CN114733329B - Dry desulfurization process and dry desulfurization device for cement clinker - Google Patents
Dry desulfurization process and dry desulfurization device for cement clinker Download PDFInfo
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- CN114733329B CN114733329B CN202210341486.XA CN202210341486A CN114733329B CN 114733329 B CN114733329 B CN 114733329B CN 202210341486 A CN202210341486 A CN 202210341486A CN 114733329 B CN114733329 B CN 114733329B
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- dry desulfurization
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 36
- 230000023556 desulfurization Effects 0.000 title claims abstract description 36
- 239000004568 cement Substances 0.000 title claims abstract description 15
- 238000000034 method Methods 0.000 title claims abstract description 15
- 239000002994 raw material Substances 0.000 claims abstract description 62
- 239000008247 solid mixture Substances 0.000 claims abstract description 34
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 29
- 239000007787 solid Substances 0.000 claims abstract description 22
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 18
- 239000000920 calcium hydroxide Substances 0.000 claims abstract description 18
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims abstract description 18
- 239000000843 powder Substances 0.000 claims abstract description 17
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 235000012054 meals Nutrition 0.000 claims abstract description 6
- 239000000463 material Substances 0.000 claims description 47
- 230000001105 regulatory effect Effects 0.000 claims description 8
- 239000007921 spray Substances 0.000 claims description 2
- 238000001816 cooling Methods 0.000 abstract description 24
- 230000003009 desulfurizing effect Effects 0.000 abstract description 7
- 239000002245 particle Substances 0.000 abstract description 7
- 239000003795 chemical substances by application Substances 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 10
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 7
- 239000000292 calcium oxide Substances 0.000 description 7
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- 239000000498 cooling water Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000005507 spraying Methods 0.000 description 4
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 230000005514 two-phase flow Effects 0.000 description 3
- 244000261422 Lysimachia clethroides Species 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- 239000000356 contaminant Substances 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 230000001079 digestive effect Effects 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 235000011389 fruit/vegetable juice Nutrition 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000003116 impacting effect Effects 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 125000001741 organic sulfur group Chemical group 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D45/00—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces
- B01D45/12—Separating dispersed particles from gases or vapours by gravity, inertia, or centrifugal forces by centrifugal forces
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0233—Other waste gases from cement factories
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
- Y02P40/121—Energy efficiency measures, e.g. improving or optimising the production methods
Abstract
The application discloses a dry desulfurization process of cement clinker, which comprises the following steps: (1) Extracting the hot raw meal gas-solid mixture from the C5 cyclone; (2) Cooling and gas-solid separation are carried out on the hot raw material gas-solid mixture to obtain cooled raw material; (3) Adding water into the cooled raw material in a digester to digest the cooled raw material to form calcium hydroxide; (4) And (3) putting calcium hydroxide into a first air pipe from the C2 cyclone separator to the C1 cyclone separator for desulfurization treatment. The application also discloses a dry desulfurization device for the dry desulfurization process. In the application, the hot raw material gas-solid mixture is extracted from the C5 cyclone separator, and when the hot raw material gas-solid mixture is extracted, a small amount of gas in the C5 cyclone separator is utilized to carry out the powder collected by the C5 cyclone separator, so that the particle concentration of the C5 cyclone separator is higher, and the influence of taking and exhausting to a preheater system is reduced. Calcium hydroxide is used as a desulfurizing agent, SO that SO is easier to realize 2 Is not limited, and is not limited.
Description
Technical Field
The application relates to a dry desulfurization process and a dry desulfurization device for cement clinker.
Background
SO produced by calcining cement clinker 2 The contaminants are mainly derived from the raw meal and from the fuel in two parts. The sulfur in the raw material mainly exists in the form of organic sulfide, sulfide or sulfate; the sulfate in the feed will not typically form SO in the preheater system 2 Most enter the kiln system. Sulfide and organic sulfur in the raw material generate SO at 400-600 DEG C 2 And is discharged along with the exhaust gas. According to the regulations in the emission standard of atmospheric pollutants in the cement industry: existing clinker production line SO 2 The discharge concentration is not higher than 200mg/Nm 3 The critical area is not higher than 100mg/Nm 3 . For cement clinker production line with higher sulfur content of partial raw material, SO is generated in flue gas 2 The contaminants are relatively high, SO SO may be present 2 And (3) exceeding the pollutant emission concentration.
To reduce SO 2 Pollutant discharge, cementThe plant uses various preparations for desulfurization, one of which is to utilize a hot raw material desulfurization process, the principle of which is that hot raw material taken out from a gooseneck or a C5 cyclone separator of a decomposing furnace is cooled and digested to be converted into Ca (OH) 2 Feeding the material into a C1 cyclone separator, entering a preheater system, and absorbing SO in the preheater system 2 。
When the material is extracted by the gooseneck of the decomposing furnace, the solid-gas ratio (hot raw material and air volume ratio) is lower, the air volume extracted by the system is larger, the carried heat is more, the temperature of the waste gas discharged from the C1 cyclone separator is higher, the use of the waste heat power generation device is seriously affected, and meanwhile, the air volume is larger, the air volume in the preheater system is reduced, and the stability of the preheater system is affected.
When the hot raw materials are taken out from the discharging pipe of the C5 cyclone separator, the system is easy to block, the material taking system is unstable, the material breaking condition is easy to occur, and the operation of the desulfurization system is influenced.
Disclosure of Invention
In order to solve the problems, the application firstly provides a dry desulfurization process of cement clinker, which comprises the following steps:
(1) Extracting the hot raw meal gas-solid mixture from the C5 cyclone;
(2) Cooling and gas-solid separation are carried out on the hot raw material gas-solid mixture to obtain cooled raw material;
(3) Adding water into the cooled raw material in a digester to digest the cooled raw material to form calcium hydroxide;
(4) And (3) putting calcium hydroxide into a first air pipe from the C2 cyclone separator to the C1 cyclone separator for desulfurization treatment.
In the application, the hot raw material gas-solid mixture is extracted from the C5 cyclone separator, and when the hot raw material gas-solid mixture is extracted, a small amount of gas in the C5 cyclone separator is utilized to carry out the powder collected by the C5 cyclone separator, so that the particle concentration of the C5 cyclone separator is higher, and the influence of taking and exhausting to a preheater system is reduced. The application adopts calcium hydroxide as desulfurizing agent, has higher activity than calcium oxide, and is easier to realize SO 2 Is not limited, and is not limited.
Further, in step (2), when the hot raw material gas-solid mixture is cooled and gas-solid separated, the hot raw material gas-solid mixture is cooled once, and gas-solid separation is performed simultaneously, so as to obtain a cooled material once, and then the cooled material is cooled again, so that the cooled raw material is obtained.
The temperature of the cooled raw material can be smoothly reduced to the set temperature by adopting a twice cooling mode, the whole hot raw material gas-solid mixture can be cooled when being cooled for the first time, the raw material is only cooled when being cooled for the second time, and the temperature of the gas in the hot raw material gas-solid mixture can be reduced by adopting the twice cooling mode on the basis of ensuring the temperature reduction of the raw material, so that the heat loss of the gas in the cooling process is reduced.
Further, in the step (2), the hot raw material gas-solid mixture enters the separator, atomized water is sprayed into the separator, the hot raw material gas-solid mixture is cooled once, and gas-solid separation is carried out at the same time.
The spraying amount of atomized water can be completely evaporated to the maximum spraying amount, so that the phenomenon that excessive atomized water cannot be completely evaporated, so that the humidity of powder is increased and wall sticking phenomenon is generated is avoided. The hot raw material is pre-cooled by utilizing the gasification heat with higher water, so that the cooling speed of the hot raw material can be increased, the volume of the separator is reduced, and the manufacturing cost of the separator is reduced. The conventional indirect cooling equipment such as a jacket or a tube array is adopted for directly cooling the hot raw material gas-solid mixture, so that the cooling efficiency can be improved by utilizing atomized water to directly cool under the condition of reducing the same temperature, the volume of the cooling equipment is reduced, the utilization amount of cooling water is reduced, and the heat load of a cooling water system is reduced.
Specifically, in step (2), the primary cooling material is cooled again in a cooler, and the cooler is a water-cooled cooler. The discharge temperature of the hot raw meal from the cooler is 60-300 c. Too high discharge temperature can affect the digestion effect, too low discharge temperature can result in too high model selection and running cost of the cooler, and can also affect the digestion effect.
At present, the hot raw material is firstly collected and then cooled by a jacket type cooler, and a large amount of cooling water is needed to cool the hot raw material to a set temperature.
The application further provides a dry desulfurization device for cement clinker, which is used for the dry desulfurization process of any one of the above, and comprises a separator, a digester and a powder bin, wherein a C5 cyclone separator is communicated with the separator through a material taking pipe, and an exhaust port at the top of the separator is communicated with a first air pipe through an exhaust pipe; an air outlet at the top of the C2 cyclone separator is communicated with a material inlet of the C1 cyclone separator through a first air pipe;
a discharge hole at the bottom of the separator is communicated with the digester, and a water inlet pipe is connected to the digester; the discharge port of the digester is communicated with the powder bin, and the discharge port of the powder bin is communicated with the first air pipe.
According to the application, the dry desulfurization device is utilized to directly extract the hot raw material gas-solid mixture from the C5 cyclone separator, then the hot raw material gas-solid mixture is separated in the separator, gas is discharged into the C1 cyclone separator through the first air pipe, wherein the hot raw material generates calcium hydroxide through the digester, and then the calcium hydroxide is sent into the first air pipe as a desulfurizing agent to desulfurize the exhaust gas flow from the top of the C2 cyclone separator. By using the application, the raw materials on the cement clinker production line can be used as the raw materials of the desulfurizing agent. Because calcium hydroxide is used as the desulfurizing agent, the calcium hydroxide has higher activity than calcium oxide and is easier to realize SO 2 Is not limited, and is not limited. The separator is preferably a cyclone separator. The cyclone separator is adopted as a separator, so that the gas and the solid in the hot raw material gas-solid mixture can be separated by utilizing the advantages of cyclone separation and gas-solid separation, and the gas-solid separation efficiency is improved.
Further, in order to enhance the cooling effect, an atomizer for spraying atomized water into the separator is mounted on the separator. The atomizer is utilized to spray atomized water into the separator, and the hot raw material is cooled in advance by utilizing higher gasification heat of the water so as to ensure the subsequent cooling effect.
Further, in order to ensure the cooling effect, a discharge hole at the bottom of the separator is communicated with the digester through a cooler, and the cooler is a horizontal water-cooled cooler.
Further, in order to be convenient for measure the material that enters into the digester to add appropriate amount of digestive juice, the cooler is through first spiral metering and is linked together the digester, and the discharge gate in powder storehouse is through second spiral metering and is linked together first tuber pipe. The second spiral metering meter is used for metering the amount of the calcium hydroxide added into the first air pipe so as to adjust the amount of the calcium hydroxide according to the content of sulfur dioxide in the first air pipe. In order to measure the adding amount of the digestive water conveniently, a flowmeter is arranged on the water inlet pipe of the digester.
Further, a material taking hole is formed in the lower cone of the C5 cyclone separator, the material taking pipe is communicated with the C5 cyclone separator through the material taking hole, and an air cannon is further connected to the material taking hole. Further preferably, the material taking opening is arranged at the middle part of the lower cone in the height direction, and as the materials are collected at the straight cylinder part of the cyclone cylinder, the gas-solid separation is completed, and the collected powder is collected in the cone. The design can reduce the influence of the air quantity in the C5 cyclone separator during material taking. The material in the material taking opening can be dredged by utilizing the air cannon, and the material is prevented from being blocked at the material taking opening.
Further, a material taking valve is arranged on the material taking pipe, and a regulating valve is arranged on the exhaust pipe. The collecting amount of the hot raw material gas-solid mixture can be conveniently adjusted by using the material taking valve and the regulating valve, and during adjustment, coarse adjustment can be performed by using the material taking pipe firstly, and then fine adjustment can be performed by using the regulating valve.
Drawings
Fig. 1 is a schematic structural view of an embodiment of the present application.
Detailed Description
In the following description of the dry desulfurization apparatus for cement clinker, referring to fig. 1, the C1 cyclone 31, the C2 cyclone 32 and the C5 cyclone 35 are respectively referred to by the common names in the prior art, wherein the C1 cyclone 31 is used for gas-solid separation of the gas-solid two-phase flow entering the C1 cyclone, the C2 cyclone 32 is used for gas-solid separation of the gas-solid two-phase flow entering the C2 cyclone, and the C5 cyclone 35 is used for gas-solid separation of the gas-solid two-phase flow entering the C5 cyclone.
The dry desulfurization device is used for a dry desulfurization process for desulfurizing cement clinker, and comprises a separator 4, a cooler 9, a digester 11 and a powder bin 14, wherein a material taking opening 21 is formed in a lower cone 351 of a C5 cyclone separator 35, the material taking opening is specifically formed in the middle part of the lower cone 351 in the height direction, and two ends of a material taking pipe 20 are respectively communicated with the material taking opening 21 and a first feeding opening 401 of the separator 4. An air cannon 22 is connected to both the first inlet 401 and the outlet 21 to avoid clogging of the first inlet and outlet. A gate valve 23 is mounted on the take-off pipe 20.
The exhaust port 402 at the top of the separator 4 is communicated with the first air pipe 37 through the exhaust pipe 42; an air outlet 322 at the top of the C2 cyclone separator is communicated with a material inlet 311 of the C1 cyclone separator 31 through a first air pipe 37. A regulating valve 46 and a first thermocouple 44 are mounted on the discharge pipe. The amount of material entering the separator is regulated by means of a gate valve 23 and a regulating valve 46, wherein the gate valve 23 is used for coarse adjustment and the regulating valve 46 is used for fine adjustment. Pressure detectors 25 are also mounted on the take off pipe 20 and the exhaust pipe 42, respectively.
In this embodiment, the separator 4 includes a cylinder 404 extending in a vertical direction and a conical portion 405 disposed at a lower end of the cylinder 404, and an atomizer 41 is mounted on the cylinder 404, and the atomizer 41 is used for spraying atomized water into the separator. A second thermocouple 43 is mounted on the barrel 404 of the separator.
The first discharge port 403 at the bottom of the separator 4 is communicated with the second feed port 901 of the cooler 9 through the blanking pipe 47, a third thermocouple 48 and a flap valve 49 are arranged on the blanking pipe 47, the third thermocouple 48 is used for monitoring the discharge temperature of the separator 4, and the flap valve 49 is used for adjusting the discharge amount.
The second outlet 902 of the cooler 9 communicates with the third inlet 111 of the digester 11 via the first screw scale 10. A fourth thermocouple 903 is mounted at the second tap 902 to monitor the tap temperature of the cooler 9. In this embodiment, the cooler is a horizontal water-cooled cooler. A water inlet pipe 113 is connected to the digester, a flowmeter 114 is installed on the water inlet pipe, and digested water 150 enters the digester through the water inlet pipe 113.
The third discharge port 112 of the digester 11 is communicated with the fourth feed port 141 at the top of the powder bin 14 through the screw conveyor 13, and the fourth discharge port 142 at the bottom of the powder bin 14 is communicated with the first air pipe 37 through the second screw metering scale 15 and the desulfurization pipe 38 in sequence.
In this embodiment a separator is provided for separating and cooling the hot raw gas-solid mixture and a cooler is provided for re-cooling the material discharged from the separator, it being understood that in another embodiment the cooler may be omitted when the temperature of the material discharged from the separator has reached the desired temperature.
The dry desulfurization process of cement clinker is described below, and is performed by using the dry desulfurization device, and specifically includes the following steps:
(1) The hot raw meal gas-solid mixture is extracted from the C5 cyclone 35.
When the hot raw material gas-solid mixture is extracted from the C5 cyclone separator, a small amount of gas in the C5 cyclone separator is utilized to carry out powder collected by the C5 cyclone separator, so that the particle concentration of the C5 cyclone separator is higher, and the influence of taking and exhausting to a preheater system is reduced. When the hot raw material gas-solid mixture is extracted, the air cannon 22 is used for impacting the material taking hole 21 and the first feeding hole 401 of the separator 4 periodically, so that the material taking hole 21 and the first feeding hole 401 are prevented from being blocked.
(2) And cooling and gas-solid separation are carried out on the hot raw material gas-solid mixture, so as to obtain the cooled raw material.
The cooling water 110 and the compressed air 120 enter the separator 4 through the atomizer 41 to form atomized water in an atomized state, the addition amount of the cooling water is controlled under the action of the waste heat of the hot raw material gas-solid mixture to enable the atomized water to be completely evaporated to form steam, the temperature of the hot raw material gas-solid mixture is reduced, the gas in the hot raw material gas-solid mixture carries the steam upwards to enter the exhaust pipe 42 through the exhaust port 402, and the forward exhaust pipe 42 enters the first air pipe 37.
The solid particles in the hot raw material gas-solid mixture are taken as primary cooling materials, most of the solid particles are calcium oxide, the solid particles enter the cooler 9 through the blanking pipe 47 downwards to be cooled again, the cooling water 904 enters the jacket of the cooler to maintain the cooling temperature in the cooler, and the cooled calcium oxide is discharged from the cooler 9 as cooling raw material and then enters the digester 11 after being metered by the first spiral metering scale 10. The temperature of the calcium oxide discharged from the cooler is controlled within 200-220 ℃. (3) Adding water into the cooled raw material in a digester to digest to form calcium hydroxide. It will be appreciated that in other embodiments, the temperature of the calcium oxide exiting the cooler may also be specifically controlled in the range of 60-300 c, as desired.
The slaked water 150 enters the slaker through the water inlet pipe 113 and reacts with calcium oxide to produce calcium hydroxide, and the addition amount of slaked water is controlled to avoid excessive water. The digested calcium hydroxide is sent into a powder bin 14 for storage through a screw conveyor 13 and a lifting machine.
(4) According to the requirement, the calcium hydroxide is fed into the first air pipe after passing through the second spiral metering scale 15, and is mixed with SO in the air flow 2 React with SO 2 Absorbing and desulfurizing.
In this embodiment, the solid particles in the hot raw material gas-solid mixture are cooled by adopting a twice cooling manner, and it can be understood that in other embodiments, when the temperature of the primary cooling material discharged from the separator has reached the set temperature, the primary cooling material is not required to be cooled again, i.e. the cooled raw material is obtained by adopting the primary cooling.
Claims (9)
1. The dry desulfurization process of the cement clinker is characterized by comprising the following steps of:
(1) Extracting the hot raw meal gas-solid mixture from the C5 cyclone;
(2) The hot raw material gas-solid mixture enters a separator, atomized water is sprayed into the separator, the hot raw material gas-solid mixture is cooled once, and gas-solid separation is carried out simultaneously to obtain cooled raw materials;
(3) Adding water into the cooled raw material in a digester to digest the cooled raw material to form calcium hydroxide;
(4) And (3) putting calcium hydroxide into a first air pipe from the C2 cyclone separator to the C1 cyclone separator for desulfurization treatment.
2. The dry desulfurization process according to claim 1, wherein in the step (2), when the hot raw material gas-solid mixture is cooled and gas-solid separated, the hot raw material gas-solid mixture is first cooled once and simultaneously separated to obtain a cooled material, and then the cooled material is cooled again to obtain a cooled raw material.
3. The dry desulfurization process according to claim 2, wherein in the step (2), the primary temperature-decreasing material is cooled again in a cooler, which is a water-cooled cooler.
4. A dry desulfurization device for cement clinker, which is characterized in that the dry desulfurization device is used for the dry desulfurization process of any one of claims 1-3, and comprises a separator, a digester and a powder bin, wherein a C5 cyclone separator is communicated with the separator through a material taking pipe, and an exhaust port at the top of the separator is communicated with a first air pipe through an exhaust pipe; an air outlet at the top of the C2 cyclone separator is communicated with a material inlet of the C1 cyclone separator through a first air pipe; a discharge hole at the bottom of the separator is communicated with the digester, and a water inlet pipe is connected to the digester; the discharge port of the digester is communicated with the powder bin, and the discharge port of the powder bin is communicated with the first air pipe.
5. The dry desulfurization apparatus according to claim 4, wherein an atomizer is mounted on the separator, and the atomizer is configured to spray atomized water into the separator.
6. The dry desulfurization device according to claim 4, wherein the outlet at the bottom of the separator is connected to the digester via a cooler, which is a horizontal water-cooled cooler.
7. The dry desulfurization device according to claim 6, wherein the cooler is connected to the digester through a first screw scale, and the outlet of the powder bin is connected to the first air duct through a second screw scale.
8. The dry desulfurization device according to claim 4, wherein a material taking opening is arranged on the lower cone of the C5 cyclone separator, the material taking pipe is communicated with the C5 cyclone separator through the material taking opening, and an air cannon is further connected to the material taking opening.
9. The dry desulfurization apparatus according to claim 4, wherein a take-off valve is installed on the take-off pipe, and a regulating valve is installed on the exhaust pipe.
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| CN202210341486.XA CN114733329B (en) | 2022-04-02 | 2022-04-02 | Dry desulfurization process and dry desulfurization device for cement clinker |
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| CN202210341486.XA CN114733329B (en) | 2022-04-02 | 2022-04-02 | Dry desulfurization process and dry desulfurization device for cement clinker |
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| JP6223791B2 (en) * | 2013-11-18 | 2017-11-01 | 太平洋セメント株式会社 | Method for removing lead from cement firing equipment |
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| CN104692689A (en) * | 2015-02-05 | 2015-06-10 | 江苏苏博特新材料股份有限公司 | Method and device for producing modified calcium oxide expansion agent after dry desulfurization of flue gas |
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