CN112500002A - Denitration and consumption reduction system for greatly increasing yield of dry-process kiln without ammonia escape - Google Patents
Denitration and consumption reduction system for greatly increasing yield of dry-process kiln without ammonia escape Download PDFInfo
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- CN112500002A CN112500002A CN202010775990.1A CN202010775990A CN112500002A CN 112500002 A CN112500002 A CN 112500002A CN 202010775990 A CN202010775990 A CN 202010775990A CN 112500002 A CN112500002 A CN 112500002A
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- cyclone
- flue
- decomposing furnace
- kiln
- furnace
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 38
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 19
- 238000001035 drying Methods 0.000 title claims abstract description 6
- 230000009467 reduction Effects 0.000 title claims description 7
- 239000002994 raw material Substances 0.000 claims abstract description 45
- 239000000779 smoke Substances 0.000 claims abstract description 35
- 239000003245 coal Substances 0.000 claims abstract description 34
- 238000004519 manufacturing process Methods 0.000 claims abstract description 15
- 238000000197 pyrolysis Methods 0.000 claims abstract description 14
- 230000001174 ascending effect Effects 0.000 claims description 37
- 238000007599 discharging Methods 0.000 claims description 10
- 239000000428 dust Substances 0.000 claims description 9
- 239000004568 cement Substances 0.000 abstract description 30
- 239000000463 material Substances 0.000 abstract description 28
- 230000007704 transition Effects 0.000 abstract description 6
- 238000010521 absorption reaction Methods 0.000 abstract description 2
- 230000008859 change Effects 0.000 abstract description 2
- 239000003795 chemical substances by application Substances 0.000 abstract description 2
- 230000002035 prolonged effect Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 71
- 235000012054 meals Nutrition 0.000 description 17
- 238000000926 separation method Methods 0.000 description 14
- 230000000630 rising effect Effects 0.000 description 11
- 238000000034 method Methods 0.000 description 9
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 9
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 6
- 239000000292 calcium oxide Substances 0.000 description 6
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 238000005265 energy consumption Methods 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 3
- 235000011941 Tilia x europaea Nutrition 0.000 description 3
- 239000004571 lime Substances 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 238000003491 array Methods 0.000 description 2
- 229910000019 calcium carbonate Inorganic materials 0.000 description 2
- 239000004927 clay Substances 0.000 description 2
- 239000002989 correction material Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- -1 mineralizer Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
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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
- C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
- C04B7/44—Burning; Melting
-
- 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
- C04B7/43—Heat treatment, e.g. precalcining, burning, melting; Cooling
-
- 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
- F27D13/00—Apparatus for preheating charges; Arrangements for preheating charges
-
- 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
-
- 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
- F27D2017/009—Cyclone for separating fines from gas
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Ceramic Engineering (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Organic Chemistry (AREA)
- Furnace Details (AREA)
Abstract
The invention discloses a system for greatly increasing production of a dry-process kiln and reducing denitration and consumption without ammonia escape, which relates to the technical field of cement production, and is characterized in that a pyrolysis furnace, a C6 cyclone cylinder and a C0-level cyclone cylinder are additionally arranged on the basis of a preheater of an original dry-process cement kiln production line, so that materials can be decomposed by 100%, the heat consumption of the system is reduced, the efficiency of a rotary kiln is improved, the yield is improved, the coal consumption is reduced, a denitration agent is not used when the emission index of NOX smoke is less than 200mg/m3, and the denitration without ammonia escape is really realized. The invention changes the original raw material fed into the rotary kiln from C5 into C6 to feed into the kiln by adding the primary C6 cyclone, so that the raw material is completely decomposed outside the kiln and then is fed into the kiln, the temperature of the raw material is increased from 860 ℃ to 870 ℃ to 1000 ℃ to 1100 ℃, the heat absorption time of the raw material in the kiln is reduced, the transition zone is shortened by phase change, the burning zone is prolonged, and the yield of the production line can be greatly increased.
Description
Technical Field
The invention relates to the technical field of cement production, in particular to a denitration and consumption reduction system capable of greatly increasing yield of a dry-process kiln without ammonia escape.
Background
The existing dry-method cement production line mainly produces cement clinker, and does not produce other accessory products. The dry production line is developed in China for more than half a century, the dry production line technology is continuously improved, and the yield and the energy consumption of the clinker reach a higher level.
The existing dry cement production line has the following defects:
firstly, heat exchange is carried out between flue gas in a decomposing furnace and raw materials, but the heat exchange efficiency of the existing preheater system is developed to reach a certain bottleneck, and the requirement of lower energy consumption is continuously improved;
secondly, because the temperature of the raw materials entering the kiln is 870 ℃ for 860 ℃, a longer transition zone is needed in the kiln after the raw materials enter the kiln, and the raw materials in the kiln absorb heat to 1300 ℃ for 1200 ℃, and then enter the burning zone, the utilization rate of the kiln is relatively low.
③ during the preparation of cement clinker, a large amount of NO is generatedXThe NOx is reduced by spraying ammonia water by an SNCR system, and ammonia generated by the ammonia water escapes to pollute the environment.
Disclosure of Invention
The invention provides a denitration and consumption reduction system for greatly increasing yield of a dry-method kiln without ammonia escape.
In order to achieve the purpose, the invention adopts the following technical scheme:
a denitration and consumption reduction system for greatly increasing yield of a dry kiln without ammonia escape comprises a decomposing furnace, wherein the decomposing furnace is connected with a five-stage preheating system, a C0 cyclone cylinder with the lower part discharging gas is arranged at the top end of the five-stage preheating system, the feeding end of a CO cyclone cylinder is communicated with an ascending flue of a C1 cyclone cylinder in the five-stage preheating system, the ascending flue of the C1 cyclone cylinder is connected with a raw material source, the discharging end of the CO cyclone cylinder is communicated with the ascending flue of a C2 cyclone cylinder in the five-stage preheating system, the lower end of the decomposing furnace is connected with a smoke chamber, the gas outlet end of the smoke chamber is connected with the lower end of the pyrolyzing furnace through a pipeline, the upper end of the pyrolyzing furnace is connected with a decomposing furnace raw material mill through a pipeline, the smoke chamber is also connected with the feeding end of the C6 cyclone cylinder through a pipeline, the discharging end of the lower end of the C6 cyclone cylinder is connected with the smoke chamber, the lower end of the decomposing furnace is also connected with the pipeline, the gas outlet end of the C6 cyclone cylinder is connected with the decomposing furnace, and a lean coal burner is also arranged between the C6 cyclone cylinder and the decomposing furnace.
Furthermore, a coal inlet is arranged at the upper end of the pyrolysis furnace.
Further, the five-stage preheating system comprises a C1 cyclone, a C2 cyclone, a C3 cyclone, a C4 cyclone and a C5 cyclone, the gas outlet end of the upper end of the decomposing furnace is connected with the feed end of the C5 cyclone, the discharge end of the C5 cyclone is connected with the feed end of the C6 cyclone, the uptake of the C5 cyclone is connected with the feed end of the C4 cyclone, the discharge end of the C4 cyclone is connected with the decomposing furnace, the uptake of the C4 cyclone is connected with the feed end of the C3 cyclone, the discharge end of the C3 cyclone is communicated with the uptake of the C5 cyclone, the uptake of the C3 cyclone is connected with the feed end of the C2 cyclone, the discharge end of the C2 cyclone is communicated with the uptake of the C4 cyclone, the uptake of the C1 cyclone is communicated with the feed end of the C1 cyclone, the C1 of the C3 cyclone is communicated with the discharge end of the C3 cyclone, the ascending flue of the C1 cyclone is connected with the feed end of the C0 cyclone, the discharge end of the lower end of the C0 cyclone is communicated with the ascending flue of the C2 cyclone, and the ascending flue of the C1 cyclone is connected with a raw material source.
Further, the lower air outlet end of the C0 cyclone is connected with a waste heat boiler.
Furthermore, the C0 cyclone comprises a cylinder body, a cyclone dust collector is arranged at the upper end of the cylinder body, the air inlet end of the cyclone dust collector is communicated with the uptake flue, the air outlet end of the cyclone dust collector is communicated with the air outlet pipe, a discharge pipe is arranged at the lower end of the cylinder body, and a plurality of air guide blades are arranged between the uptake flue and the cyclone dust collector.
Furthermore, the air guide blades are arranged linearly.
Further, each air guide blade is installed between the uptake flue and the cyclone dust collector through a shaft column.
Furthermore, a plurality of stationary blades are arranged in the air outlet pipe.
Further, the stationary blades are linearly arranged in the air outlet pipe.
Further, the discharge hole is conical.
The invention has the following advantages: the invention heats the lime raw meal from ambient temperature to around 750℃ through the C0 to C4 cyclones. The addition of the C0 increases the primary heat exchange of the whole system, further improves the heat exchange efficiency of raw meal, and reduces the energy consumption of the whole device. Through the C6 cyclone, the transition zone of the rotary kiln is shortened, the burning zone is lengthened, the material can be 100% decomposed, and the yield is improved. The load of the rotary kiln is reduced; and carbon monoxide is generated by the lean coal burner, and nitrogen oxides generated in the decomposition process are converted into nitrogen in the advancing process of the carbon monoxide, so that the denitration function of the system is realized.
Drawings
FIG. 1 is a schematic structural view of example 1 of the present invention;
FIG. 2 is a schematic structural view of embodiment 1 of the present invention;
FIG. 3 is a schematic view of the C0 cyclone according to the present invention.
In the figure: 1. the device comprises a decomposing furnace, 2, a smoke chamber, 3, a rotary kiln, 4, a pyrolyzing furnace, 5, a C6 cyclone cylinder, 6, a C0 cyclone cylinder, 601, a cylinder body, 602, a cyclone dust collector, 603, an ascending flue, 604, air guide blades, 605, an adjusting screw, 606, an air outlet pipe, 607, a stationary blade, 608, a discharge pipe, 7, a C1 cyclone cylinder, 8, a C2 cyclone cylinder, 9, a C3 cyclone cylinder, 10, a C4 cyclone cylinder and 11, a C5 cyclone cylinder.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "front", "rear", "left", "right", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention.
Example 1:
referring to fig. 1, a system for greatly increasing yield of a dry kiln without ammonia escape, including a decomposing furnace 1, wherein the decomposing furnace 1 is connected with a five-stage preheating system, a C0 cyclone 6 discharging gas at the lower part is arranged at the top end of the five-stage preheating system, the feed end of the CO cyclone is communicated with the uptake of a C1 cyclone 7 in the five-stage preheating system, the uptake of the C1 cyclone 7 is connected with a raw material source, the discharge end of the CO cyclone is communicated with the uptake of a C2 cyclone 8 in the five-stage preheating system, the lower end of the decomposing furnace 1 is connected with a smoke chamber 2, the gas outlet end of the smoke chamber 2 is connected with the lower end of a pyrolyzing furnace 4 through a pipeline, the upper end of the pyrolyzing furnace 4 is connected with the decomposing furnace 1 through a pipeline, the lower end of the pyrolyzing furnace 4 is connected with a raw material mill, the smoke chamber 2 is also connected with the feed end of a C6 cyclone 5 through a pipeline, the discharge end of the lower end of the C6 cyclone cylinder 5 is connected with the smoke chamber 2 through a pipeline, the lower end of the decomposing furnace 1 is also connected with the pipeline, the gas outlet end of the C6 cyclone cylinder 5 is connected with the decomposing furnace 1, and a lean coal burner is also arranged between the C6 cyclone cylinder 5 and the decomposing furnace 1.
And a coal inlet is formed at the upper end of the pyrolysis furnace 4. The pyrolysis furnace 4 is supplied with coal and coal gangue through a coal inlet.
The five-stage preheating system comprises a C1 cyclone 7, a C2 cyclone 8, a C3 cyclone 9, a C4 cyclone 10 and a C5 cyclone 1, wherein the gas outlet end of the upper end of the decomposing furnace 1 is connected with the feed end of the C5 cyclone 1, the discharge end of the C5 cyclone 1 is connected with the feed end of the C6 cyclone 5, the ascending flue of the C5 cyclone 1 is connected with the feed end of the C4 cyclone 10, the discharge end of the C4 cyclone 10 is connected with the decomposing furnace 1, the ascending flue of the C4 cyclone 10 is connected with the feed end of the C3 cyclone 9, the discharge end of the C3 cyclone 9 is communicated with the ascending flue of the C5 cyclone 1, the ascending flue of the C3 cyclone 9 is connected with the feed end of the C2 cyclone 8, the discharge end of the C2 cyclone 8 is communicated with the ascending flue of the C4 cyclone 10, and the C2 flue of the C467 cyclone 1, the discharge end of the C1 cyclone 7 is communicated with the uptake flue of the C3 cyclone 9, the uptake flue of the C1 cyclone 7 is connected with the feed end of the C0 cyclone 6, the discharge end of the lower end of the C0 cyclone 6 is communicated with the uptake flue of the C2 cyclone 8, and the uptake flue of the C1 cyclone 7 is connected with a raw material source. The raw material source is a material prepared by mixing calcareous material, clay material, a small amount of correction material, mineralizer, crystal seed and the like, and coal is added during the production of the vertical kiln and is matched according to a proportion to be ground into a certain fineness. The cyclone is provided with an array of C0 cyclone 6, C1 cyclone 7, C2 cyclone 8, C3 cyclone 9, C4 cyclone 10, C5 cyclone 1 and C6 cyclone 5.
Referring to fig. 3, the C0 cyclone 6 includes a cylinder 601, a cyclone 602 is installed at the upper end of the cylinder 601, an air inlet end of the cyclone 602 is communicated with an uptake flue, an air outlet end of the cyclone 602 is communicated with an air outlet pipe 606, a discharge pipe 608 is installed at the lower end of the cylinder 601, and a plurality of wind guide blades 604 are installed between the uptake flue and the cyclone 602. The wind guide blades 604 are arranged linearly. Each of the air guide blades 604 is installed between the uptake duct and the cyclone 602 by an adjusting screw 605. A plurality of stationary vanes 607 are arranged in the air outlet pipe 606. The stationary blades 607 are linearly arranged in the outlet duct 606. The discharge hole is conical. The C0 cyclone 6 further improves the efficiency of gas-material separation by adopting a mode of discharging air from the lower part. And the air guide blade 604 with adjustable angle is arranged at the joint of the uptake flue and the cyclone dust collector 602, so that the air inlet angle of the uptake flue can be adjusted, and the gas-material separation efficiency is further improved.
When the cement raw material heat exchanger is used, cement raw material enters a CO cyclone along with hot gas through an ascending flue of a C1 cyclone 7, the hot gas and cement raw material in the CO cyclone are subjected to heat exchange, the hot gas in the C0 cyclone 6 is subjected to gas-material separation, the hot gas in the C0 cyclone 6 enters a waste heat boiler through a gas outlet at the lower part, the cement raw material subjected to primary heating enters a C1 cyclone 7 through an ascending flue of a C2 cyclone 8 and is subjected to heat exchange with the cement raw material subjected to primary heating, the hot gas in the C1 cyclone 7 is subjected to gas-material separation, the hot gas in a C1 cyclone 7 enters a C0 cyclone 6 through an ascending flue of a C1 cyclone 7, the cement raw material subjected to secondary heating enters a C2 cyclone 8 through an ascending flue of a C3 cyclone 9, the hot gas and the cement raw material in the C2 cyclone 8 are subjected to third heat exchange, the gas-material separation in the C2 cyclone 8, hot gas in a C2 cyclone 8 enters a C1 cyclone 7 through a rising flue of a C2 cyclone 8, cement raw meal heated for three times enters a C3 cyclone 9 through a rising flue of a C4 cyclone 10, the hot gas and the cement raw meal are subjected to fourth heat exchange in the C3 cyclone 9, the hot gas is subjected to gas-material separation in the C3 cyclone 9, the hot gas in the C3 cyclone 9 enters a C2 cyclone 8 through a rising flue of the C3 cyclone 9, the cement raw meal heated for four times enters a C4 cyclone 10 through a rising flue of a C5 cyclone 1, the hot gas and the cement raw meal are subjected to fifth heat exchange in the C4 cyclone 10, the hot gas is subjected to gas-material separation in the C4 cyclone 10, the hot gas in the C4 cyclone 10 enters a C3 cyclone 9 through a rising flue of the C4 cyclone 10, the raw meal heated for five times reaches about 750 ℃, and the hot gas directly enters a decomposing furnace 1 to be decomposed again, calcium carbonate is pyrolyzed into calcium oxide, hot gas in a decomposing furnace 1 enters the decomposing furnace 1 from the upper end of the decomposing furnace 1 from the feed end of a C5 cyclone 1, partial raw materials in the powder are decomposed into calcium oxide again by remixing and contacting the hot gas and the powder in the C5 cyclone 1, the calcium oxide is separated from the gas and the material in the C5 cyclone 1, the hot gas in the C5 cyclone 1 enters a C4 cyclone 10 through an ascending flue of the C5 cyclone 1, the C5 cyclone 1 simultaneously sends a mixture of partial raw materials and clinker generated in the decomposing furnace 1 into a connecting pipeline between the C6 cyclone 5 and a smoke chamber 2, the connecting pipeline of the smoke chamber 2 sends the hot gas in a tail smoke chamber 2 of a rotary kiln 3 into the C6 cyclone 5, the temperature of the hot gas is about 1150 ℃, so that the mixture decomposed in the decomposing furnace 1 reaches 1100 ℃ after being heated by the hot gas at 1150 ℃, and then the gas in the C6 cyclone 5 is separated, the hot gas in the C6 cyclone 5 is sent back to the decomposing furnace 1 through a pipeline, and a lean coal burner is additionally arranged on the pipeline, because the content of oxygen in the hot gas in the C6 cyclone 5 is only about 3%, coal in the lean coal burner is burnt in the gas with the oxygen content of 3%, the coal is not burnt sufficiently to generate carbon monoxide gas, and the carbon monoxide converts nitrogen oxide generated in the decomposing process into nitrogen gas in the advancing process, thereby realizing the denitration function of the system.
The lime raw meal is heated from ambient temperature to around 750℃ by passing from the C0 cyclone 6 to the C4 cyclone 10. The addition of the C0 increases the primary heat exchange of the whole system, further improves the heat exchange efficiency of raw meal, and reduces the energy consumption of the whole device.
Through the C6 cyclone 5, the transition zone of the rotary kiln 3 is shortened, the burning zone is lengthened, the material can be 100% decomposed, and the yield is improved. The load of the rotary kiln 3 is reduced.
Example 2:
referring to fig. 2, a system for greatly increasing yield of a dry kiln without ammonia escape, including a decomposing furnace 1, wherein the decomposing furnace 1 is connected with a five-stage preheating system, a C0 cyclone 6 discharging gas at the lower part is arranged at the top end of the five-stage preheating system, the feed end of the CO cyclone is communicated with the uptake of a C1 cyclone 7 in the five-stage preheating system, the uptake of the C1 cyclone 7 is connected with a raw material source, the discharge end of the CO cyclone is communicated with the uptake of a C2 cyclone 8 in the five-stage preheating system, the lower end of the decomposing furnace 1 is connected with a smoke chamber 2, the gas outlet end of the smoke chamber 2 is connected with the lower end of a pyrolyzing furnace 4 through a pipeline, the upper end of the pyrolyzing furnace 4 is connected with the decomposing furnace 1 through a pipeline, the lower end of the pyrolyzing furnace 4 is connected with a raw material mill, the smoke chamber 2 is also connected with the feed end of a C6 cyclone 5 through a pipeline, the discharge end of the lower end of the C6 cyclone cylinder 5 is connected with the smoke chamber 2 through a pipeline, the lower end of the decomposing furnace 1 is also connected with the pipeline, the gas outlet end of the C6 cyclone cylinder 5 is connected with the decomposing furnace 1, and a lean coal burner is also arranged between the C6 cyclone cylinder 5 and the decomposing furnace 1. The two arrays of the C0 cyclone 6, the C1 cyclone 7, the C2 cyclone 8, the C3 cyclone 9, the C4 cyclone 10, the C5 cyclone 1 and the C6 cyclone 5 are arranged on the cyclone. The two rows of C0 cyclone 6, C1 cyclone 7, C2 cyclone 8, C3 cyclone 9, C4 cyclone 10, C5 cyclone 1 and C6 cyclone 5 are arranged at two sides of the decomposing furnace 1.
The smoke chamber is connected with the feeding end of a C6 cyclone cylinder through a pipeline, the discharging end of the lower end of the C6 cyclone cylinder 5 is connected with the smoke chamber 2 through a pipeline, the lower end of the decomposing furnace 1 is also connected with the pipeline, the gas outlet end of the C6 cyclone cylinder 5 is connected with the decomposing furnace 1, and a lean coal burner is further arranged between the C6 cyclone cylinder 5 and the decomposing furnace 1.
The end of giving vent to anger of smoke chamber 2 is connected with pyrolysis oven 4 through the pipeline, pyrolysis oven 4 upper end is connected with dore furnace 1 through the pipeline, pyrolysis oven 4 lower extreme is connected with the raw meal mill. And a coal inlet is formed at the upper end of the pyrolysis furnace 4. The pyrolysis furnace 4 is supplied with coal and coal gangue through a coal inlet.
The five-stage preheating system comprises a C1 cyclone 7, a C2 cyclone 8, a C3 cyclone 9, a C4 cyclone 10 and a C5 cyclone 1, wherein the gas outlet end of the upper end of the decomposing furnace 1 is connected with the feed end of the C5 cyclone 1, the discharge end of the C5 cyclone 1 is connected with the feed end of the C6 cyclone 5, the ascending flue of the C5 cyclone 1 is connected with the feed end of the C4 cyclone 10, the discharge end of the C4 cyclone 10 is connected with the decomposing furnace 1, the ascending flue of the C4 cyclone 10 is connected with the feed end of the C3 cyclone 9, the discharge end of the C3 cyclone 9 is communicated with the ascending flue of the C5 cyclone 1, the ascending flue of the C3 cyclone 9 is connected with the feed end of the C2 cyclone 8, the discharge end of the C2 cyclone 8 is communicated with the ascending flue of the C4 cyclone 10, and the C2 flue of the C467 cyclone 1, the discharge end of the C1 cyclone 7 is communicated with the uptake flue of the C3 cyclone 9, the uptake flue of the C1 cyclone 7 is connected with the feed end of the C0 cyclone 6, the discharge end of the lower end of the C0 cyclone 6 is communicated with the uptake flue of the C2 cyclone 8, and the uptake flue of the C1 cyclone 7 is connected with a raw material source. The raw material source is a material prepared by mixing calcareous material, clay material, a small amount of correction material, mineralizer, crystal seed and the like, and coal is added during the production of the vertical kiln and is matched according to a proportion to be ground into a certain fineness. The two arrays of the C0 cyclone 6, the C1 cyclone 7, the C2 cyclone 8, the C3 cyclone 9, the C4 cyclone 10, the C5 cyclone 1 and the C6 cyclone 5 are arranged on the cyclone. The two rows of C0 cyclone 6, C1 cyclone 7, C2 cyclone 8, C3 cyclone 9, C4 cyclone 10, C5 cyclone 1 and C6 cyclone 5 are arranged at two sides of the decomposing furnace 1.
Referring to fig. 3, the C0 cyclone 6 includes a cylinder 601, a cyclone 602 is installed at the upper end of the cylinder 601, an air inlet end of the cyclone 602 is communicated with an uptake flue, an air outlet end of the cyclone 602 is communicated with an air outlet pipe 606, a discharge pipe 608 is installed at the lower end of the cylinder 601, and a plurality of wind guide blades 604 are installed between the uptake flue and the cyclone 602. The wind guide blades 604 are arranged linearly. Each of the air guide blades 604 is installed between the uptake duct and the cyclone 602 by an adjusting screw 605. A plurality of stationary vanes 607 are arranged in the air outlet pipe 606. The stationary blades 607 are linearly arranged in the outlet duct 606. The discharge hole is conical. The C0 cyclone 6 further improves the efficiency of gas-material separation by adopting a mode of discharging air from the lower part. And the air guide blade 604 with adjustable angle is arranged at the joint of the uptake flue and the cyclone dust collector 602, so that the air inlet angle of the uptake flue can be adjusted, and the gas-material separation efficiency is further improved.
When the cement raw material heat exchanger is used, cement raw material enters a CO cyclone along with hot gas through an ascending flue of a C1 cyclone 7, the hot gas and cement raw material in the CO cyclone are subjected to heat exchange, the hot gas in the C0 cyclone 6 is subjected to gas-material separation, the hot gas in the C0 cyclone 6 enters a waste heat boiler through a gas outlet at the lower part, the cement raw material subjected to primary heating enters a C1 cyclone 7 through an ascending flue of a C2 cyclone 8 and is subjected to heat exchange with the cement raw material subjected to primary heating, the hot gas in the C1 cyclone 7 is subjected to gas-material separation, the hot gas in a C1 cyclone 7 enters a C0 cyclone 6 through an ascending flue of a C1 cyclone 7, the cement raw material subjected to secondary heating enters a C2 cyclone 8 through an ascending flue of a C3 cyclone 9, the hot gas and the cement raw material in the C2 cyclone 8 are subjected to third heat exchange, the gas-material separation in the C2 cyclone 8, hot gas in a C2 cyclone 8 enters a C1 cyclone 7 through a rising flue of a C2 cyclone 8, cement raw meal heated for three times enters a C3 cyclone 9 through a rising flue of a C4 cyclone 10, the hot gas and the cement raw meal are subjected to fourth heat exchange in the C3 cyclone 9, the hot gas is subjected to gas-material separation in the C3 cyclone 9, the hot gas in the C3 cyclone 9 enters a C2 cyclone 8 through a rising flue of the C3 cyclone 9, the cement raw meal heated for four times enters a C4 cyclone 10 through a rising flue of a C5 cyclone 1, the hot gas and the cement raw meal are subjected to fifth heat exchange in the C4 cyclone 10, the hot gas is subjected to gas-material separation in the C4 cyclone 10, the hot gas in the C4 cyclone 10 enters a C3 cyclone 9 through a rising flue of the C4 cyclone 10, the raw meal heated for five times reaches about 750 ℃, and the hot gas directly enters a decomposing furnace 1 to be decomposed again, calcium carbonate is pyrolyzed into calcium oxide, hot gas in a decomposing furnace 1 enters the decomposing furnace 1 from the upper end of the decomposing furnace 1 from the feed end of a C5 cyclone 1, partial raw materials in the powder are decomposed into calcium oxide again by remixing and contacting the hot gas and the powder in the C5 cyclone 1, the calcium oxide is separated from the gas and the material in the C5 cyclone 1, the hot gas in the C5 cyclone 1 enters a C4 cyclone 10 through an ascending flue of the C5 cyclone 1, the C5 cyclone 1 simultaneously sends a mixture of partial raw materials and clinker generated in the decomposing furnace 1 into a connecting pipeline between the C6 cyclone 5 and a smoke chamber 2, the connecting pipeline of the smoke chamber 2 sends the hot gas in a tail smoke chamber 2 of a rotary kiln 3 into the C6 cyclone 5, the temperature of the hot gas is about 1150 ℃, so that the mixture decomposed in the decomposing furnace 1 reaches 1100 ℃ after being heated by the hot gas at 1150 ℃, and then the gas in the C6 cyclone 5 is separated, the hot gas in the C6 cyclone 5 is sent back to the decomposing furnace 1 through a pipeline, and a lean coal burner is additionally arranged on the pipeline, because the content of oxygen in the hot gas in the C6 cyclone 5 is only about 3%, coal in the lean coal burner is burnt in the gas with the oxygen content of 3%, the coal is not burnt sufficiently to generate carbon monoxide gas, and the carbon monoxide converts nitrogen oxide generated in the decomposing process into nitrogen gas in the advancing process, thereby realizing the denitration function of the system.
The lime raw meal is heated from ambient temperature to around 750℃ by passing from the C0 cyclone 6 to the C4 cyclone 10. The addition of the C0 increases the primary heat exchange of the whole system, further improves the heat exchange efficiency of raw meal, and reduces the energy consumption of the whole device.
Through the C6 cyclone 5, the transition zone of the rotary kiln 3 is shortened, the burning zone is lengthened, the material can be 100% decomposed, and the yield is improved. The load of the rotary kiln 3 is reduced.
The invention adds the pyrolysis furnace, the C6 cyclone cylinder and the C0 cyclone cylinder on the basis of the preheater of the original dry-method cement kiln production line, so that the material can be decomposed by 100 percent, the heat consumption of the system is reduced, the efficiency of the rotary kiln is improved, the yield is improved, the coal consumption is reduced, no denitrifier is used when the NOx flue gas emission index is less than 200mg/m3, and the denitration without ammonia escape is really realized.
In the invention, the lower end of the decomposing furnace is connected with the smoke chamber, the upper opening of the smoke chamber is provided with a pipeline connected with the pyrolyzing furnace, a pyrolysis gas pipeline at the upper end of the pyrolyzing furnace is connected with the tertiary air pipe and the tertiary air distributing inlet of the decomposing furnace, and pulverized coal (coal gangue, domestic garbage or municipal sludge) enters the pyrolyzing furnace through the feeding device. Transferring the bottom tailings of the pyrolysis furnace to a raw material mill; the upper opening of the smoke chamber is provided with a hot air flue connected with an air inlet of a C6 cyclone cylinder, and the blanking of C5 enters the smoke chamber through a material scattering device and is connected with a rising flue of C6; the C6 cyclone is fed into the smoke chamber, the hot smoke outlet of the C6 cyclone is connected with the cone of the decomposing furnace, and an oxygen-deficient burner is arranged between the hot smoke pipelines connected with the C6 cyclone and the cone of the decomposing furnace; the original preheater C1 outlet uptake flue is connected with an added C0 stage air duct.
The system changes the original raw material fed into the rotary kiln from C5 into C6 to be fed into the kiln by adding the primary C6 cyclone, so that the raw material is completely decomposed outside the kiln and then is fed into the kiln, the temperature of the raw material is increased from 860 ℃ to 870 ℃ to 1000 ℃ to 1100 ℃, the heat absorption time of the raw material in the kiln is reduced, the transition zone is shortened by phase change, the burning zone is prolonged, and the yield of a production line can be greatly increased.
The invention adds the C6 cyclone, the connecting pipe between the hot smoke outlet of the C6 cyclone and the cone of the decomposing furnace is provided with the oxygen-deficient burner, and a longer NOx reducing region is formed in the cone of the decomposing furnace and the hot air pipeline connected with the cone of the decomposing furnace by combining the original staged combustion, so that the reducing region not only can better reduce the fuel type NOx generated in the kiln, but also can reduce the fuel type NOx generated by burning the pulverized coal; the combustible reducing gas generated by the newly added pyrolysis furnace can reduce part of NOx newly generated by burning the pulverized coal on the upper part of the tertiary air pipe, and the system does not use a denitrifying agent, can control the NOx to be less than 200mg/m3, and really realizes the denitration without ammonia escape.
According to the system, a set of C0-level cyclone cylinder is additionally arranged on the C1 cyclone cylinder, the cyclone cylinder adopts a high-efficiency resistance-reducing cyclone cylinder, the maximum efficiency of the 1-level cyclone cylinder is increased, the heat utilization rate of the preheater is improved, the temperature of waste gas discharged by the C0-level cyclone cylinder of the preheater is reduced to 260-level-270 ℃ from the original 320-level-330 ℃, and the burnout rate of pulverized coal in the decomposing furnace can be improved by expanding the furnace volume of the decomposing furnace. The system can greatly reduce coal consumption.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.
Claims (7)
1. A dry-process kiln greatly-increased production denitration and consumption reduction system without ammonia escape is characterized in that: the device comprises a decomposing furnace (1), wherein the decomposing furnace (1) is connected with a five-stage preheating system, a C0 cyclone (6) discharging gas at the lower part is arranged at the top end of the five-stage preheating system, the feeding end of the CO cyclone is communicated with the uptake flue of a C1 cyclone (7) in the five-stage preheating system, the uptake flue of the C1 cyclone (7) is connected with a raw material source, the discharging end of the CO cyclone is communicated with the uptake flue of a C2 cyclone (8) in the five-stage preheating system, the lower end of the decomposing furnace (1) is connected with a smoke chamber (2), the gas outlet end of the smoke chamber (2) is connected with the lower end of a pyrolyzing furnace (4) through a pipeline, the upper end of the pyrolyzing furnace (4) is connected with the decomposing furnace (1) through a pipeline, the lower end of the pyrolyzing furnace (4) is connected with a raw material mill, and the smoke chamber (2) is also connected with the feeding end of a C (6) cyclone (5) through a, and the discharge end at the lower end of the C (6) cyclone cylinder (5) is connected with the smoke chamber (2) through a pipeline. The gas outlet end of the C (6) cyclone cylinder (5) is connected with the decomposing furnace (1), the lower end of the decomposing furnace (1) is also connected with the pipeline, and a lean coal burner is also arranged between the C (6) cyclone cylinder (5) and the decomposing furnace (1).
2. The system for greatly increasing yield of denitration and consumption reduction without ammonia escape in the dry kiln according to claim 1, characterized in that a coal inlet is arranged at the upper end of the pyrolysis furnace (4).
3. The system for greatly increasing production without ammonia escape and reducing the NOx and consumption of a dry kiln according to claim 1, wherein the five-stage preheating system comprises a C1 cyclone (7), a C2 cyclone (8), a C3 cyclone (9), a C4 cyclone (10) and a C5 cyclone (1), the air outlet end of the upper end of the decomposing furnace (1) is connected with the feed end of the C5 cyclone (1), the discharge end of the C5 cyclone (1) is connected with the feed end of the C6 cyclone (5), the ascending flue of the C5 cyclone (1) is connected with the feed end of the C4 cyclone (10), the discharge end of the C4 cyclone (10) is connected with the decomposing furnace (1), the ascending flue of the C4 cyclone (10) is connected with the feed end of the C3 cyclone (9), the discharge end of the C3 cyclone (9) is communicated with the ascending flue of the C5), the ascending flue of the C3 cyclone (9) is connected with the feed end of the C2 cyclone (8), the discharge end of the C2 cyclone (8) is communicated with the ascending flue of the C4 cyclone (10), the ascending flue of the C2 cyclone (8) is connected with the feed end of the C1 cyclone (7), the discharge end of the C1 cyclone (7) is communicated with the ascending flue of the C3 cyclone (9), the ascending flue of the C1 cyclone (7) is connected with the feed end of the C0 cyclone (6), the discharge end of the lower end of the C0 cyclone (6) is communicated with the ascending flue of the C2 cyclone (8), and the ascending flue of the C1 cyclone (7) is connected with a raw material source.
4. The system for greatly increasing yield, denitrating and reducing consumption of ammonia by a dry kiln according to claim 3, characterized in that the C0 cyclone (6) comprises a cylinder body (601), a cyclone (602) is arranged at the upper end of the cylinder body (601), the air inlet end of the cyclone (602) is communicated with an uptake flue, the air outlet end of the cyclone (602) is communicated with an air outlet pipe (606), a discharge pipe (608) is arranged at the lower end of the cylinder body (601), and a plurality of air guide blades (604) are arranged between the uptake flue and the cyclone (602).
5. The system for greatly increasing yield, denitrating and reducing consumption of ammonia escape in the dry kiln according to claim 4, characterized in that the air guide blades (604) are linearly arranged.
6. The system for greatly increasing yield, denitrating and reducing consumption of ammonia escape in the dry kiln according to claim 4, wherein each air guide blade (604) is installed between the uptake flue and the cyclone dust collector (602) through an adjusting screw (605).
7. The system for greatly increasing yield, denitrating and reducing consumption of ammonia escape in the dry kiln according to claim 4, characterized in that a plurality of stationary blades (607) are arranged in the air outlet pipe (606).
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| CN213037673U (en) * | 2020-08-05 | 2021-04-23 | 山东卓昶节能科技有限公司 | Denitration and consumption reduction system for greatly increasing yield of dry-process kiln without ammonia escape |
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| JPH06287035A (en) * | 1993-03-31 | 1994-10-11 | Sumitomo Cement Co Ltd | Apparatus for burning cement clinker |
| JP2010222203A (en) * | 2009-03-25 | 2010-10-07 | Taiheiyo Cement Corp | Method for utilizing resin-based waste |
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