CN110201511A - A kind of ceramic industry kiln desulfuration processing method - Google Patents

A kind of ceramic industry kiln desulfuration processing method Download PDF

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Publication number
CN110201511A
CN110201511A CN201910516540.8A CN201910516540A CN110201511A CN 110201511 A CN110201511 A CN 110201511A CN 201910516540 A CN201910516540 A CN 201910516540A CN 110201511 A CN110201511 A CN 110201511A
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China
Prior art keywords
flue gas
absorption tower
ceramic industry
processing method
desulfurization
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CN201910516540.8A
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Chinese (zh)
Inventor
周玉祥
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HEFEI TIANXIANG ENVIRONMENTAL ENGINEERING Co Ltd
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HEFEI TIANXIANG ENVIRONMENTAL ENGINEERING Co Ltd
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Priority to CN201910516540.8A priority Critical patent/CN110201511A/en
Publication of CN110201511A publication Critical patent/CN110201511A/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
    • 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
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • 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
    • B01D53/75—Multi-step processes
    • 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
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • 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
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • 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
    • B01D2251/402—Alkaline earth metal or magnesium compounds of magnesium
    • 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
    • B01D2258/0283—Flue gases

Abstract

The invention discloses a kind of ceramic industry kiln desulfuration processing methods, specifically includes the following steps: S1, first, sulfur-containing smoke gas enters inside deduster be dusted after, then, the bulky grain flue dust in flue gas removes substantially after cooling, finally, the magnesia through curing, which generates magnesium hydroxide and process water, is reduced to 100 DEG C -150 DEG C, while Mg (OH) for flue dust temperature by the evaporation of heat exchanger2Liquid removes the hydrogen halide in flue gas substantially；S2, firstly, flue gas is warming up to inside 170 DEG C or so input absorption towers after dedusting dehalogenation by flue gas heater by flue gas, while supplementing Mg (OH) into absorption tower in time2Liquid, then, after the loop slurry in flue gas and absorption tower comes into full contact with, finally, the SO in flue gas2It is oxidized to MgSO3, it is discharged after the flue gas of desulfurization process carries out demisting processing from chimney；S3, firstly, SO in flue gas2Through Mg (OH)2Oxidation generate MgSO3SO is generated by the laggard high temperature calcining and decomposing of crossing of dehydration2And MgO.

Description

A kind of ceramic industry kiln desulfuration processing method
Technical field
Invention is related to technical field of desulfurization, specially a kind of ceramic industry kiln desulfuration processing method.
Background technique
Ceramic industry kiln can generate the mixed flue gas such as sulfur dioxide and hydrogen halides during carrying out Production of Ceramics, and two Sulfur oxide is one of common, simplest oxysulfide and Air Pollutant Discharge, during industrial gas emission, when The sulfur dioxide of discharge is merged with rainwater, and will form sulfurous acid and sulfurous acid and further aoxidize will produce a large amount of sulfuric acid i.e. The main component of acid rain, thus huge destruction is caused to environment, while sulfur dioxide is also one of carcinogenic substance, therefore for combustion Coal industry and ceramic industry, develop the reasonable desulfurization process method of more system, advantageously reduce sulfur dioxide and halogen Change hydrogen discharge amount, be conducive to protect environment, avoid environmental pollution, for desulfurization process method there are many kinds of, usually Be divided into wet process, dry method and semidry method three categories, generally use most technologies it is most mature be Wet Flue Gas Desulfurization Technique.
Meanwhile traditional limestone/lime-gypsum method flue gas desulfurization treatment process absorbs titanium dioxide using calcium-based desulfurizing agent The calcium sulfite and calcium sulfate produced after sulphur is easily tied in the inner wall duct of absorption tower since the dissolubility of its own is smaller Dirt, and then lead to line clogging, so that equipment breaks down, increase maintenance cost, simultaneously because calcium in calcium-based desulfurizing agent The dissolution alkalinity and desulphurizing ability of ion is not high, it is therefore desirable to which a large amount of shower water is catalyzed, while power consumption is huge, fortune Row is at high cost, unfavorable to use with having more large-tonnage enterprise, it is therefore desirable to make moderate progress.
Summary of the invention
Invention is designed to provide a kind of ceramic industry kiln desulfuration processing method, to solve to mention in above-mentioned background technique Out the problem of.
To achieve the above object, invention provides the following technical solutions: a kind of ceramic industry kiln desulfuration processing method, specifically The following steps are included:
S1, firstly, the sulfur-containing smoke gas inside Industrial Stoves enters inside deduster and is dusted after, then, via air inducing Machine enter in heat exchanger carry out it is cooling after bulky grain flue dust in flue gas remove substantially, finally, the magnesia through curing generates hydrogen Flue dust temperature is reduced to 100 DEG C -150 DEG C by the evaporation of heat exchanger by magnesia and process water, while 2 liquid of Mg (OH) is by cigarette Hydrogen halide in gas removes substantially；
S2, firstly, flue gas is warming up to 170 DEG C or so inputs by flue gas heater after dedusting dehalogenation by flue gas absorbs Inside tower, while 2 holding vessel of Mg (OH) supplements Mg (OH) 2 liquid, then, flue gas and absorption tower by pump into absorption tower in time After interior loop slurry comes into full contact with, finally, the SO2 in flue gas is oxidized to MgSO3 by Mg (OH) 2, the flue gas through desulfurization process It is discharged after carrying out demisting processing from chimney；
S3, firstly, the MgSO3 liquid that is generated through the oxidation of Mg (OH) 2 of SO2 in flue gas reactor tank after pipeline inputs, Then, MgSO3 by dehydration it is laggard cross high temperature calcining and decomposing generate SO2 and MgO, finally, SO2 after oxygenolysis be System prepares industrial sulphuric acid with water reaction, and MgO continues on for desulfurization after curing.
Preferably, the internal structure on absorption tower described in step 2 is followed successively by exhaust gases passes, slurries area and de- under upper Sulphur product pathways, and flue gas through exhaust gases passes enters absorption tower and need to meet with slurries area and inversely contacts.
Preferably, according to SO inside absorption tower described in step 22Oxidization condition constantly inputs fresh preparation into absorption tower Mg (OH) 2 so that absorb slurries pH value be maintained at 7.6 or so.
Preferably, absorption tower described in step 2 is equipped with 3-4 layers of spraying layer, and every layer of spraying layer is equipped with a circulating pump, passes through For flue gas after desulfurization process after atomizer is atomized, the free water content in flue gas is less than or equal to 70mg/Nm3。
Preferably, MgSO described in step 33The temperature condition for being dehydrated high-temperature calcination is 500 DEG C -1000 DEG C.
Compared with prior art, advantageous effect of the invention is:
1, the desulfurization process method, the Mg generated after curing using MgO (OH) 2 as Mg-base desulfurizing agent, due to magnesium from The dissolubility of son is higher by hundreds times than calcium ion, thus the desulfurization that Mg-base desulfurizing agent is higher by decades of times compared to calcium-based desulfurizing agent is imitated Fruit, thus Mg-base desulfurizing agent has higher desulfurization effect compared to calcium-based desulfurizing agent, while required water spray is into phase When in the one third of calcium-based desulfurizing agent, production cost is reduced.
2, the desulfurization process method, product solubility is high after Mg-base desulfurizing agent desulfurization, generates compared to calcium-based desulfurizing agent Calcium sulfite and the small product of calcium sulfate solubility be not easy to generate fouling, clogging in the pipeline on absorption tower, improve The service life on absorption tower, maintenance cost decline.
3, the desulfurization process method, the MgSO3 liquid that the SO2 in step 3 in flue gas is generated through the oxidation of Mg (OH) 2 pass through Reactor tank after pipeline input, MgSO3 is by generating SO2 and MgO, SO2 by 500 DEG C of -1000 DEG C of calcining and decomposings after dehydration It is reacted after oxygenolysis with system water and prepares industrial sulphuric acid, MgO continues on for desulfurization after curing, so that desulfurization product obtains To making full use of, the MgO of generation returns system utilization, high financial profit.
4, desulfurization process method, according to SO inside absorption tower described in step 22Oxidization condition is defeated constantly into absorption tower Enter freshly prepared Mg (OH) 2 so that absorb slurries pH value be maintained at 7.6 or so so that pH value control zone of reasonableness it The case where class avoids excessively high easy fouling, too low, will affect reaction effect.
5, the desulfurization process method, absorption tower described in step 2 are equipped with 3-4 layers of spraying layer, and every layer of spraying layer is equipped with one Circulating pump ensure that desulfurization effect, by flue gas through atomizer mist after desulfurization process so that system keeps higher liquid-gas ratio After change, the free water content in flue gas is less than or equal to 70mg/Nm3, so that the drop in flue gas is sufficiently deviate from, and then discharge Clean air out.
Detailed description of the invention
Fig. 1 is a kind of process flow diagram of ceramic industry kiln desulfuration processing method.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts every other Embodiment shall fall within the protection scope of the present invention.
Referring to Fig. 1, invention provides a kind of technical solution: a kind of ceramic industry kiln desulfuration processing method specifically includes Following steps:
S1, firstly, the sulfur-containing smoke gas inside Industrial Stoves enters inside deduster and is dusted after, then, via air inducing Machine enter in heat exchanger carry out it is cooling after bulky grain flue dust in flue gas remove substantially, finally, the magnesia through curing generates hydrogen Flue dust temperature is reduced to 100 DEG C -150 DEG C by the evaporation of heat exchanger by magnesia and process water, while 2 liquid of Mg (OH) is by cigarette Hydrogen halide in gas removes substantially；
S2, firstly, flue gas is warming up to 170 DEG C or so inputs by flue gas heater after dedusting dehalogenation by flue gas absorbs Inside tower, while 2 holding vessel of Mg (OH) supplements Mg (OH) 2 liquid, then, flue gas and absorption tower by pump into absorption tower in time After interior loop slurry comes into full contact with, finally, the SO2 in flue gas is oxidized to MgSO3 by Mg (OH) 2, the flue gas through desulfurization process It is discharged after carrying out demisting processing from chimney；
S3, firstly, the MgSO3 liquid that is generated through the oxidation of Mg (OH) 2 of SO2 in flue gas reactor tank after pipeline inputs, Then, MgSO3 by dehydration it is laggard cross high temperature calcining and decomposing generate SO2 and MgO, finally, SO2 after oxygenolysis be System prepares industrial sulphuric acid with water reaction, and MgO continues on for desulfurization after curing.
The internal structure on absorption tower described in step 2 is followed successively by exhaust gases passes, slurries area and desulfurization product under upper Channel, and flue gas through exhaust gases passes enters absorption tower and need to meet with slurries area and inversely contacts.
According to SO inside absorption tower described in step 22Oxidization condition constantly inputs freshly prepared Mg into absorption tower (OH)2, so that the pH value for absorbing slurries is maintained at 7.6 or so.
Absorption tower described in step 2 is equipped with 3-4 layers of spraying layer, and every layer of spraying layer is equipped with a circulating pump, is passed through by flue gas After desulfurization process after atomizer is atomized, the free water content in flue gas is less than or equal to 70mg/Nm3。
MgSO described in step 33The temperature condition for being dehydrated high-temperature calcination is 500 DEG C -1000 DEG C.
Working principle: flue gas is warming up to after dedusting dehalogenation by flue gas heater by the desulfurization process method, flue gas Inside 170 DEG C or so input absorption towers, while 2 holding vessel of Mg (OH) supplements Mg (OH) 2 liquid by pump into absorption tower in time, Then, after the loop slurry in flue gas and absorption tower comes into full contact with, finally, the SO2 in flue gas is oxidized to MgSO3 by Mg (OH) 2, It is discharged after the flue gas of desulfurization process carries out demisting processing from chimney, Mg (OH) 2 generated after curing using MgO is as magnesium-based Desulfurizing agent, since the dissolubility of magnesium ion is higher by hundreds times than calcium ion, thus Mg-base desulfurizing agent is compared to calcium-based desulfurizing agent height The desulfurization effect of decades of times out, thus Mg-base desulfurizing agent has higher desulfurization effect compared to calcium-based desulfurizing agent, while being wanted The water spray asked is reduced into the one third for being equivalent to calcium-based desulfurizing agent, production cost.The desulfurization process method, Mg-basic desulphuration Product solubility is high after agent desulfurization, the small product of the calcium sulfite and calcium sulfate solubility generated compared to calcium-based desulfurizing agent It is not easy to generate fouling, clogging in the pipeline on absorption tower, improves the service life on absorption tower, maintenance cost decline.It should Desulfurization process method, firstly, the MgSO3 liquid that the SO2 in flue gas is generated through the oxidation of Mg (OH) 2 reacts after pipeline inputs Tank, then, MgSO3 generate SO2 and MgO by the laggard high temperature calcining and decomposing of crossing of dehydration, finally, SO2 is after oxygenolysis It is reacted with system water and prepares industrial sulphuric acid, MgO continues on for desulfurization, MgSO after curing3Through the temperature for being dehydrated high-temperature calcination Condition is 500 DEG C -1000 DEG C, so that desulfurization product is fully used, the MgO of generation returns system utilization, high financial profit.
Obviously, various changes and modifications can be made to the invention without departing from essence of the invention by those skilled in the art Mind and range.In this way, if these modifications and changes of the present invention belongs to the range of the claims in the present invention and its equivalent technologies Within, then the present invention is also intended to include these modifications and variations.

Claims (5)

1. a kind of ceramic industry kiln desulfuration processing method, it is characterised in that: specifically includes the following steps:
S1, firstly, the sulfur-containing smoke gas inside Industrial Stoves enters inside deduster and is dusted after, then, via air-introduced machine into Enter the bulky grain flue dust after carrying out cooling in heat exchanger in flue gas to remove substantially, finally, the magnesia through curing generates hydroxide Flue dust temperature is reduced to 100 DEG C -150 DEG C, while Mg (OH) by the evaporation of heat exchanger with process water by magnesium2Liquid will be in flue gas Hydrogen halide remove substantially；
S2, firstly, flue gas is warming up in 170 DEG C or so input absorption towers after dedusting dehalogenation by flue gas heater by flue gas Portion, while Mg (OH)2Holding vessel supplements Mg (OH) into absorption tower in time by pump2Liquid, then, in flue gas and absorption tower After loop slurry comes into full contact with, finally, Mg (OH)2By the SO in flue gas2It is oxidized to MgSO3, the flue gas through desulfurization process removed It is discharged after mist processing from chimney；
S3, firstly, SO in flue gas2Through Mg (OH)2Oxidation generate MgSO3Liquid reactor tank after pipeline inputs, then, MgSO3SO is generated by the laggard high temperature calcining and decomposing of crossing of dehydration2And MgO, finally, SO2After oxygenolysis with system water Reaction prepares industrial sulphuric acid, and MgO continues on for desulfurization after curing.
2. a kind of ceramic industry kiln desulfuration processing method as described in claim 1, it is characterised in that: inhaled described in step 2 The internal structure for receiving tower is followed successively by exhaust gases passes, slurries area and desulfurization product channel under upper, and flue gas is through exhaust gases passes It need to meet into absorption tower with slurries area and inversely contact.
3. a kind of ceramic industry kiln desulfuration processing method as described in claim 1, it is characterised in that: root described in step 2 According to SO inside absorption tower2Oxidization condition constantly inputs freshly prepared Mg (OH) 2 into absorption tower, so that absorbing the pH value of slurries It is maintained at 7.6 or so.
4. a kind of ceramic industry kiln desulfuration processing method as described in claim 1, it is characterised in that: inhaled described in step 2 It receives tower and is equipped with 3-4 layers of spraying layer, every layer of spraying layer is equipped with a circulating pump, is atomized after desulfurization process through atomizer by flue gas Afterwards, the free water content in flue gas is less than or equal to 70mg/Nm3。
5. a kind of ceramic industry kiln desulfuration processing method as described in claim 1, it is characterised in that: described in step 3 MgSO3The temperature condition for being dehydrated high-temperature calcination is 500 DEG C -1000 DEG C.
CN201910516540.8A 2019-06-14 2019-06-14 A kind of ceramic industry kiln desulfuration processing method Withdrawn CN110201511A (en)

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CN201910516540.8A CN110201511A (en) 2019-06-14 2019-06-14 A kind of ceramic industry kiln desulfuration processing method

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Application publication date: 20190906