CN114409290B - Device and method for heating and modifying desulfurized ash based on blast furnace gas - Google Patents
Device and method for heating and modifying desulfurized ash based on blast furnace gas Download PDFInfo
- Publication number
- CN114409290B CN114409290B CN202111632131.8A CN202111632131A CN114409290B CN 114409290 B CN114409290 B CN 114409290B CN 202111632131 A CN202111632131 A CN 202111632131A CN 114409290 B CN114409290 B CN 114409290B
- Authority
- CN
- China
- Prior art keywords
- air
- gas
- cooling
- blast furnace
- oxidation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000034 method Methods 0.000 title claims abstract description 43
- 238000010438 heat treatment Methods 0.000 title claims abstract description 22
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 78
- 230000003647 oxidation Effects 0.000 claims abstract description 75
- 239000010881 fly ash Substances 0.000 claims abstract description 39
- 239000007789 gas Substances 0.000 claims description 100
- 238000001816 cooling Methods 0.000 claims description 84
- 239000002956 ash Substances 0.000 claims description 76
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 71
- 239000003546 flue gas Substances 0.000 claims description 71
- 239000000428 dust Substances 0.000 claims description 46
- 238000006477 desulfuration reaction Methods 0.000 claims description 43
- 230000023556 desulfurization Effects 0.000 claims description 43
- 239000002994 raw material Substances 0.000 claims description 37
- 238000007599 discharging Methods 0.000 claims description 35
- 239000000463 material Substances 0.000 claims description 32
- 238000006243 chemical reaction Methods 0.000 claims description 25
- 230000001590 oxidative effect Effects 0.000 claims description 21
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 20
- 239000000292 calcium oxide Substances 0.000 claims description 20
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 20
- 239000000047 product Substances 0.000 claims description 16
- 238000002485 combustion reaction Methods 0.000 claims description 15
- 239000002918 waste heat Substances 0.000 claims description 10
- 229910000831 Steel Inorganic materials 0.000 claims description 9
- 239000010959 steel Substances 0.000 claims description 9
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 8
- 239000002912 waste gas Substances 0.000 claims description 7
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical group C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 6
- 239000002699 waste material Substances 0.000 claims description 5
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 4
- 239000006227 byproduct Substances 0.000 claims description 3
- 239000003345 natural gas Substances 0.000 claims description 3
- 229920000742 Cotton Polymers 0.000 claims description 2
- YKTSYUJCYHOUJP-UHFFFAOYSA-N [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] Chemical compound [O--].[Al+3].[Al+3].[O-][Si]([O-])([O-])[O-] YKTSYUJCYHOUJP-UHFFFAOYSA-N 0.000 claims description 2
- 239000011449 brick Substances 0.000 claims description 2
- 238000009413 insulation Methods 0.000 claims description 2
- 230000002093 peripheral effect Effects 0.000 claims description 2
- 239000011343 solid material Substances 0.000 claims description 2
- 239000000779 smoke Substances 0.000 claims 3
- 239000004566 building material Substances 0.000 abstract description 7
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 17
- 235000010261 calcium sulphite Nutrition 0.000 description 17
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000011575 calcium Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- 239000004568 cement Substances 0.000 description 2
- 239000004567 concrete Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000006703 hydration reaction Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 238000013016 damping Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000003111 delayed effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000006056 electrooxidation reaction Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000036571 hydration Effects 0.000 description 1
- 239000011810 insulating material Substances 0.000 description 1
- 239000012774 insulation material Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000005204 segregation Methods 0.000 description 1
- 230000001568 sexual effect Effects 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Images
Classifications
-
- 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
- C04B20/00—Use of materials as fillers for mortars, concrete or artificial stone according to more than one of groups C04B14/00 - C04B18/00 and characterised by shape or grain distribution; Treatment of materials according to more than one of the groups C04B14/00 - C04B18/00 specially adapted to enhance their filling properties in mortars, concrete or artificial stone; Expanding or defibrillating materials
- C04B20/02—Treatment
- C04B20/04—Heat treatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/18—Carbonates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F11/00—Compounds of calcium, strontium, or barium
- C01F11/46—Sulfates
-
- 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
- C04B18/00—Use of agglomerated or waste materials or refuse as fillers for mortars, concrete or artificial stone; Treatment of agglomerated or waste materials or refuse, specially adapted to enhance their filling properties in mortars, concrete or artificial stone
- C04B18/04—Waste materials; Refuse
- C04B18/14—Waste materials; Refuse from metallurgical processes
-
- 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
- C04B20/00—Use of materials as fillers for mortars, concrete or artificial stone according to more than one of groups C04B14/00 - C04B18/00 and characterised by shape or grain distribution; Treatment of materials according to more than one of the groups C04B14/00 - C04B18/00 specially adapted to enhance their filling properties in mortars, concrete or artificial stone; Expanding or defibrillating materials
- C04B20/02—Treatment
- C04B20/023—Chemical treatment
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/91—Use of waste materials as fillers for mortars or concrete
Abstract
The invention relates to a device and a method for heating and modifying desulfurized fly ash based on blast furnace gas, wherein the device comprises a pretreatment device, a carbonation oxidation device and a heat exchange device, aiming at the problems that the desulfurized fly ash by a dry method and a semi-dry method has unstable performance, the strength of produced building materials is low, and resource utilization is difficult.
Description
Technical Field
The invention belongs to the field of industrial solid waste comprehensive treatment, mainly relates to a method for treating calcium-based desulfurized fly ash by a dry method/semi-dry method in a steel enterprise, and particularly relates to a device and a method for modifying desulfurized fly ash based on blast furnace gas heating.
Background
The flue gas desulfurization process mainly comprises a wet method, a semi-dry method and a dry method, the semi-dry method desulfurization process is well received by steel enterprises, and a large amount of semi-dry method desulfurization ash is generated. Instability of semi-dry desulfurized fly ash limits application of the desulfurized fly ash in building material fields, and influences stability of desulfurized fly ashThe main sexual factors are calcium sulfite and free calcium oxide. The content of calcium sulfite in the desulfurized fly ash is up to 20-40%, the hydration reaction of calcium sulfite is slow, and the calcium sulfite can not be quickly coagulated and hardened, so that the cement or building material doped with the desulfurized fly ash can generate delayed coagulation; under a humid environment, calcium sulfite is easily oxidized into calcium sulfate, so that a cement product doped with desulfurized ash or a building poured by concrete generates micro-expansion, and the strength of the concrete or a building material is damaged; the calcium sulfite can be decomposed again to release SO when meeting high temperature or acidic conditions 2 Causing secondary pollution. The content of free calcium oxide in the desulfurized fly ash can reach 5 to 30 percent, and the free calcium oxide can continuously generate Ca (OH) in the long-term hydration process 2 The volume continues to expand, stress concentration occurs, and thus structural strength is deteriorated, and in addition, free calcium oxide is hydrated to form Ca (OH) 2 In the process, a large amount of heat is released. Based on the instability influence of calcium sulfite and free calcium oxide in the desulfurized fly ash, the desulfurized fly ash can not be directly used in the field of building materials to realize resource utilization. At present, the comprehensive utilization level of the semi-dry desulfurized fly ash for recycling is relatively low.
The utility model discloses a chinese utility model publication CN210438429U discloses a calcium sulfite oxidation modification system in semidry desulfurization waste ash, and this patent utilizes the system of preheating kiln, oxidation kiln and cooling kiln syllogic, and to calcium sulfite content in the desulfurization ash, easy inflation, the shortcoming of slow setting carry out oxidation modification treatment, and this system has advantages such as the energy consumption is high, the oxidation rate is high, throughput is big. The system only solves the instability influence of calcium sulfite in the desulfurized fly ash, is suitable for oxidizing the semidry desulfurized fly ash with high calcium sulfite and low free calcium oxide, and still has the instability influence factor limiting the resource utilization of the desulfurized fly ash with high free calcium oxide content.
The Chinese patent publication CN104150520A discloses a dry and semi-dry desulfurization ash oxygen-enriched additional oxidation process and a device, the process is characterized in that air heat introduced into a kiln is transferred from flue gas of a heating furnace, the heat transfer efficiency is low, the material preheating effect is poor, and the energy consumption is high. The waste heat of the finished product is recovered by indirect heat exchange of a heat exchanger, so that the heat exchange efficiency is low, and the waste heat of the product cannot be effectively recovered.
At present, some colleges and universities, scientific research institutions and related enterprises are also actively researching and exploring technologies and equipment for realizing resource utilization of desulfurized fly ash, wherein the main research emphasis is placed on the technologies and equipment for efficient oxidation and conversion of calcium sulfite in desulfurized fly ash, such as a catalytic oxidation method, a high-temperature oxidation method and an electrochemical oxidation method, and the instability influence of free calcium oxide in desulfurized fly ash is ignored.
Disclosure of Invention
Based on the defects of the prior art, the invention provides a device and a method for modifying desulfurized ash based on heating of blast furnace gas.
The method is realized by the following technical scheme:
a device for heating and modifying desulfurized ash based on blast furnace gas comprises a pretreatment device, a carbonation oxidation device and a heat exchange device.
The pretreatment device comprises a raw material buffer bin, a metering and conveying part, a dust removal device and a preheating kiln.
The raw material buffer bin is used for temporarily storing the desulfurization ash raw material conveyed by an external system.
The metering and conveying component comprises a feeder and a metering screw conveyor, one end of the feeder is communicated with the raw material buffer bin, the other end of the feeder is communicated with the metering screw conveyor, the feeder is used for conveying the desulfurization ash raw material to the metering screw conveyor, and the metering screw conveyor is used for conveying the desulfurization ash raw material conveyed by the feeder to the preheating kiln and metering the quality of the desulfurization ash.
The dust removal device is used for collecting desulfurization ash dust in waste flue gas discharged by the preheating kiln, and the collected dust is returned and sent into the raw material buffer bin; the dust removal device comprises a dust removal waste gas inlet, a dust discharge port and a dust removal flue gas discharge port, and the dust discharge port is communicated with the raw material buffer bin.
The preheating kiln comprises a preheating material inlet, a preheating flue gas inlet, a preheating cavity body, a preheating material outlet and a preheating flue gas outlet; the preheating material inlet is communicated with the metering screw conveyor, and the preheating flue gas outlet is communicated with the dedusting waste gas inlet.
The carbonation oxidation device comprises an oxidation kiln body, an oxidation feeding part, an oxidation discharging part, an oxidation air inlet and an oxidation air outlet; the oxidation feeding part is communicated with the preheating material outlet, the oxidation exhaust port is communicated with the preheating flue gas inlet, and the oxidation kiln body is used for mixing and reacting the desulfurization ash solid material and the flue gas entering the oxidation kiln body.
The heat exchange device comprises a hot air device, a cooling cavity body, a cooling feeding part, a cooling discharging part, a cooling first air inlet, a cooling second air inlet, a cooling first exhaust port and a cooling second exhaust port; the hot air device comprises a hot air furnace body, a first hot air furnace air inlet, a second hot air furnace air inlet and a hot air furnace air outlet; the cooling cavity body comprises a body inner cavity and a cooling jacket, the cooling jacket is sleeved outside the body inner cavity, the cooling second air inlet and the cooling second air outlet are both arranged on the outer wall of the cooling jacket, the cooling first air inlet and the cooling discharging component are both arranged on one end wall of the body inner cavity, the cooling feeding component and the cooling first air outlet are both arranged on the other end wall of the body inner cavity, the cooling feeding component is communicated with the oxidation discharging component, the cooling discharging component is communicated with a peripheral finished product bin, the cooling first air inlet is used for discharging oxidation air, and the cooling second air inlet is used for discharging blast furnace gas and combustion-supporting air; the first air intake of hot-blast furnace sets up in the lateral part of hot-blast furnace, the first air intake of hot-blast furnace with the first gas vent intercommunication of cooling, hot-blast furnace second air intake sets up in the bottom of hot-blast furnace, hot-blast furnace second air intake with the second gas vent intercommunication of cooling, the hot-blast furnace air exit with the oxidation air inlet intercommunication.
Preferably, the raw material surge bin is of a cylindrical steel structure, and comprises a raw material surge bin inlet, a vibrator (a device which is known in the prior art and is used for preventing and eliminating the phenomena of blocking and tower arching of various storage bins caused by internal friction, deliquescence, electrification, composition segregation and the like of materials), a bin top dust remover and a raw material surge bin outlet. The bin top dust remover is arranged at the top of the raw material buffer bin and used for avoiding discharging floating dust materials in the raw materials, and is a commodity purchased in the market.
Preferably, the feeding machine comprises a motor, a hopper and a damping device, and the metering screw conveyor comprises a screw conveyor body, a screw conveyor feeding port, a screw conveyor discharging port and a driving device. The spiral conveyer body is a double-spiral or triple-spiral known existing spiral conveyer body, and the driving device is a motor, a speed reducer matched with the motor and the like.
Preferably, the dust outlet of the dust removal device is communicated with the raw material buffer bin through a raw material buffer bin inlet; the preheating material inlet is a chute and is communicated with the metering screw conveyor through a discharge hole of the screw conveyor.
The oxidation kiln body of the carbonation oxidation device is of a steel roller structure, the lining of the steel roller is a refractory brick, a lifting blade is arranged in the steel roller, and the outside of the steel roller is insulated by aluminum silicate insulation cotton.
Preferably, a thermocouple is provided in a cooling jacket of the cooling chamber body.
Preferably, a thermocouple is arranged at the air outlet of the hot blast stove.
The method for heating and modifying the desulfurized ash based on the blast furnace gas is characterized by comprising the following steps of:
(1) The mixed gas of blast furnace gas and combustion-supporting air is continuously introduced into the cooling jacket through the cooling second gas inlet, the oxidizing air is continuously introduced into the inner cavity of the body through the cooling first gas inlet, the mixed gas of the blast furnace gas and the combustion-supporting air is discharged through the cooling second gas outlet and then into the hot blast furnace through the second air inlet of the hot blast furnace, the oxidizing air is discharged through the cooling first gas outlet and then into the hot blast furnace through the first air inlet of the hot blast furnace, the flue gas of the hot blast furnace is discharged through the air outlet of the hot blast furnace and then into the oxidation kiln body through the oxidation gas inlet, the formed reaction treatment gas is discharged through the oxidation gas outlet and then into the preheating cavity body through the preheating flue gas inlet, the formed preheating flue gas with dust is discharged through the preheating flue gas outlet and then into the dust removal device through the dust removal waste gas inlet, the generated dust removal flue gas is discharged through the dust removal flue gas outlet (preferably discharged to the position before desulfurization), and the generated dust is discharged into the raw material buffer bin through the dust discharge outlet.
(2) The desulfurization ash is placed into the raw material buffer bin through the raw material buffer bin inlet, then the desulfurization ash is fed into the preheating kiln through the preheating material inlet after being metered by the metering screw conveyor, the temperature of reaction treatment gas discharged from the preheating flue gas inlet is 420-580 ℃, the desulfurization ash which moves to the preheating material outlet is heated to 300-450 ℃ by high-temperature reaction treatment gas, the reaction treatment gas is cooled to 180-230 ℃ to form dust-containing preheating flue gas, and the preheated desulfurization ash is discharged through the preheating material outlet.
(3) Discharging the preheated desulfurization ash discharged in the step (2) into an oxidation kiln body through an oxidation feeding part, and reacting the preheated desulfurization ash with the hot blast stove flue gas entering the oxidation kiln body, wherein the temperature of the hot blast stove flue gas is 550-625 ℃, the desulfurization ash is heated to 550-610 ℃, and CaSO in the desulfurization ash is completed 3 Converted into CaSO by reacting with flue gas of hot blast stove 4 The oxidation process of (2) is to complete the carbonation process of converting calcium oxide in the desulfurized fly ash into calcium carbonate through the reaction with flue gas of the hot blast stove, the reacted desulfurized fly ash material is discharged through the oxidation discharge component, and the formed reaction treatment gas is discharged through the oxidation exhaust port.
(4) And (3) discharging the desulfurized ash material discharged in the step (3) into the cooling feeding part, performing indirect heat exchange on the desulfurized ash material through mixed gas of blast furnace gas and combustion-supporting air, and performing direct heat exchange on the desulfurized ash material and oxidizing air in the inner cavity of the body to ensure that the modified desulfurized ash is cooled to below 200 ℃ in the inner cavity of the body, then discharging the modified desulfurized ash through the cooling discharging part, and controlling the temperature of the mixed gas of the blast furnace gas and the combustion-supporting air discharged from the cooling second exhaust port to be lower than 600 ℃ through a thermocouple arranged in a cooling jacket of the cooling cavity body.
(5) After indirectly absorbing the waste heat in the cooling jacket, the mixed gas of the blast furnace gas and the combustion air is discharged through a second cooling exhaust port, then is discharged into the hot blast furnace through a second air inlet of the hot blast furnace, and is combusted in the hot blast furnace to generate CO-rich gas 2 The oxidizing air directly absorbs the waste heat in the inner cavity of the body and then is discharged into the hot blast stove through a first air inlet of the hot blast stove, the high-temperature flue gas and the low-temperature oxidizing air are mixed and exchange heat in the hot blast stove to generate hot blast stove flue gas at 550-625 ℃, and the temperature of the flue gas at the outlet of the hot blast stove is adjusted by controlling the flow of blast furnace gas and the oxidizing air.
(6) And (5) crushing the modified desulfurization ash discharged in the step (4) by a crusher, and then conveying the crushed desulfurization ash into a finished product bin by a lifter to form a modified desulfurization ash product.
Preferably, the temperature of the flue gas is detected by a thermocouple arranged at an air outlet of the hot blast stove.
Alternatively, the blast furnace gas is replaced with natural gas and/or industrial by-product gas.
Preferably, in step (1), the volume ratio of blast furnace gas to combustion air is 1: (1.2-1.5);
preferably, in the step (2), the temperature of the reaction treatment gas discharged from the preheating flue gas inlet is 450 to 550 ℃, the desulfurization ash proceeding to the preheating material discharge port is heated to 300 to 400 ℃ by the high-temperature reaction treatment gas, and the reaction treatment gas is cooled to 180 to 210 ℃.
Preferably, in the step (3), the oxidation feeding part is a chute, the temperature of the flue gas of the hot blast stove is 575-625 ℃, and the desulfurized ash is heated to 560-605 ℃.
Preferably, in the step (5), the high-temperature flue gas and the low-temperature oxidizing air are mixed and heat-exchanged in the hot blast stove to generate the flue gas of the hot blast stove at 575 to 625 ℃, and the temperature of the flue gas at the outlet of the hot blast stove is adjusted by controlling the flow rates of the blast furnace gas and the oxidizing air.
Preferably, in the step (6), the modified desulfurized fly ash discharged from the step (4) is pulverized to 40 μm or less by a pulverizer.
The combustion air and the oxidation air can be both common air or oxygen-enriched air, or one of the combustion air and the oxidation air can be common air and the other oxygen-enriched air.
The invention has the technical effects that:
aiming at the problems that the existing dry and/or semi-dry desulfurized fly ash has unstable performance, low strength of produced building materials and difficult resource utilization, the invention adopts high-temperature oxidation and high-temperature carbonation methods, not only can oxidize calcium sulfite in the desulfurized fly ash into calcium sulfate, but also carbonate free calcium oxide in the desulfurized fly ash into calcium carbonate. The modified desulfurized fly ash is more stable in performance, the influence of instability of calcium oxide is eliminated, the product can be added into building materials, the comprehensive utilization of resources is realized, the problems that desulfurized waste ash is piled everywhere and pollutes the environment are solved, and free calcium oxide in the desulfurized fly ash is utilized to solidify carbon dioxide, so that the emission of carbon dioxide is reduced.
The invention can efficiently oxidize calcium sulfite and carbonate free calcium oxide, the optimal temperature of the calcium sulfite high-temperature oxidation reaction is 500-600 ℃, the optimal temperature of the calcium oxide carbonation reaction is 600-700 ℃, and the desulfurized ash is directly heated by utilizing high-temperature flue gas with the temperature of about 600 ℃ generated by the combustion of blast furnace gas, thereby solving the problem of low utilization rate of indirect heating heat of the flue gas, and simultaneously utilizing O in the air 2 Oxidizing calcium sulfite in the desulfurized fly ash by using CO of the blast furnace gas 2 And CO produced by combustion 2 Free calcium oxide in the desulfurized fly ash is carbonated, so that the oxidation and the carbonation are realized simultaneously. And meanwhile, the oxidation reaction of the calcium sulfite and the carbonation of the calcium oxide both belong to exothermic reactions, so that heat can be provided for the continuous and stable reaction and flow of the subsequent materials, the consumption of blast furnace gas is reduced, energy is saved, the consumption of fuel is greatly reduced, the production cost is saved, and the efficiency is improved.
The invention adopts high-temperature flue gas to directly heat the desulfurized ash, the heat exchange efficiency is high, and the equipment structure is simple; meanwhile, the chemical energy generated by the carbonation reaction of calcium oxide is utilized, so that the energy consumption is reduced; and the free calcium oxide in the desulfurized fly ash is utilized to solidify carbon dioxide, so that the emission of the carbon dioxide is reduced. Meanwhile, the blast furnace gas is cheaper than natural gas and industrial byproduct gas, and the modification cost of the desulfurized fly ash can be reduced.
Drawings
FIG. 1 is a schematic diagram of the method for modifying desulfurized fly ash based on the heating of blast furnace gas according to the invention.
Wherein: 1-raw material buffer bin, 2-metering conveying component, 3-dust removing device, 4-preheating kiln, 5-carbonation oxidation device, 6-cooling cavity body, 7-hot blast stove body, A-combustion air, B-blast furnace gas and C-oxidation air.
Detailed Description
The technical scheme of the invention is further explained by combining the attached drawings:
in the embodiment, after a gas flow path is started firstly, semi-dry desulfurized ash is conveyed to a metering screw conveyor by a feeder of a metering conveying part 2 through a raw material buffer bin 1, and then is metered by the metering screw conveyor and then is sent into a preheating kiln 4, the desulfurized ash exchanges heat with high-temperature flue gas in the preheating kiln, the heat of the preheating kiln is derived from the high-temperature flue gas discharged by a carbonation oxidation device, the desulfurized ash is heated to 300-400 ℃, the high-temperature flue gas is cooled to about 200 ℃, the preheated desulfurized ash is sent into an oxidation kiln body of the carbonation oxidation device 5 through a chute, the cooled waste flue gas is discharged by the preheating kiln, and the gas is discharged into a flue gas pipeline of a desulfurization system after dust is collected by a dust collector 3 consisting of a cyclone dust collector and a cloth bag dust collector. The preheating kiln is lined with heat insulating material, and a material raising plate and a spiral plate are arranged in the preheating kiln.
High-temperature flue gas with the temperature of 600 +/-25 ℃ is introduced into the oxidation kiln body, the high-temperature flue gas is generated by burning blast furnace gas by a hot blast furnace body 6, and desulfurized ash is heated to about 600 ℃ in the oxidation kiln body to finish CaSO 3 Conversion to CaSO 4 And a carbonation process for converting calcium oxide into calcium carbonate. The modified desulfurized ash enters the cooling cavity body, and the reacted high-temperature waste gas enters the preheating kiln to provide heat for preheating the desulfurized ash. The oxidation kiln body is lined with a heat insulation material, and a lifting blade and a spiral plate are arranged in the oxidation kiln body.
The cooling cavity body adopts an inner-outer double-layer cooling mode, oxidation air C is introduced into the inner cavity body, and the oxidation air C is directly sent into the heating furnace after heat exchange is carried out to absorb waste heat of products. Blast furnace gas B and combustion air A are introduced into the cooling jacket, and the volume ratio of the blast furnace gas to the combustion air is 1: (1.2-1.5), indirectly exchanging heat to absorb the waste heat of the product and then sending the product into a hot blast stove. The modified desulfurized fly ash is cooled to below 200 ℃ in the cooling cavity body, and the cooled desulfurized fly ash is crushed by the crusher and then is sent to a finished product bin by the elevator. The thermocouple is arranged at the outlet of the blast furnace gas mixed gas of the cooling kiln outer jacket, the temperature of the outlet mixed gas is strictly controlled, and the temperature of the outlet mixed gas is ensured to be lower than the ignition temperature of the blast furnace gas (the ignition point of the blast furnace gas is about 600 ℃).
The mixed gas of blast furnace gas and combustion air is sent into the hot blast stove after indirectly absorbing the waste heat of the product by a jacket outside the cooling kiln, and is combusted in the hot blast stove to generate CO-rich gas 2 The high-temperature flue gas and the oxidizing air directly absorb the waste heat of the product in the cooling kiln and then are sent into the hot blast stove, the high-temperature flue gas and the low-temperature oxidizing air are mixed and exchange heat in the hot blast stove to generate the high-temperature flue gas with the temperature of 600 +/-25 ℃, and the flue gas temperature at the outlet of the hot blast stove is adjusted by controlling the flow of blast furnace gas and the flow of the oxidizing air. And sending the high-temperature flue gas into an oxidation kiln for modification treatment of semi-dry desulfurized fly ash. And a thermocouple is arranged at the outlet of the hot blast stove to detect the temperature of the flue gas.
Claims (9)
1. The method for modifying the desulfurized ash based on the heating of the blast furnace gas is characterized by being carried out by using a device for modifying the desulfurized ash based on the heating of the blast furnace gas, wherein the device for modifying the desulfurized ash based on the heating of the blast furnace gas comprises a pretreatment device, a carbonation oxidation device and a heat exchange device;
the pretreatment device comprises a raw material buffer bin, a metering conveying part, a dust removal device and a preheating kiln;
the raw material buffer bin is used for temporarily storing the desulfurization ash raw material conveyed by an external system;
the metering and conveying component comprises a feeder and a metering screw conveyor, one end of the feeder is communicated with the raw material buffer bin, the other end of the feeder is communicated with the metering screw conveyor, the feeder is used for conveying the desulfurization ash raw material to the metering screw conveyor, and the metering screw conveyor is used for conveying the desulfurization ash raw material conveyed by the feeder to the preheating kiln and metering the mass of the desulfurization ash;
the dust removal device is used for collecting desulfurization ash dust in waste flue gas discharged by the preheating kiln, and the collected dust is returned and sent into the raw material buffer bin; the dust removal device comprises a dust removal waste gas inlet, a dust discharge port and a dust removal flue gas discharge port, and the dust discharge port is communicated with the raw material buffer bin;
the preheating kiln comprises a preheating material inlet, a preheating flue gas inlet, a preheating cavity body, a preheating material outlet and a preheating flue gas outlet; the preheating material inlet is communicated with the metering screw conveyer, and the preheating flue gas outlet is communicated with the dedusting waste gas inlet;
the carbonation oxidation device comprises an oxidation kiln body, an oxidation feeding part, an oxidation discharging part, an oxidation air inlet and an oxidation air outlet; the oxidation feeding part is communicated with the preheated material discharge port, the oxidation exhaust port is communicated with the preheated flue gas inlet, and the oxidation kiln body is used for mixing and reacting the desulfurized ash solid material and the flue gas entering the oxidation kiln body;
the heat exchange device comprises a hot air device, a cooling cavity body, a cooling feeding part, a cooling discharging part, a cooling first air inlet, a cooling second air inlet, a cooling first exhaust port and a cooling second exhaust port; the hot air device comprises a hot air furnace body, a first hot air furnace air inlet, a second hot air furnace air inlet and a hot air furnace air outlet; the cooling cavity body comprises a body inner cavity and a cooling jacket, the cooling jacket is sleeved outside the body inner cavity, the cooling second air inlet and the cooling second air outlet are both arranged on the outer wall of the cooling jacket, the cooling first air inlet and the cooling discharging component are both arranged on one end wall of the body inner cavity, the cooling feeding component and the cooling first air outlet are both arranged on the other end wall of the body inner cavity, the cooling feeding component is communicated with the oxidation discharging component, the cooling discharging component is communicated with a peripheral finished product bin, the cooling first air inlet is used for discharging oxidation air, and the cooling second air inlet is used for discharging blast furnace gas and combustion-supporting air; the first air inlet of the hot blast stove is arranged at the side part of the hot blast stove and is communicated with the cooling first exhaust port, the second air inlet of the hot blast stove is arranged at the bottom of the hot blast stove and is communicated with the cooling second exhaust port, and the air outlet of the hot blast stove is communicated with the oxidation air inlet;
the method comprises the following steps:
(1) Continuously introducing mixed gas of blast furnace gas and combustion-supporting air into a cooling jacket through a cooling second air inlet, continuously introducing oxidizing air into an inner cavity of a body through a cooling first air inlet, discharging the mixed gas of the blast furnace gas and the combustion-supporting air through a cooling second air outlet, then discharging the mixed gas into a hot blast furnace through a second air inlet of the hot blast furnace, discharging the oxidizing air through a cooling first air outlet, then discharging the oxidizing air into the hot blast furnace through a first air inlet of the hot blast furnace, discharging flue gas of the hot blast furnace through an air outlet of the hot blast furnace, then discharging the formed reaction treatment gas into an oxidation kiln body through an oxidation air inlet, then discharging the formed reaction treatment gas into a preheating cavity body through a preheating flue gas inlet, then discharging the formed preheating flue gas with dust through a preheating flue gas outlet, then entering a dust removal device through a dust removal waste gas inlet, discharging the generated dust removal flue gas through a dust removal flue gas outlet, and discharging the generated dust into a raw material buffer bin through a dust discharge outlet;
(2) Putting raw material desulfurization ash into a raw material buffer bin through a raw material buffer bin inlet, then feeding the desulfurization ash into a preheating kiln through a preheating material inlet after metering by a metering screw conveyor, wherein the temperature of reaction treatment gas discharged from a preheating flue gas inlet is 420-580 ℃, the desulfurization ash proceeding to a preheating material discharge outlet is heated to 300-450 ℃ by high-temperature reaction treatment gas, the reaction treatment gas is cooled to 180-230 ℃ to form dust-carrying preheating flue gas, and the preheated desulfurization ash is discharged through a preheating material discharge outlet;
(3) Discharging the preheated desulfurization ash discharged in the step (2) into an oxidation kiln body through an oxidation feeding part, and reacting the preheated desulfurization ash with the hot blast stove flue gas entering the oxidation kiln body, wherein the temperature of the hot blast stove flue gas is 550-625 ℃, and the desulfurization ash is heatedThe CaSO in the desulfurized fly ash is finished at the same time when the temperature is 550 to 610 DEG C 3 Converted into CaSO by reacting with flue gas of hot blast stove 4 The oxidation process of (1) is to complete the carbonation process of converting calcium oxide in the desulfurized fly ash into calcium carbonate through the reaction with flue gas of a hot blast stove, the reacted desulfurized fly ash material is discharged through an oxidation discharge component, and the formed reaction treatment gas is discharged through an oxidation exhaust port;
(4) Discharging the desulfurized ash material discharged in the step (3) into the inner cavity of the body through the cooling feeding part, carrying out indirect heat exchange on the desulfurized ash material through mixed gas of blast furnace gas and combustion air, and carrying out direct heat exchange on the desulfurized ash material and oxidized air in the inner cavity of the body, so that the modified desulfurized ash is cooled to below 200 ℃ in the inner cavity of the body, and then discharging the modified desulfurized ash through the cooling discharging part;
(5) The mixed gas of blast furnace gas and combustion air indirectly absorbs the waste heat in the cooling jacket, is discharged through a cooling second exhaust port, is discharged into the hot blast furnace through a second air inlet of the hot blast furnace, and is combusted in the hot blast furnace to generate CO-rich gas 2 The oxidizing air directly absorbs waste heat in the inner cavity of the body and then is discharged into the hot air furnace through a first air inlet of the hot air furnace, the high-temperature flue gas and the low-temperature oxidizing air are mixed in the hot air furnace for heat exchange to generate the flue gas of the hot air furnace at the temperature of 550-625 ℃, and the temperature of the flue gas at the outlet of the hot air furnace is adjusted by controlling the flow of blast furnace gas and the oxidizing air;
(6) And (4) crushing the modified desulfurization ash discharged in the step (4) by a crusher, and then conveying the crushed desulfurization ash into a finished product bin by a lifter to form a modified desulfurization ash product.
2. The method for heating and modifying desulfurization ash based on blast furnace gas according to claim 1, wherein the raw material surge bin is of a cylindrical steel structure and comprises a raw material surge bin inlet, a vibrator, a bin top dust remover and a raw material surge bin outlet.
3. The method for modifying the desulfurized ash based on the heating of the blast furnace gas according to claim 1, wherein the feeding machine comprises a motor, a hopper and a shock-absorbing device, and the metering screw conveyor comprises a screw conveyor body, a screw conveyor feeding port, a screw conveyor discharging port and a driving device.
4. The method for modifying desulfurized ash based on the heating of blast furnace gas according to claim 1, wherein said dust discharge port of said dust removal device is communicated with said raw material surge bin through a raw material surge bin inlet; the preheating material inlet is a chute and is communicated with the metering screw conveyor through a discharge hole of the screw conveyor;
the oxidation kiln body of the carbonation oxidation device is of a steel roller structure, a refractory brick and a material raising plate are lined in the roller, and the outside of the roller is insulated by aluminum silicate insulation cotton.
5. The method for modifying desulfurized ash based on the heating of blast furnace gas according to claim 1, characterized in that a thermocouple is disposed within the cooling jacket of the cooling chamber body.
6. The method for modifying the desulfurized ash based on the heating of the blast furnace gas according to claim 1, wherein a thermocouple is arranged at the air outlet of the hot blast stove.
7. The method for heating and modifying desulfurized ash based on blast furnace gas according to claim 1, wherein the temperature of the mixed gas of blast furnace gas and combustion air discharged from the second exhaust port through the cooling is controlled to be lower than 600 ℃ by measuring the temperature of the mixed gas of blast furnace gas and combustion air by means of a thermocouple arranged in a cooling jacket of the cooling chamber body; the temperature of the flue gas is detected by a thermocouple arranged at an air outlet of the hot blast stove.
8. The method for modifying desulfurized ash based on the heating of blast furnace gas according to claim 2, characterized in that the blast furnace gas is replaced with natural gas and/or industrial by-product gas as a replacement.
9. The method for heating and modifying desulfurized ash based on blast furnace gas according to claim 2, wherein in step (1), the volume ratio of blast furnace gas to combustion air is 1: (1.2 to 1.5);
in the step (2), the temperature of reaction treatment gas discharged from a preheating flue gas inlet is 450 to 550 ℃, the desulfurization ash proceeding to a preheating material discharge outlet is heated to 300 to 400 ℃ by the high-temperature reaction treatment gas, and the reaction treatment gas is cooled to 180 to 210 ℃;
in the step (3), the oxidation feeding part is a chute, the temperature of the flue gas of the hot blast stove is 575 to 625 ℃, and the desulfurized fly ash is heated to 560 to 605 ℃;
in the step (5), high-temperature smoke and low-temperature oxidizing air are mixed in a hot blast stove for heat exchange to generate smoke of the hot blast stove at 575-625 ℃, and the smoke temperature of an outlet of the hot blast stove is adjusted by controlling the flow of blast furnace gas and the flow of the oxidizing air;
in the step (6), the modified desulfurized fly ash discharged from the step (4) is pulverized to 40 μm or less by a pulverizer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111632131.8A CN114409290B (en) | 2021-12-28 | 2021-12-28 | Device and method for heating and modifying desulfurized ash based on blast furnace gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111632131.8A CN114409290B (en) | 2021-12-28 | 2021-12-28 | Device and method for heating and modifying desulfurized ash based on blast furnace gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN114409290A CN114409290A (en) | 2022-04-29 |
| CN114409290B true CN114409290B (en) | 2022-11-04 |
Family
ID=81269779
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111632131.8A Active CN114409290B (en) | 2021-12-28 | 2021-12-28 | Device and method for heating and modifying desulfurized ash based on blast furnace gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN114409290B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114804804B (en) * | 2022-05-31 | 2023-01-24 | 北京北科环境工程有限公司 | Preparation method of gypsum binder |
| CN115649870B (en) * | 2022-11-14 | 2023-03-17 | 北京天中方环保科技有限公司 | Dry-method calcium-based desulfurization low-positive-pressure pneumatic continuous conveying device and using method thereof |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101797470A (en) * | 2010-01-11 | 2010-08-11 | 山东大学 | Method for circularly trapping SO2 and CO2 by using calcium-based absorbent |
| CN102701618A (en) * | 2012-06-25 | 2012-10-03 | 甘肃省建材科研设计院 | Method for using calcium sulfite type desulfurization gypsum to produce high-strength environmental-friendly type plastering gypsum |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3035015B2 (en) * | 1991-08-13 | 2000-04-17 | 三菱重工業株式会社 | Desulfurization method |
| EP0628340B1 (en) * | 1990-11-28 | 1996-10-30 | Mitsubishi Jukogyo Kabushiki Kaisha | Method for desulfurizing exhaust gas |
| CN101539037B (en) * | 2009-04-03 | 2011-05-04 | 东南大学 | Method for catching carbon dioxide by pressurized fluidized bed combustion combined recycled generating system |
| EP2305366B1 (en) * | 2009-09-16 | 2012-05-30 | Consejo Superior de Investigaciones Científicas (CSIC) | Method of capturing CO2 by means of CaO and the exothermal reduction of a solid |
| CN204057990U (en) * | 2014-08-04 | 2014-12-31 | 辽宁能源环境工程技术有限公司 | Dry method, semi-dry desulphurization ash two sections revolution oxygen enrichment external heat oxidation unit |
| CN104229855B (en) * | 2014-08-04 | 2016-06-15 | 辽宁能源环境工程技术有限公司 | Utilize electricity generation boiler or the technique of sintering device flue gas on-line heating oxidation sweetening ash |
| CN105642651A (en) * | 2016-01-06 | 2016-06-08 | 西昌市蓝鼎环保科技有限公司 | Method for improving desulphurization ash stability |
| CN112058049A (en) * | 2020-09-16 | 2020-12-11 | 广东佳德环保科技有限公司 | Flue gas desulfurization and denitrification system device and method adopting ozone oxidation and semidry method |
| CN112939495A (en) * | 2021-02-05 | 2021-06-11 | 北京北科环境工程有限公司 | Production process for processing plastering gypsum by using semidry desulfurization ash |
-
2021
- 2021-12-28 CN CN202111632131.8A patent/CN114409290B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101797470A (en) * | 2010-01-11 | 2010-08-11 | 山东大学 | Method for circularly trapping SO2 and CO2 by using calcium-based absorbent |
| CN102701618A (en) * | 2012-06-25 | 2012-10-03 | 甘肃省建材科研设计院 | Method for using calcium sulfite type desulfurization gypsum to produce high-strength environmental-friendly type plastering gypsum |
Also Published As
| Publication number | Publication date |
|---|---|
| CN114409290A (en) | 2022-04-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN114409290B (en) | Device and method for heating and modifying desulfurized ash based on blast furnace gas | |
| CN103771734B (en) | A kind of mass-producing calcination processing utilizes the method for electrolytic manganese residues | |
| CN101987783B (en) | Method for producing active pulverized lime by utilizing coal gas to calcine limestone through suspended state pre-heating decomposing furnace | |
| CN102351444B (en) | Method for producing high grade cement clinker from full waste residues through rapidly calcining at low temperature | |
| CN102258923A (en) | Method for recycling and reusing tail gas of calcium carbide furnace | |
| CN104555946A (en) | Method for jointly producing sulphuric acid and cement clinker by using sulphur gas to reduce gypsum | |
| CN102180604B (en) | Spinning bed equipment and process for producing high-activity lime with spinning bed | |
| CN101955166B (en) | Method for decomposing semi-hydrated phosphogypsum | |
| CN112939495A (en) | Production process for processing plastering gypsum by using semidry desulfurization ash | |
| CN110065962A (en) | A kind of energy-efficient oxidative system of the useless ash of desulfurization and method | |
| CN206352122U (en) | A kind of cement production system | |
| CN105314894A (en) | Rotary kiln device and method for indirectly producing lime and recycling carbon dioxide | |
| CN105152141B (en) | A kind of gypsum relieving haperacidity thermal technology and device | |
| CN113548815A (en) | Novel household garbage incineration fly ash resource recycling system and method | |
| CN110343878B (en) | Energy-saving and environment-friendly production method of nickel-iron alloy | |
| CN105271841A (en) | Rotary kiln device and method for constant temperature indirect calcination of limestone | |
| CN211060653U (en) | Desulfurization ash oxidation modification system based on hot flue gas circulation indirect heating | |
| CN101239706B (en) | Method for producing calcium sulfide from calcium sulfate | |
| CN110642548B (en) | Method for treating dry-process desulfurized fly ash | |
| CN202157013U (en) | Novel environment-friendly and energy-saving limekiln | |
| CN115259102B (en) | Process and equipment for preparing sulfur dioxide concentrated flue gas and silicate clinker by flue gas diversion | |
| CN103043930A (en) | Method and equipment for producing cement and gathering CO2 by utilizing closed ring-shaped calcination furnace | |
| CN215713243U (en) | System for improving medium-temperature denitration effect of chain grate machine rotary kiln pellets | |
| CN202089901U (en) | Rotating bed equipment | |
| CN204625480U (en) | A kind of rotary kiln device of constant temperature indirect calcination Wingdale |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |