CN111229011A - System and method for performing flue gas desulfurization by using cement kiln tail return ash - Google Patents
System and method for performing flue gas desulfurization by using cement kiln tail return ash Download PDFInfo
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- CN111229011A CN111229011A CN202010163333.1A CN202010163333A CN111229011A CN 111229011 A CN111229011 A CN 111229011A CN 202010163333 A CN202010163333 A CN 202010163333A CN 111229011 A CN111229011 A CN 111229011A
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 148
- 239000003546 flue gas Substances 0.000 title claims abstract description 148
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 99
- 230000023556 desulfurization Effects 0.000 title claims abstract description 99
- 239000004568 cement Substances 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 34
- 239000002002 slurry Substances 0.000 claims abstract description 194
- 239000000428 dust Substances 0.000 claims abstract description 73
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 59
- 238000005507 spraying Methods 0.000 claims abstract description 56
- 238000009827 uniform distribution Methods 0.000 claims abstract description 6
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 46
- 239000003795 chemical substances by application Substances 0.000 claims description 42
- 239000006227 byproduct Substances 0.000 claims description 34
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 238000007254 oxidation reaction Methods 0.000 claims description 20
- 229910052602 gypsum Inorganic materials 0.000 claims description 17
- 239000010440 gypsum Substances 0.000 claims description 17
- 238000004519 manufacturing process Methods 0.000 claims description 15
- 238000003756 stirring Methods 0.000 claims description 15
- 238000006243 chemical reaction Methods 0.000 claims description 14
- 230000007246 mechanism Effects 0.000 claims description 14
- 150000004683 dihydrates Chemical class 0.000 claims description 10
- 238000002844 melting Methods 0.000 claims description 9
- 230000008018 melting Effects 0.000 claims description 9
- 238000010517 secondary reaction Methods 0.000 claims description 9
- 238000004064 recycling Methods 0.000 claims description 7
- 238000007664 blowing Methods 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 4
- 208000005156 Dehydration Diseases 0.000 claims description 3
- 239000000654 additive Substances 0.000 claims description 3
- 230000000996 additive effect Effects 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 3
- 238000006297 dehydration reaction Methods 0.000 claims description 3
- 239000003595 mist Substances 0.000 abstract description 5
- 239000000779 smoke Substances 0.000 abstract 5
- 230000003647 oxidation Effects 0.000 description 12
- 230000000694 effects Effects 0.000 description 8
- 239000002994 raw material Substances 0.000 description 8
- 239000007921 spray Substances 0.000 description 8
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 229910000019 calcium carbonate Inorganic materials 0.000 description 3
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 3
- 239000000292 calcium oxide Substances 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 3
- 239000004927 clay Substances 0.000 description 3
- 229910052570 clay Inorganic materials 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- GBAOBIBJACZTNA-UHFFFAOYSA-L calcium sulfite Chemical compound [Ca+2].[O-]S([O-])=O GBAOBIBJACZTNA-UHFFFAOYSA-L 0.000 description 2
- 235000010261 calcium sulphite Nutrition 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 238000000265 homogenisation Methods 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 235000012054 meals Nutrition 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
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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
- B01D53/46—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
- 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
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/602—Oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/606—Carbonates
-
- 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
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention provides a system for performing flue gas desulfurization by using cement kiln tail return ash, which comprises a kiln tail dust-containing flue gas treatment device, a desulfurization tower and a desulfurizer slurry treatment device; the device for treating the dust-containing smoke at the tail of the kiln removes dust from the dust-containing smoke at the tail of the kiln to obtain dust-free smoke and return dust at the tail of the kiln, and comprises a dust remover, a smoke pipe, an induced draft fan, a chute and a conveyor, wherein the top end of the chute is connected with the bottom of the dust remover, the bottom end of the chute is connected with the conveyor, and the induced draft fan is arranged on the smoke pipe outside the dust remover; a dust and mist removal device, a spraying layer, an air flow uniform distribution plate, a pre-spraying device and a slurry pool are arranged in the desulfurizing tower, and a flue gas pipe outside the dust remover is connected with the pre-spraying device; the desulfurizer slurry treatment device comprises a tower external circulation tank, a desulfurizer tank and a slurry mixing tank, wherein the slurry tank is communicated with the tower external circulation tank through a pipeline, slurry in the desulfurizer tank is conveyed to the pre-spraying device through a primary pump, and kiln tail return ash is conveyed to the slurry mixing tank through a conveyor. The invention also provides a method for flue gas desulfurization by using the cement kiln tail return ash.
Description
Technical Field
The invention belongs to the technical field of environmental protection, and particularly relates to a system and a method for performing flue gas desulfurization by using cement kiln tail return ash.
Background
With the rapid development of economy, the energy consumption is increased year by year, and the environmental pollution is more and more serious. The exhaust emission is increased year by year, and the exhaust emission is emitted to the atmospheric environment, which causes serious haze pollution. The industries of power plants, steel and the like gradually implement ultralow emission of flue gas, namely the emission of sulfur dioxide is lower than 35mg/Nm3. China is a major country for cement production and consumption, cement is an important building material, and the national standard emission of sulfur dioxide in a cement kiln is 200mg/Nm3With the increasing environmental requirements of China, the ultra-low emission of cement kilns becomes a key treatment field.
The traditional cement kiln flue gas desulfurization generally needs sodium alkali, hydrated lime, an oxidant, urea and the like as a desulfurizing agent, the cost of raw materials is high, the ultralow emission standard is difficult to achieve, and generated byproducts cannot be treated to form secondary pollution. The cement production process in the prior art generally comprises the following steps: the first step of crushing and pre-homogenizing, namely crushing the ore raw material; step two, raw material preparation; thirdly, raw material homogenization, wherein a raw material homogenization system plays a last bang role in stabilizing the components of the raw materials entering the cellar; the fourth step is preheating decomposition, preheating and partial decomposition of raw meal are completed by a preheater; the fifth step is a core step, the cement clinker is generated by using a rotary kiln; finally, the cement is ground to form a certain grain composition. In the cement production process, high-temperature sulfur-containing dust-containing flue gas (the temperature is 100-130 ℃) is generated at the kiln tail of the rotary kiln, dust in the flue gas is collected through cloth bag dust removal or electric dust removal, the dust is called kiln tail return ash, and the main components of the kiln tail return ash are calcium carbonate, silica, alumina, clay, calcium oxide and the like. At present, an effective recycling method for kiln tail ash return is lacked.
In summary, there is a need to develop an efficient system and method for desulfurizing flue gas of a cement kiln by using returned ash at the tail of the cement kiln, so as to solve the problems in the prior art that the desulfurization efficiency of the flue gas of the cement kiln is low and the emission product can not meet the emission standard.
The invention content is as follows:
the invention aims to provide a system and a method for performing flue gas desulfurization by using cement kiln tail return ash, and aims to solve the problems that the traditional cement kiln flue gas desulfurization efficiency is low and the emission product cannot reach the emission standard in the prior art.
In order to achieve the purpose, the invention adopts the following technical scheme:
a system for flue gas desulfurization by using cement kiln tail return ash comprises a kiln tail dust-containing flue gas treatment device, a desulfurization tower and a desulfurizer slurry treatment device; the device for treating the dust-containing flue gas at the tail of the kiln is used for dedusting the dust-containing flue gas at the tail of the kiln to obtain the dust-free flue gas and the return ash at the tail of the kiln, and comprises a dust remover, a flue gas pipe, an induced draft fan, a chute and a conveyor, wherein the top end of the chute is connected with the bottom of the dust remover, the bottom end of the chute is connected with the conveyor, and the induced draft fan is arranged on the flue gas pipe outside the dust remover; a dust removal demister, a spraying layer, an airflow uniform distribution plate, a pre-spraying device and a slurry pool are arranged in the desulfurizing tower from top to bottom, and a flue gas pipe outside the dust remover is connected with the pre-spraying device; the desulfurizer slurry treatment device comprises a tower external circulation tank, a desulfurizer tank and a slurry melting tank which are sequentially connected through a pipeline, wherein the slurry tank is communicated with the tower external circulation tank through a pipeline, desulfurizer slurry in the desulfurizer tank is conveyed to the pre-spraying device through a primary pump, and a conveyor is used for conveying kiln tail return ash after dust removal treatment to the slurry melting tank.
In another preferred embodiment, the desulfurization tower further comprises a return pipe and a secondary circulating pump, two ends of the return pipe are respectively connected with the spraying layer and the slurry tank, the secondary circulating pump is arranged on the return pipe, and the secondary circulating pump conveys slurry in the slurry tank to the spraying layer.
In another preferred embodiment, the number of the return pipes and the two-stage circulating pumps is 2-5 groups, the number of the spraying layers is 2-5 layers, and each group of the return pipes and the two-stage circulating pumps corresponds to one spraying layer.
In another preferred embodiment, a stirring mechanism is arranged in the slurry tank, and a stirring mechanism is arranged in the tower external circulation tank.
In another preferred embodiment, the system further comprises a desulfurization byproduct treatment device, wherein the desulfurization byproduct treatment device comprises cyclones arranged according to the process, a vacuum belt dehydrator and a vacuum pump, a discharge pump is arranged on a pipeline communicated with the cyclones of the tower external circulation tank, the vacuum belt dehydrator is arranged below the cyclones, and the vacuum pump and the vacuum belt dehydrator are used for dehydrating the slurry treated by the cyclones.
In another preferred embodiment, the tower external circulation tank is connected with the desulfurizer tank through a pipeline, and a stirring mechanism is also arranged in the desulfurizer tank.
In another preferred embodiment, the desulfurization byproduct treatment device conveys the dehydrated water to the slurry tank through a pipeline.
The invention also provides a method for performing flue gas desulfurization by using the cement kiln tail return ash, and the system for performing flue gas desulfurization by using the cement kiln tail return ash comprises the following steps:
s1, treating the dust-containing flue gas at the tail of the kiln: dedusting the kiln tail dust-containing flue gas by using a kiln tail dust-containing flue gas treatment device to obtain dust-free flue gas and kiln tail return ash, wherein the dust-free flue gas is sent to a pre-spraying device of a desulfurizing tower through a draught fan, and the kiln tail return ash is conveyed to a slurry pond of a desulfurizing agent slurry treatment device and dissolved in water to obtain desulfurizing agent slurry;
s2, reacting the desulfurizer slurry with dust-free flue gas at one time: conveying the desulfurizer slurry in the slurry melting tank to a desulfurizer tank, conveying the desulfurizer slurry in the desulfurizer tank to a pre-spraying device of a desulfurization tower through a primary pump, carrying out primary reaction on the desulfurizer slurry at the pre-spraying device and sulfur dioxide in dust-free flue gas, and storing the reacted desulfurizer slurry in a slurry tank at the bottom of the desulfurization tower;
s3 desulfurizing agent slurry treatment: and conveying the desulfurizer slurry reacted in the slurry tank to an external circulation tank of the tower, blowing air into the external circulation tank of the tower for oxidation reaction, inputting part of the slurry in the external circulation tank of the tower into the desulfurizer tank through a pipeline, and adding part of the desulfurizer slurry in the slurry tank into the desulfurizer tank.
In another preferred embodiment, after the step S2 and before the step S3, the method further comprises a secondary reaction of the desulfurizing agent slurry with the dust-free flue gas: conveying the desulfurizer slurry in the slurry pool to the spraying layer through a second-stage circulating pump, atomizing the desulfurizer slurry into liquid drops by a nozzle at the tail end of the spraying pipe, fully contacting with dust-free flue gas and carrying out secondary reaction. In another more preferred embodiment, when the desulfurizing agent slurry is subjected to secondary reaction with the dust-free flue gas, the pH value of the desulfurizing agent slurry is 4.9-5.6. Thus, the multi-layer spraying combination can generate better desulfurization effect, and the emission concentration of sulfur dioxide can be stably lower than 35mg/Nm3。
In another preferred embodiment, in the step S2, the pH of the desulfurizing agent slurry is 5.6 to 6.4 in the primary reaction of the desulfurizing agent slurry and the dust-free flue gas. Thus, the reaction of the desulfurizing agent slurry and the sulfur dioxide is quicker.
In another preferred embodiment, in step S3, before the reacted desulfurizing agent slurry in the slurry pool is sent to the tower external circulation pool, air is blown into the slurry pool at the bottom of the desulfurizing agent by the oxidation fan to stir the desulfurizing agent slurry for oxidation reaction.
In another preferred embodiment, the step S3 is followed by a step S4 of desulfurization by-product treatment: and conveying part of the slurry in the tower external circulation pool to a desulfurization byproduct treatment device through a discharge pump for dehydration treatment to obtain a desulfurization byproduct with the main component of dihydrate gypsum.
In another preferred embodiment, the dihydrate gypsum byproduct obtained in the desulfurization byproduct treatment of step S4 is transported to a cement production line, and added to cement clinker as a production additive, so as to realize the recycling of byproduct resources.
The invention has the following beneficial effects:
1. the system of the invention utilizes the kiln tail dust-containing flue gas treatment device to carry out dust removal treatment on the kiln tail dust-containing flue gas to obtain dust-free flue gas and kiln tail return ash, and the chute and the conveyor send the kiln tail return ash stored in the dust remover ash bucket to the slurry tank and dissolve the kiln tail return ash in water to generate desulfurizer slurry which can be used as a desulfurizer of the dust-free flue gas; and (3) pressurizing the kiln tail flue gas subjected to dust removal by a draught fan, sending the pressurized kiln tail flue gas into a desulfurizing tower, and reacting the pressurized kiln tail flue gas with desulfurizing agent slurry. The system has the advantages of exquisite structure, low cost, full utilization of the existing equipment on the cement production line and low investment.
2. The kiln tail return ash contains more impurities and has low activity. In order to ensure the full reaction between the desulfurizer slurry and the dust-free flue gas and improve the desulfurization efficiency, the scheme adopts the one-time pre-spraying at the inlet of the desulfurization tower, so that the desulfurizer slurry and the dust-free flue gas react at one time; and then, circulating spraying is arranged in the desulfurizing tower, namely, the desulfurizing agent slurry in the slurry pool at the bottom of the desulfurizing tower is conveyed to the spraying layer again, so that the desulfurizing agent slurry and the dust-free flue gas are subjected to secondary reaction. 2-5 layers can be arranged in the circulating spray, so that the full reaction between the desulfurizer slurry and the dust-free flue gas can be ensured to the utmost extentCan remove the sulfur dioxide in the flue gas by reaction. The pre-spraying adopts a higher pH value of 5.6-6.4, so that the reaction of the desulfurizer slurry and sulfur dioxide is faster; meanwhile, the tower internal circulation spraying adopts a lower pH value of 4.9-5.6, the multilayer spraying combination can generate a better desulfurization effect, and the emission concentration of sulfur dioxide can be stably lower than 35mg/Nm3. Through a dust and mist eliminator of the high-efficiency mist eliminator, the emission concentration of particulate matters is lower than 10mg/Nm3。
3. Because the kiln tail return ash contains fine particles such as alumina, silica, clay and the like, the desulfurization slurry is sticky, the slurry is not easy to oxidize, and gypsum particles are not easy to crystallize. Therefore, stirring mechanisms are arranged in a slurry pool and an external circulation pool in the desulfurization tower, and the desulfurizer slurry reacted with the dedusting flue gas is subjected to forced oxidation twice in the slurry pool and the external circulation pool, so that the oxidation is more sufficient, and the gypsum crystallization amount and the gypsum quality in the desulfurization byproduct treatment process are facilitated; and the desulfurized byproducts can be used as a retarder in a cement production line, so that the resource recycling is realized, and the secondary pollution is avoided.
4. The invention relates to a method for flue gas desulfurization by using cement kiln tail return ash, which directly removes dust and separates the kiln tail flue gas of a rotary kiln during cement production to obtain dust-free flue gas and kiln tail return ash, and then dissolves the kiln tail return ash in water as desulfurizer slurry with the concentration of 15-20%. And then the desulfurizer slurry is adopted to react with dust-free flue gas, sulfur dioxide in the dust-free flue gas reacts with calcium carbonate, calcium oxide and other components in the desulfurizer to generate calcium sulfite, the flue gas sequentially passes through an air flow uniform distribution plate, a spray pipe and a high-efficiency demister in a desulfurization tower, and the purified flue gas is finally discharged into a chimney. The raw material of a desulfurizing agent does not need to be purchased, so that the desulfurizing cost is greatly saved; every time 1kg of sulfur dioxide is removed, 2.1kg of kiln tail return ash can be consumed, and 3.1kg of gypsum by-products are generated. The desulfurization effect of the dust-free flue gas is good, the ultralow emission standard is achieved, and the method is very environment-friendly.
Drawings
FIG. 1 is a schematic structural view of a system for flue gas desulfurization using cement kiln tail fly-back ash in example 1;
FIG. 2 is a schematic structural diagram of a system for flue gas desulfurization using cement kiln tail fly-back ash in example 2 (hiding a pipeline connected between a conveyor and a slurry pond);
FIG. 3 is a schematic flow chart of a method for flue gas desulfurization using cement kiln tail fly-back ash in example 2.
Reference numerals:
1-dust remover 2-chute 3-conveyor
4-induced draft fan 5-desulfurizing tower 6-dust-removing demister
7-spraying layer 8-airflow uniform distribution plate 9-pre-spraying device
10-two-stage circulating pump 11-slurry pool 12-oxidation fan
13-slurry melting tank 14-tower external circulation tank 15-desulfurizing agent slurry tank
16-first-stage pump 17-process water tank 18-flushing water pump
19-process water pump 20-cyclone 21-vacuum belt dehydrator
22-vacuum pump 23-discharge pump 24-stirring mechanism
Detailed Description
Reference will now be made to the description to illustrate selected embodiments of the present invention, and the following description of the embodiments of the present invention, which is based on the present disclosure, is by way of illustration only and is not intended to limit the scope of the invention.
Example 1
Referring to fig. 1, the present embodiment is a system for performing flue gas desulfurization by using cement kiln tail return ash, and the system includes a kiln tail dust-containing flue gas treatment device, a desulfurization tower, and a desulfurizer slurry treatment device. The device for treating the dust-containing flue gas at the tail of the kiln removes dust to obtain the dust-free flue gas and the return ash at the tail of the kiln, and comprises a dust remover, a flue gas pipe, an induced draft fan, a chute and a conveyor, wherein the top end of the chute is connected with the bottom of the dust remover, the bottom end of the chute is connected with the conveyor, and the induced draft fan is arranged on the flue gas pipe outside the dust remover; the dust-containing flue gas at the tail of the cement kiln enters a dust remover and is separated into dust-free flue gas and kiln tail return ash through the dust remover, wherein the kiln tail return ash enters through a chute and is conveyed to a desulfurizer slurry treatment device through a conveyor. Inside from last dust removal defroster, spray layer, air current equipartition board, spray set and thick liquid pond in advance of being provided with down of desulfurizing tower, the outside flue gas pipe of dust remover is connected with spray set in advance, and the draught fan carries dustless flue gas to spray set in advance and get into the desulfurizing tower. The desulfurizer slurry treatment device comprises a tower external circulation tank, a desulfurizer tank and a slurry dissolving tank which are sequentially connected through a pipeline, wherein the slurry tank at the bottom of the desulfurization tower is communicated with the tower external circulation tank through the pipeline, the desulfurizer slurry in the desulfurizer tank is conveyed to a pre-spraying device of the desulfurization tower through a primary pump, the conveyor conveys the dust-removed kiln tail return ash to the slurry dissolving tank, and a stirring mechanism is arranged in the slurry dissolving tank to mix the kiln tail return ash with water to generate the desulfurizer slurry.
In the flue gas desulfurization system of the embodiment, the kiln tail dust-containing flue gas is subjected to dust removal treatment by using the kiln tail dust-containing flue gas treatment device to obtain dust-free flue gas and kiln tail return ash, the chute and the conveyor convey the kiln tail return ash stored in the dust remover ash bucket to the slurry tank and dissolve the kiln tail return ash in water to generate desulfurizer slurry which is used as a desulfurizer for the dust-free flue gas; and (3) pressurizing the kiln tail flue gas subjected to dust removal by a draught fan, sending the pressurized kiln tail flue gas into a desulfurizing tower, and reacting the pressurized kiln tail flue gas with desulfurizing agent slurry. The existing kiln tail dust-containing flue gas treatment device on a cement production line is utilized to separate the dust-free flue gas from the kiln tail return ash, and a desulfurization tower is utilized to realize the desulfurization treatment of the flue gas; the system has the advantages of low investment, low cost and strong practicability.
Briefly described, the flue gas desulfurization method using the flue gas desulfurization system shown in fig. 1, which uses the cement kiln tail ash return, comprises the following steps:
s1, treating the dust-containing flue gas at the tail of the kiln: dedusting the kiln tail dust-containing flue gas by using a kiln tail dust-containing flue gas treatment device to obtain dust-free flue gas and kiln tail return ash, wherein the dust-free flue gas is sent to a pre-spraying device of a desulfurizing tower through a draught fan, and the kiln tail return ash is conveyed to a slurry pond of a desulfurizing agent slurry treatment device and dissolved in water to obtain desulfurizing agent slurry;
s2, reacting the desulfurizer slurry with dust-free flue gas at one time: conveying the desulfurizer slurry in the slurry melting tank to a desulfurizer tank, conveying the desulfurizer slurry in the desulfurizer tank to a pre-spraying device of a desulfurization tower through a primary pump, carrying out primary reaction on the desulfurizer slurry at the pre-spraying device and sulfur dioxide in dust-free flue gas, and storing the reacted desulfurizer slurry in a slurry tank at the bottom of the desulfurization tower;
s3 desulfurizing agent slurry treatment: and conveying the desulfurizer slurry reacted in the slurry tank to an external circulation tank of the tower, blowing air into the external circulation tank of the tower for oxidation reaction, inputting part of the slurry in the external circulation tank of the tower into the desulfurizer tank through a pipeline, and adding part of the desulfurizer slurry in the slurry tank into the desulfurizer tank.
In the method for flue gas desulfurization by using cement kiln tail return ash in the embodiment, the dust removal separation of the kiln tail flue gas of the rotary kiln during cement production is directly carried out to obtain the dust-free flue gas and the kiln tail return ash, and then the kiln tail return ash is dissolved in water to be used as desulfurizer slurry with the concentration of 15-20%, so that a desulfurizer raw material does not need to be purchased, and the desulfurization cost is greatly saved. And then the desulfurizer slurry is adopted to react with dust-free flue gas, sulfur dioxide in the dust-free flue gas reacts with calcium carbonate, calcium oxide and other components in the desulfurizer to generate calcium sulfite, the flue gas sequentially passes through an air flow uniform distribution plate, a spray pipe and a high-efficiency demister in a desulfurization tower, and the purified flue gas is finally discharged into a chimney. When 1kg of sulfur dioxide is removed, 2.1kg of kiln tail return ash can be consumed. The desulfurization effect of the dust-free flue gas is good, the ultralow emission standard is achieved, and the method is very environment-friendly.
Continuing to refer to fig. 1, on the basis of this embodiment, in another modified embodiment, the desulfurization tower further includes a return pipe and a secondary circulation pump, two ends of the return pipe are respectively connected with the spraying layer and the slurry tank, the secondary circulation pump is disposed on the return pipe, and the secondary circulation pump conveys the slurry in the slurry tank to the spraying layer. In the attached figure 1, the number of the return pipes and the two-stage circulating pumps is 3 groups, the spraying layers are 3 layers, and each group of the return pipes and the two-stage circulating pumps correspond to one spraying layer. In other embodiments, 2-5 groups of return pipes and two-stage circulating pumps can be arranged according to actual conditions, and the spraying layers with the same number as the return pipes are configured. The arrangement can ensure that the desulfurizing agent slurry and the dust-free flue gas are fully reacted, and the sulfur dioxide in the flue gas is removed as much as possible. Pre-spray time desulfurizationThe pH value of the agent slurry is 5.6-6.4, so that the reaction of the desulfurizer slurry and sulfur dioxide is quicker; meanwhile, when the tower is internally circulated and sprayed, the pH value of the desulfurizer is 4.9-5.6, better desulfurization effect can be generated by multi-layer spraying combination, and the emission concentration of sulfur dioxide can be stably lower than 35mg/Nm3. Through a dust and mist eliminator of the high-efficiency mist eliminator, the emission concentration of particulate matters is lower than 10mg/Nm3。
Referring to the attached fig. 1, on the basis of this embodiment, in another modified embodiment, a stirring mechanism is arranged in the slurry tank, an oxidation fan (2 oxidation fans are arranged in fig. 1 for standby) is arranged outside the desulfurization tower, and the oxidation fan blows air into the slurry tank so that the slurry in the tank is oxidized by the air. Because the kiln tail return ash contains fine particles such as alumina, silica, clay and the like, the desulfurization slurry is sticky, the slurry is not easy to oxidize, and gypsum particles are not easy to crystallize. Therefore, the slurry pool in the desulfurizing tower is provided with the stirring mechanism, and the desulfurizing agent slurry reacted with the dedusting flue gas is subjected to oxidation reaction with air in the slurry pool, so that the oxidation is more sufficient, and the subsequent recycling of the desulfurizing agent slurry is facilitated.
Referring to the attached figure 1, on the basis of the embodiment, in another modified embodiment, an agitating mechanism is arranged in the tower external circulation pool. The desulfurizer slurry reacted with the dedusting flue gas in the slurry pool at the bottom of the desulfurizing tower enters the tower external circulation pool, and the stirring mechanism can ensure that the slurry is more fully contacted with air, so that the forced oxidation of the desulfurizer slurry is realized, the oxidation is more sufficient, and the subsequent treatment of the desulfurizer slurry is facilitated.
Example 2
Referring to fig. 2, in the system for flue gas desulfurization by using cement kiln tail ash return in the present embodiment, a desulfurization byproduct treatment device is further added on the basis of embodiment 1. The desulfurization byproduct treatment device comprises a cyclone, a vacuum belt dehydrator and a vacuum pump which are arranged according to the working procedures, wherein a discharge pump is arranged on a pipeline which is communicated with the cyclone and is arranged outside the tower; the vacuum belt dehydrator is arranged below the cyclone, and the vacuum pump and the vacuum belt dehydrator are used for dehydrating the slurry treated by the cyclone. Wherein the tower external circulation tank is connected with the desulfurizer tank through a pipeline, and the desulfurizer tank is also internally provided with a stirring mechanism. And the desulfurization byproduct treatment device conveys the dehydrated water to the slurry tank through a pipeline.
In this embodiment, still be provided with the process water tank, carry the moisture in the process water tank to washing dust removal defroster in the desulfurizing tower through the washing water pump, carry the moisture in the process water tank to vacuum belt hydroextractor through the process water pump.
By the arrangement, the desulfurizer slurry reacted with the dust-free flue gas can be recycled by the desulfurization byproduct treatment device to generate dihydrate gypsum; and the water produced in the desulfurization byproduct treatment process can be added into a slurry pond and used for dissolving kiln tail return ash to form desulfurizer slurry. All the components are effectively utilized, and no secondary pollution exists; and the sulfur dioxide emission concentration and the particulate matter emission concentration both meet the national standard, thereby being very environment-friendly.
Referring to the attached drawings 2 and 3, the method for performing flue gas desulfurization by using cement kiln tail return ash by using the system for performing flue gas desulfurization by using cement kiln tail return ash comprises the following steps:
s1, treating the dust-containing flue gas at the tail of the kiln: dedusting the kiln tail dust-containing flue gas by using a kiln tail dust-containing flue gas treatment device to obtain dust-free flue gas and kiln tail return ash, wherein the dust-free flue gas is sent to a pre-spraying device of a desulfurizing tower through a draught fan, and the kiln tail return ash is conveyed to a slurry pond of a desulfurizing agent slurry treatment device and dissolved in water to obtain desulfurizing agent slurry;
s2, reacting the desulfurizer slurry with dust-free flue gas at one time: conveying the desulfurizer slurry in the slurry melting tank to a desulfurizer tank, conveying the desulfurizer slurry in the desulfurizer tank to a pre-spraying device of a desulfurization tower through a primary pump, carrying out primary reaction on the desulfurizer slurry at the pre-spraying device and sulfur dioxide in dust-free flue gas, and storing the reacted desulfurizer slurry in a slurry tank at the bottom of the desulfurization tower; then carrying out secondary reaction of the desulfurizer slurry and dust-free flue gas: conveying the desulfurizer slurry in the slurry pool to the spraying layer through a second-stage circulating pump, atomizing the desulfurizer slurry into liquid drops by a nozzle at the tail end of the spraying pipe, fully contacting with dust-free flue gas and carrying out secondary reaction. In another more preferred embodimentIn the embodiment, when the desulfurizing agent slurry and the dust-free flue gas are subjected to secondary reaction, the pH value of the desulfurizing agent slurry is 4.9-5.6. Thus, the multi-layer spraying combination can generate better desulfurization effect, and the emission concentration of sulfur dioxide can be stably lower than 35mg/Nm3。
S3 desulfurizing agent slurry treatment: and conveying the desulfurizer slurry reacted in the slurry tank to an external circulation tank of the tower, blowing air into the external circulation tank of the tower for oxidation reaction, inputting part of the slurry in the external circulation tank of the tower into the desulfurizer tank through a pipeline, and adding part of the desulfurizer slurry in the slurry tank into the desulfurizer tank.
S4 desulfurization byproduct treatment: and conveying part of the slurry in the tower external circulation pool to a desulfurization byproduct treatment device through a discharge pump for dehydration treatment to obtain a desulfurization byproduct with the main component of dihydrate gypsum. The obtained dihydrate gypsum by-product is conveyed to a cement production line and added into cement clinker to be used as a production additive, so that the recycling of the by-product resource is realized.
In the method for flue gas desulfurization by using cement kiln tail return ash, dihydrate gypsum crystals with qualified quality can be generated in the desulfurization byproduct treatment process, and the dihydrate gypsum can be used as a retarder in a cement production line, so that resource recycling is realized, and secondary pollution is avoided. Test calculation shows that 3.1kg of dihydrate gypsum can be generated by removing 1kg of sulfur dioxide.
In another preferred embodiment, in step S3, before the reacted desulfurizing agent slurry in the slurry pool is sent to the tower external circulation pool, air is blown into the slurry pool at the bottom of the desulfurizing agent by the oxidation fan to stir the desulfurizing agent slurry for oxidation reaction. Blowing air into the slurry tank in the desulfurizing tower through the oxidation fan, and forcibly oxidizing the desulfurizing agent slurry after the reaction with the dedusting flue gas in the slurry tank, so that the oxidation is more sufficient, and the gypsum crystallization amount and the gypsum quality in the desulfurization byproduct treatment process are facilitated.
Based on this embodiment, in another preferred embodiment, in the step S2, the pH of the desulfurizing agent slurry transported from the desulfurizing agent slurry pool is 5.6-6.4 in the primary reaction of the desulfurizing agent slurry and the dust-free flue gas. Thus, the device is provided withThe reaction of the desulfurizer slurry with sulfur dioxide is faster. When the desulfurization tower is internally and circularly sprayed, the pH value of the desulfurizer slurry is 4.9-5.6, and the multilayer spraying combination can generate better desulfurization effect, so that the sulfur dioxide emission concentration can be stably lower than 35mg/Nm after the desulfurization treatment of dust-free flue gas3。
Finally, it should be noted that the above embodiments are only used for illustrating the technical solutions of the present application and not for limiting the protection scope thereof, and although the present application is described in detail with reference to the above embodiments, those of ordinary skill in the art should understand that: numerous variations, modifications, and equivalents will occur to those skilled in the art upon reading the present application and are within the scope of the claims as issued or as granted.
Claims (11)
1. A system for flue gas desulfurization by using cement kiln tail return ash is characterized by comprising a kiln tail dust-containing flue gas treatment device, a desulfurization tower and a desulfurizer slurry treatment device; the device for treating the dust-containing flue gas at the tail of the kiln is used for dedusting the dust-containing flue gas at the tail of the kiln to obtain the dust-free flue gas and the return ash at the tail of the kiln, and comprises a dust remover, a flue gas pipe, an induced draft fan, a chute and a conveyor, wherein the top end of the chute is connected with the bottom of the dust remover, the bottom end of the chute is connected with the conveyor, and the induced draft fan is arranged on the flue gas pipe outside the dust remover; a dust removal demister, a spraying layer, an airflow uniform distribution plate, a pre-spraying device and a slurry pool are arranged in the desulfurizing tower from top to bottom, and a flue gas pipe outside the dust remover is connected with the pre-spraying device; the desulfurizer slurry treatment device comprises a tower external circulation tank, a desulfurizer tank and a slurry melting tank which are sequentially connected through a pipeline, wherein the slurry tank is communicated with the tower external circulation tank through a pipeline, desulfurizer slurry in the desulfurizer tank is conveyed to the pre-spraying device through a primary pump, and a conveyor is used for conveying kiln tail return ash after dust removal treatment to the slurry melting tank.
2. The system for performing flue gas desulfurization by using cement kiln tail return ash according to claim 1, wherein the desulfurization tower further comprises a return pipe and a secondary circulating pump, two ends of the return pipe are respectively connected with the spraying layer and the slurry tank, the secondary circulating pump is arranged on the return pipe, and the secondary circulating pump conveys slurry in the slurry tank to the spraying layer.
3. The system for flue gas desulfurization by using cement kiln tail return ash according to claim 2, wherein the number of the return pipes and the secondary circulating pumps is 2-5 groups, the number of the spraying layers is 2-5 layers, and each group of the return pipes and the secondary circulating pumps corresponds to one spraying layer.
4. The system for flue gas desulfurization by using cement kiln tail return ash according to claim 2, characterized in that a stirring mechanism is arranged in the slurry tank, and a stirring mechanism is arranged in the tower external circulation tank.
5. The system for flue gas desulfurization by using cement kiln tail ash return according to any one of claims 1 to 4, further comprising a desulfurization byproduct treatment device, wherein the desulfurization byproduct treatment device comprises a cyclone, a vacuum belt dehydrator and a vacuum pump which are arranged according to the procedures, a discharge pump is arranged on a pipeline communicating the tower external circulation tank and the cyclone, the vacuum belt dehydrator is arranged below the cyclone, and the vacuum pump and the vacuum belt dehydrator are used for dehydrating the slurry treated by the cyclone.
6. The system for flue gas desulfurization by using cement kiln tail return ash according to claim 5, wherein the tower external circulation tank is connected with the desulfurizer tank through a pipeline, and a stirring mechanism is also arranged in the desulfurizer tank.
7. The system for flue gas desulfurization by using cement kiln tail return ash according to claim 5, wherein the desulfurization byproduct treatment device conveys the dehydrated water to the slurrying pool through a pipeline.
8. A method for performing flue gas desulfurization by using cement kiln tail return ash, which is characterized in that the system for performing flue gas desulfurization by using cement kiln tail return ash, which is disclosed by any one of claims 1 to 7, comprises the following steps:
s1, treating the dust-containing flue gas at the tail of the kiln: dedusting the kiln tail dust-containing flue gas by using a kiln tail dust-containing flue gas treatment device to obtain dust-free flue gas and kiln tail return ash, wherein the dust-free flue gas is sent to a pre-spraying device of a desulfurizing tower through a draught fan, and the kiln tail return ash is conveyed to a slurry pond of a desulfurizing agent slurry treatment device and dissolved in water to obtain desulfurizing agent slurry;
s2, reacting the desulfurizer slurry with dust-free flue gas at one time: conveying the desulfurizer slurry in the slurry melting tank to a desulfurizer tank, conveying the desulfurizer slurry in the desulfurizer tank to a pre-spraying device of a desulfurization tower through a primary pump, carrying out primary reaction on the desulfurizer slurry at the pre-spraying device and sulfur dioxide in dust-free flue gas, and storing the reacted desulfurizer slurry in a slurry tank at the bottom of the desulfurization tower;
s3 desulfurizing agent slurry treatment: and conveying the desulfurizer slurry reacted in the slurry tank to an external circulation tank of the tower, blowing air into the external circulation tank of the tower for oxidation reaction, inputting part of the slurry in the external circulation tank of the tower into the desulfurizer tank through a pipeline, and adding part of the desulfurizer slurry in the slurry tank into the desulfurizer tank.
9. The method for flue gas desulfurization by using cement kiln tail return ash according to claim 8, further comprising a secondary reaction of a desulfurizing agent slurry with dust-free flue gas after the step S2 and before the step S3: conveying the desulfurizer slurry in the slurry pool to the spraying layer through a second-stage circulating pump, atomizing the desulfurizer slurry into liquid drops by a nozzle at the tail end of the spraying pipe, fully contacting with dust-free flue gas and carrying out secondary reaction.
10. The method for flue gas desulfurization by using cement kiln tail return ash according to claim 9, characterized in that the step S3 is followed by a step S4 of desulfurization byproduct treatment: and conveying part of slurry in the tower external circulation pool to a desulfurization byproduct treatment device through a discharge pump for dehydration treatment to obtain a desulfurization byproduct with the main component of dihydrate gypsum.
11. The method for flue gas desulfurization by using cement kiln tail return ash according to claim 10, wherein the dihydrate gypsum byproduct obtained in the desulfurization byproduct treatment of step S4 is transported to a cement production line and added to cement clinker as a production additive to realize the recycling of byproduct resources.
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