sub.2 gas and CO.sub.2 gas; a solid/liquid separator 9 for solid/liquid separating a slurry S discharged from the dissolution reaction tank 8. The construction from the probe 3 to the dust tank 7 is the same as that of conventional chlorine bypass facilities, so that explanations thereof will be omitted.

(5) The dissolution reaction tank 8 is installed to slurry the dust D5 from the dust tank 7 with water (or hot water), and to the dissolution reaction tank 8 is supplied the exhaust gas G4 including SO.sub.2 gas from the bag filter 6 or/and the exhaust gas G5 including CO.sub.2 gas from the cement kiln 2, which allows calcium compounds contained in the slurry and SO.sub.2 gas and CO.sub.2 gas to react with each other. In this connection, as the dissolution reaction tank 8, a packed tower, a perforated-plate tower, a venturi scrubber, a spray tower, a mixing-type scrubber, a diffusion plate or the like may be used, and those may be any one of continuous type and batch type. All or a part of the exhaust gas G4 can be introduced to the dissolution reaction tank 8. It is preferable that all of the exhaust gas G4 is introduced to the dissolution reaction tank 8 because acidic gas contained in the exhaust gas G4 can be removed. On the other hand, when a part of the exhaust gas G4 is utilized, the gas G4 that is not introduced to the dissolution reaction tank 8, and a gas discharged from the dissolution reaction tank 8 are introduced to a kiln exhaust gas system such as a preheater and a preheater outlet.

(6) The solid/liquid separator 9 is installed to solid/liquid separate the slurry S, which reacted with the exhaust gas G4 and the exhaust gas G5 in the dissolution reaction tank 8. As the solid/liquid separator 9, a filter press, a centrifugal separator, a belt filter, or the like may be used.

(7) Next, the motion of the chlorine bypass facility 1 with the above-mentioned construction will be explained with reference to FIG. 1.

(8) The part G of the combustion gas extracted from the kiln exhaust gas passage, which runs from the inlet end of the cement kiln 2 to the bottom cyclone, is cooled in the probe 3 with a cooling air from a cooling fan (not shown), and fine crystals of chloride compounds are generated. These fine crystals of chloride compounds are unevenly distributed on the fine powder side of the dust included in the extracted gas G1, so that the coarse dust D1 separated by the cyclone 4 is returned to the cement kiln system.

(9) The extracted gas G2 containing the fine dust D2 separated by the cyclone 4 is introduced to the heat exchanger 5 to perform heat exchange between the extracted gas G2 and a medium. The extracted gas G3 cooled by the heat exchange is introduced to the bag filter 6, and the dust D4 contained in the extracted gas G3 is collected in the bag filter 6. The dust D4 collected in the bag filter 6 is temporarily stored together with the dust D3 discharged from the heat exchanger 5 in the dust tank 7, and is introduced to the dissolution reaction tank 8.

(10) The dust D5 introduced to the dissolution reaction tank 8 becomes the slurry S after mixed with water in the dissolution reaction tank 8. Here, in the slurry S exist CaO, CaCO.sub.3 and Ca(OH).sub.2 as calcium compounds in a mixed state, and CaO and Ca(OH).sub.2 are converted into CaSO.sub.4 and CaCO.sub.3 after reacting with SO.sub.2 contained in the exhaust gas G4 and CO.sub.2 contained in the exhaust gas G5. At the reaction between CaO, Ca(OH).sub.2 and SO.sub.2, CO.sub.2, residence time of the slurry S in the dissolution reaction tank 8 is adjusted based on rate of decrease in the exhaust gases G4, G5 (rate of decrease in the SO.sub.2, CO.sub.2 gases), pH of the slurry in the dissolution reaction tank 8, chemical analysis value of the dust D5, and so on.

(11) Next, the slurry S discharged from the dissolution reaction tank 8 is solid/liquid separated in the solid/liquid separator 9, and obtained solid content C is fed to a cement finishing process. On the other hand, in the filtrate L discharged from the solid/liquid separator 9 is included salt and heavy metals, so that treatments of the salt and the heavy metals are performed by adding them to a cement finishing process while considering quality of cement as a product. Meanwhile, the filtrate L which could not be added to the cement finishing process is released after recovering salt and heavy metals.

(12) As described above, in the present embodiment, CaO and Ca(OH).sub.2, which may affect quality of a product when added to a cement, are reacted with SO.sub.2 and CO.sub.2 gases to convert them to CaSO.sub.4 and CaCO.sub.3, and then solid content obtained by dehydration is supplied to a cement finishing process, so that it is possible to produce cement with low CaO and Ca(OH).sub.2 contents, which does not affect property such as setting time and allows the chlorine bypass dust to be treated while ensuring stability in cement quality.

(13) Next, the second embodiment of the apparatus for treating chlorine bypass dust according to the present invention will be explained with reference to FIG. 2.

(14) The present embodiment is characterized by installing a pH control tank 12 between the dissolution reaction tank 8 and solid/liquid separator 9 shown in FIG. 1, and other components are the same as those of the above-mentioned chlorine bypass facility 1. Then, in FIG. 2, to the same components as the chlorine bypass facility 1 shown in FIG. 1 are attached the same symbols, and explanations thereof will be omitted.

(15) To the pH control tank 12, from the dissolution reaction tank 8, the slurry S1 in which CaO and Ca(OH).sub.2 are converted to CaSO.sub.4 and CaCO.sub.3 by reacting SO.sub.2 and CO.sub.2, is fed, and in the pH control tank 12, pH of the slurry S1 is controlled between 7.0 and 10.5 with pH controllers such as acids (H.sub.2SO.sub.4, H.sub.2CO.sub.3, HCl etc.) and alkalis (NaOH, Ca(OH).sub.2 etc.), and heavy metals contained in a liquid of the slurry S1 precipitate.

(16) With this, in the solid/liquid separator 9 at a rear stage, when solid content C is obtained by solid/liquid separating the slurry S2 discharged from the pH control tank 12, heavy metals can unevenly be distributed on the solid content side, which can decrease chemical cost required for waste water treatment, and restrains circulation and concentration of heavy metals in the cement burning system as well.

(17) In addition, in the above embodiment, although the dissolution reaction tank 8 and the pH control tank 12 are independently installed, it is possible to perform, in a single tank, chemical reaction between the calcium compounds and SO.sub.2 gas and the pH control at the same time.

(18) Furthermore, in the above-mentioned embodiment, although the coarse powder D1 separated in the cyclone is returned to a cement kiln system, it is also possible to further classify the coarse powder, and feed divided fine powder with a predetermined chlorine content to the dissolution reaction tank 8 so as to be treated in the same manner as the dusts D3, D4. Moreover, the dusts D3, D4 can be classified further, and only fine powder may be fed to the dissolution reaction tank 8.

EXPLANATION OF REFERENCE NUMBERS

(19) 1 chlorine bypass facility 2 cement kiln 3 probe 4 cyclone 5 heat exchanger 6 bag filter 7 dust tank 8 dissolution reaction tank 9 solid/liquid separator 10 electric dust collector 12 pH control tank