CN111921355A - Flue gas dust removal system and dust removal process for high borosilicate glass industrial melting furnace - Google Patents
Flue gas dust removal system and dust removal process for high borosilicate glass industrial melting furnace Download PDFInfo
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- CN111921355A CN111921355A CN202010883702.4A CN202010883702A CN111921355A CN 111921355 A CN111921355 A CN 111921355A CN 202010883702 A CN202010883702 A CN 202010883702A CN 111921355 A CN111921355 A CN 111921355A
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- flue gas
- denitration
- borosilicate glass
- dust removal
- tower
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 303
- 239000003546 flue gas Substances 0.000 title claims abstract description 301
- 239000000428 dust Substances 0.000 title claims abstract description 156
- 239000005388 borosilicate glass Substances 0.000 title claims abstract description 55
- 238000002844 melting Methods 0.000 title claims abstract description 50
- 230000008018 melting Effects 0.000 title claims abstract description 50
- 238000000034 method Methods 0.000 title claims abstract description 17
- 238000001816 cooling Methods 0.000 claims abstract description 65
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 claims abstract description 29
- 229910052796 boron Inorganic materials 0.000 claims abstract description 29
- 239000002253 acid Substances 0.000 claims abstract description 19
- 238000002347 injection Methods 0.000 claims abstract description 19
- 239000007924 injection Substances 0.000 claims abstract description 19
- 238000010502 deborylation reaction Methods 0.000 claims abstract description 17
- KGBXLFKZBHKPEV-UHFFFAOYSA-N boric acid Chemical compound OB(O)O KGBXLFKZBHKPEV-UHFFFAOYSA-N 0.000 claims description 49
- 239000004327 boric acid Substances 0.000 claims description 49
- 239000003638 chemical reducing agent Substances 0.000 claims description 42
- 239000000498 cooling water Substances 0.000 claims description 27
- 238000010438 heat treatment Methods 0.000 claims description 21
- 239000007787 solid Substances 0.000 claims description 21
- 239000000919 ceramic Substances 0.000 claims description 18
- 238000002485 combustion reaction Methods 0.000 claims description 15
- 239000007921 spray Substances 0.000 claims description 11
- 239000000376 reactant Substances 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 230000002378 acidificating effect Effects 0.000 claims description 7
- 239000007789 gas Substances 0.000 claims description 7
- 238000003860 storage Methods 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 7
- 239000002699 waste material Substances 0.000 claims description 7
- 230000003197 catalytic effect Effects 0.000 claims description 5
- 238000005507 spraying Methods 0.000 claims description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical group [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 4
- 238000005453 pelletization Methods 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 3
- 238000004891 communication Methods 0.000 claims 1
- 238000005260 corrosion Methods 0.000 abstract description 3
- 230000007797 corrosion Effects 0.000 abstract description 3
- 239000002245 particle Substances 0.000 description 22
- 239000003054 catalyst Substances 0.000 description 15
- 239000007788 liquid Substances 0.000 description 10
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 9
- 239000000835 fiber Substances 0.000 description 8
- 239000011521 glass Substances 0.000 description 8
- 239000000779 smoke Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000012528 membrane Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 230000003472 neutralizing effect Effects 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000006386 neutralization reaction Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 230000004308 accommodation Effects 0.000 description 2
- 125000005619 boric acid group Chemical group 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 235000011116 calcium hydroxide Nutrition 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 238000005137 deposition process Methods 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 230000001737 promoting effect Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 230000008094 contradictory effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 238000002834 transmittance Methods 0.000 description 1
Images
Classifications
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- 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
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/02—Particle separators, e.g. dust precipitators, having hollow filters made of flexible material
-
- 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
- B01D53/002—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 by condensation
-
- 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
- B01D53/14—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 by absorption
- B01D53/1456—Removing acid components
-
- 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
-
- 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
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
-
- 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
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
-
- 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 flue gas dust removal system and a dust removal process for a high borosilicate glass industrial melting furnace, wherein the flue gas dust removal system for the high borosilicate glass industrial melting furnace comprises a cooling tower, a flue gas inlet pipe and a flue gas outlet pipe, wherein the cooling tower is communicated with the flue gas inlet pipe; the cooling device is arranged on the cooling tower and used for cooling the flue gas entering the cooling tower to a first preset temperature; the deboronation deacidification tower is communicated with the cooling tower; the neutralizer injection device is communicated with the deboration deacidification tower and is used for injecting a neutralizer to the flue gas input to the deboration deacidification tower; the bag-type dust remover is communicated with the boron and acid removing tower and is used for removing dust from the flue gas output by the boron and acid removing tower; and the denitration unit is communicated with the boron and acid removing tower and is used for denitration of the flue gas output by the bag-type dust remover. The invention can realize the boron removal and deacidification operation of the flue gas, reduce the corrosion to the equipment when the flue gas further enters the denitration unit, and prolong the service life of the equipment.
Description
Technical Field
The invention relates to the field of dust removal systems, in particular to a high borosilicate glass industrial melting furnace flue gas dust removal system and a dust removal process.
Background
High borosilicate glass (hard glass) is made by melting glass by heating the glass inside by utilizing the conductive characteristic of the glass in a high-temperature state and processing the glass by an advanced production process. The glass is a special glass material with low expansion rate, high temperature resistance, high strength, high hardness, high light transmittance and high chemical stability, and is widely applied to the industries of solar energy, chemical engineering, medical packaging, electric light sources, craft ornaments and the like due to the excellent performance of the glass material. The flue gas of the high borosilicate glass melting furnace contains boric acid, hydrogen chloride and nitrogen oxide, the boric acid exists in a liquid state at the temperature of below 300 ℃ and above 169 ℃, and can corrode dust removal equipment, so that the service life of the dust removal equipment is influenced.
Disclosure of Invention
The invention mainly aims to provide a high borosilicate glass industrial melting furnace flue gas dust removal system and a dust removal process, and aims to solve the problem that boric acid in the existing high borosilicate glass industrial melting furnace flue gas dust removal system corrodes dust removal equipment.
In order to achieve the purpose, the flue gas dust removal system of the high borosilicate glass industrial melting furnace provided by the invention is used for removing dust from flue gas of the high borosilicate glass industrial melting furnace, and comprises:
the cooling tower is communicated with an inlet flue of the high borosilicate glass industrial melting furnace;
the cooling device is arranged on the cooling tower and used for cooling the flue gas entering the cooling tower to a first preset temperature;
the deboronation deacidification tower is communicated with the cooling tower;
the neutralizer injection device is communicated with the deboration deacidification tower and is used for injecting a neutralizer to the flue gas input to the deboration deacidification tower;
the bag-type dust remover is communicated with the boron and acid removing tower and is used for removing dust from the flue gas output by the boron and acid removing tower; and
and the denitration unit is communicated with the boron and acid removing tower and is used for denitration of the flue gas output by the bag-type dust remover.
Optionally, the denitration unit comprises:
the denitration dust removal device is communicated with the bag-type dust remover;
the flue gas heating and burning device is communicated with the denitration and dust removal device and is used for heating the flue gas conveyed to the denitration and dust removal device from the bag-type dust remover to a second preset temperature; and
and the reducing agent injection device is communicated with the denitration and dust removal device and is used for injecting the reducing agent to the flue gas heated to the second preset temperature by the flue gas heating combustion device.
Optionally, the denitration dust removal device is a catalytic ceramic filter tube denitration dust removal device.
Optionally, the flue gas dust removal system of the high borosilicate glass industrial melting furnace further comprises:
the flue gas heat exchange device is arranged between the denitration dust removal device and the bag-type dust remover, the flue gas heat exchange device is provided with a low-temperature pipeline and a high-temperature pipeline, flue gas output by the bag-type dust remover is input to the flue gas heat exchange device through the low-temperature pipeline, and purified gas output by the denitration dust removal device is conveyed to an outlet flue of the high borosilicate glass industrial melting furnace through the high-temperature pipeline.
Optionally, a denitration induced draft fan is arranged between an outlet flue of the high borosilicate glass industrial melting furnace and the high-temperature pipeline;
and/or a boron-removing and deacidifying draught fan is arranged between the bag-type dust collector and the flue gas heat exchange device.
Optionally, the flue gas dust removal system of the high borosilicate glass industrial melting furnace further comprises:
the bag-type dust collector and the denitration dust collector are respectively communicated with the waste bin through a bin pump.
Optionally, the denitration unit further comprises:
the reducing agent storage tank is connected with the reducing agent injection device through a reducing agent pump, and the reducing agent is ammonia water or liquid ammonia.
Optionally, the cooling device comprises:
a cooling water tank;
a cooling water pump; and
and the cooling water pump is respectively communicated with the cooling water tank and the cooling water spray gun and is used for pumping water in the cooling water tank into the cooling water spray gun.
The invention provides a flue gas dust removal process for a high borosilicate glass industrial melting furnace on the basis of the flue gas dust removal system for the high borosilicate glass industrial melting furnace, which comprises the following steps:
inputting the flue gas into a cooling tower;
cooling the flue gas input into the cooling tower until the temperature of the flue gas is reduced to a first preset temperature, so that part of boric acid in the flue gas is cooled to be in a solid state;
conveying the cooled flue gas to a deboronation deacidification tower, and spraying a neutralizer to the flue gas input to the deboronation deacidification tower so as to neutralize residual boric acid and other acidic substances in the flue gas;
conveying the flue gas subjected to boron removal and deacidification in the boron and acid removal tower to a bag-type dust remover to remove dust, solid boric acid and deacidification reactants in the flue gas;
heating the flue gas output by the bag-type dust collector through a flue gas heating combustion device to enable the flue gas to reach a second preset temperature;
spraying a reducing agent to the flue gas reaching the second preset temperature; and
and conveying the flue gas mixed with the reducing agent to a denitration dust removal device to form purified flue gas after denitration.
Optionally, the flue gas dust removal process for the high borosilicate glass industrial melting furnace further comprises the following steps:
conveying the flue gas output by the bag-type dust collector to a low-temperature pipeline in a flue gas heat exchange device, and conveying the purified flue gas output by the denitration dust removal device to a high-temperature pipeline in the flue gas heat exchange device so as to exchange heat between the high-temperature pipeline and the low-temperature pipeline; and
and outputting the purified flue gas output by the high-temperature pipeline to an outlet flue of the high borosilicate glass industrial melting furnace, and outputting the low-temperature flue gas output by the low-temperature pipeline to the flue gas temperature-rising combustion device.
According to the technical scheme, the cooling tower is adopted, so that most of boric acid in the flue gas is in a solid state after the flue gas is cooled to the first preset temperature, and the boric acid is further conveniently removed; mixing boric acid and a neutralizer by using a deboronation deacidification tower, and further neutralizing the residual boric acid and other acidic substances in the flue gas to generate a deacidification reactant; the bag-type dust collector is used for removing solid boric acid, deacidification reactants and neutralizer particles in the flue gas, so that the boron and deacidification operation of the flue gas is realized, and further when the flue gas further enters the denitration unit, the content of acidic substances in the flue gas is greatly reduced, so that the corrosion to subsequent equipment is reduced, the flue gas purification efficiency is improved, and the service life of the subsequent equipment is effectively prolonged.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the structures shown in the drawings without creative efforts.
FIG. 1 is a schematic structural view of an embodiment of a flue gas dust removal system of a high borosilicate glass industrial melting furnace according to the present invention;
FIG. 2 is a schematic flow chart of an embodiment of the flue gas dust removal process of the high borosilicate glass industrial melting furnace of the present invention;
FIG. 3 is a schematic structural view of an embodiment of the heat recycling of the flue gas dust removal process of the high borosilicate glass industrial melting furnace of the present invention.
The reference numbers illustrate:
| reference numerals | Name (R) | Reference numerals | Name (R) |
| 1 | |
2 | Cooling tower |
| 3 | Cooling water tank | 4 | Cooling water spray gun |
| 5 | Deboronizing deacidification tower | 6 | Neutralizer injection device |
| 7 | Bag- |
8 | Bin pump |
| 9 | |
10 | |
| 11 | Induced draft fan for removing boron and |
12 | Flue gas |
| 13 | Low |
14 | Low |
| 15 | Flue gas temperature-rising |
16 | Reducing |
| 17 | Reducing |
18 | |
| 19 | High |
20 | High |
| 21 | Denitration induced |
22 | |
| 23 | Chimney | 24 | Inlet |
| 25 | |
26 | |
| 27 | Reducing agent pump |
The implementation, functional features and advantages of the objects of the present invention will be further explained with reference to the accompanying drawings.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
It should be noted that, if directional indications (such as up, down, left, right, front, and back … …) are involved in the embodiment of the present invention, the directional indications are only used to explain the relative positional relationship between the components, the movement situation, and the like in a specific posture (as shown in the drawing), and if the specific posture is changed, the directional indications are changed accordingly.
In addition, if there is a description of "first", "second", etc. in an embodiment of the present invention, the description of "first", "second", etc. is for descriptive purposes only and is not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In addition, technical solutions between various embodiments may be combined with each other, but must be realized by a person skilled in the art, and when the technical solutions are contradictory or cannot be realized, such a combination should not be considered to exist, and is not within the protection scope of the present invention.
The high borosilicate glass melting furnace is provided with an inlet flue 1 for conveying flue gas to be dedusted to a dedusting system; the high borosilicate glass melting furnace has an outlet flue 22 for conveying purified flue gas produced by the dust removal system to a chimney 23. Wherein, an inlet gate plate 24 is arranged on the inlet flue 1 and used for opening or closing the inlet flue 1; an outlet shutter 25 is provided on the outlet stack 22 for opening or closing the outlet stack 22.
Referring to fig. 1, the present invention provides a flue gas dust removal system for a high borosilicate glass industrial melting furnace, which is used for removing dust from flue gas of the high borosilicate glass industrial melting furnace, and the flue gas dust removal system for the high borosilicate glass industrial melting furnace comprises:
and the cooling tower 2 is communicated with an inlet flue 1 of the high borosilicate glass industrial melting furnace. And the flue gas needing to be dedusted is conveyed to the cooling tower 2 through the inlet flue 1. The cooling tower 2 is used for providing a flue gas storage space so as to conveniently cool the flue gas and output the flue gas.
And the cooling device is arranged on the cooling tower 2 and used for cooling the flue gas entering the cooling tower 2 to a first preset temperature. The cooling device is used for cooling the flue gas in the cooling tower 2 so as to enable the flue gas to reach a first preset temperature. Since the boric acid is in a liquid state at a temperature below 300 ℃ and above 169 ℃, when the temperature of the flue gas is lower than 169 ℃, the boric acid in the flue gas is solidified to be in a solid state, in this embodiment, the first preset temperature is lower than 160 ℃, so that most of the boric acid in the flue gas can be in a solid granular state.
And the deboration deacidification tower 5 is communicated with the cooling tower 2. From the flue gas after the cooling tower 2 cools down contains and is solid-state boric acid to and the liquid boric acid of the remaining part, and solid-state boric acid and liquid boric acid enter into the deacidification tower 5 of taking off boron along with the flue gas, the deacidification tower 5 of taking off boron provides accommodation space for the flue gas to conveniently carry out further processing to the flue gas, and export the flue gas.
And the neutralizer injection device 6 is communicated with the deboration deacidification tower 5 and is used for injecting a neutralizer to the flue gas input to the deboration deacidification tower 5. The neutralizer injection device 6 is used for injecting a neutralizer, such as slaked lime and the like, so that the neutralizer and the liquid boric acid in the flue gas entering the boron and acid removing tower 5 are subjected to neutralization reaction to form a deacidification reactant.
And the bag-type dust collector 7 is communicated with the boron and acid removing tower 5 and is used for removing dust from the flue gas output by the boron and acid removing tower 5. The flue gas output from the deboronation and deacidification tower 5 comprises solid boric acid, deacidification reactants and partial neutralizer particles, the flue gas enters the bag-type dust remover 7, and particulate matters in the flue gas are removed through the bag-type dust remover 7 and are output.
And the denitration unit is communicated with the boron and acid removal tower 5 and is used for denitration of the flue gas output by the bag-type dust collector 7. Boric acid is basically removed from the flue gas output from the bag-type dust collector 7, and the flue gas is subjected to denitration treatment by the denitration unit to generate purified flue gas, and the purified flue gas is output from the outlet flue 22.
The denitration unit can adopt the existing denitration process equipment to realize denitration operation. As boric acid in the flue gas is removed, the corrosion of the flue gas entering the denitration unit to the denitration unit is greatly reduced, and the denitration unit can be kept in a preset using state. The flue gas output from the denitration unit to the outlet flue 22 is also relatively purified, so that the pollution caused by boric acid in the discharged flue gas is avoided.
Most of boric acid in the flue gas is formed into solid boric acid after being cooled by the cooling tower 2, and most of boric acid can be removed when entering the bag-type dust collector 7; remaining boric acid and other acidic material can be got rid of by the neutralization under the effect of neutralizer, further reduce the boric acid content in the flue gas, can effectively promote deacidification efficiency, reduce boric acid and remain, owing to at first carry out after the deacidification operation, jam and the poisoning problem that exist when follow-up denitration unit carries out denitration operation can be avoided, and then help guaranteeing the denitration efficiency of system, satisfy emission standard.
Optionally, in this embodiment, a boron-removing and deacidifying induced draft fan 11 is disposed between the bag-type dust collector 7 and the denitration unit, so as to pump the flue gas to the denitration unit. Because the entering the deboronation deacidification tower 5 with in the flue gas of sack cleaner 7, all contain solid particulate matter, the draught fan 11 that deacidifies and can promote flue gas flow efficiency, prevents sack cleaner 7 or the blocking appears in the deboronation deacidification tower 5.
Because solid particles can be collected in the bag-type dust collector 7, a waste bin 9 can be arranged in the embodiment, the bag-type dust collector 7 is communicated with the waste bin 9 through a bin pump 8 so as to collect solid boric acid, deacidification reaction products and partial neutralizer particles, and the waste bin 9 is connected with a bulk machine 10 so as to facilitate centralized treatment.
The cooling mode of the cooling tower 2 can adopt water cooling or other cooling modes. Optionally in this embodiment, the cooling device includes: a cooling water tank 3; a cooling water pump 26; and the cooling water spray gun 4, the cooling water pump 26 is respectively communicated with the cooling water tank 3 and the cooling water spray gun 4 and is used for pumping the water in the cooling water tank 3 into the cooling water spray gun 4. The cooling water spray gun 4 sprays cold water into the cooling tower 2 to cool the flue gas, so that the flue gas reaches a first preset temperature range. Through adopting the mode of cooling water spray gun 4 jet cooling can make flue gas rapid cooling, and, adopt the mode of water-cooling, when water carries out the heat exchange with the flue gas, can fully act on the flue gas, water and the mutual heat exchange in-process of flue gas, cold water can carry out the heat exchange with the flue gas fully, so that the flue gas can fully cool down, and can not cause the flue gas random flow, and then can prevent that the mode that adopts the gas heat transfer from causing the flue gas to appear the turbulent flow and the insufficient problem of heat exchange that leads to, be favorable to promoting the efficiency of heat transfer, make the overwhelming majority flue gas in the flue gas can cool down and form solid particles. When the flue gas further enters the deboronation deacidification tower 5, the using amount of a neutralizing agent can be reduced, and the deacidification efficiency is improved. Through the mode that adopts water-cooling, can reduce right cooling tower 2 carries out too much air flue diversion's demand, reduction equipment cost to cooling efficiency is controllable, helps promoting the controllability of equipment deacidification efficiency.
In one embodiment of the present invention, the denitration unit includes: the denitration dust removal device 18 is communicated with the bag-type dust remover 7; the flue gas heating and burning device 15 is communicated with the denitration and dust removal device 18 and is used for heating the flue gas conveyed to the denitration and dust removal device 18 from the bag-type dust remover 7 to a second preset temperature; and the reducing agent injection device 17 is communicated with the denitration and dust removal device 18 and is used for injecting the reducing agent to the flue gas heated to the second preset temperature by the flue gas heating combustion device 15.
The denitration dust removal device 18 is communicated with the bag-type dust remover 7 through a pipeline, and when the boron-removal deacidification induced draft fan 11 is arranged, the boron-removal deacidification induced draft fan 11 pumps smoke from the bag-type dust remover 7 to the denitration dust removal device 18. Before the flue gas enters the denitration dust removal device 18, the flue gas heating combustion device 15 heats the flue gas to enable the flue gas to reach a second preset temperature, the second preset temperature is not lower than 320 ℃, after the flue gas is heated, the reducing agent injection device 17 injects a reducing agent into the flue gas to enable the reducing agent and the flue gas to be fully mixed and then enter the denitration dust removal device 18, and the denitration dust removal device 18 conducts denitration treatment on the flue gas to form purified gas reaching the emission standard.
Because the boric acid in the flue gas is treated, when the denitration dust removal device 18 carries out denitration operation on the flue gas, the liquid boric acid can be prevented from corroding the denitration dust removal device 18.
In this embodiment, the denitration dust-removing device 18 is a catalytic ceramic filter tube denitration dust-removing device 18. The catalyst ceramic filter tube consists of a high-strength ceramic manufacturing body and a high-efficiency membrane separation layer, and catalyst components are added outside the high-efficiency membrane separation layer, so that the catalyst ceramic filter tube can filter particles and simultaneously achieve the effect of removing nitrogen oxides.
By adopting the denitration dust removal device with the catalyst ceramic fiber filter tube, the particle size of catalyst particles is nano-scale, the surface area of the filter tube is large, the active surface area and the reaction rate of the denitration catalyst can be increased, meanwhile, the retention time of flue gas is also increased, and the removal efficiency is increased. A small amount of acid, neutralizer and dust remain in the deacidified flue gas, the residual neutralizer particle dust in the flue gas forms a neutralizer particle layer cake in the dust deposition process of the ceramic fiber filter tube, the deacidification reaction is increased for the neutralizer particle layer cake, the flue gas is further deacidified, and the deacidification efficiency can be improved by 5-15%. Because the cooling tower 2 can make boric acid form solid particles, the deboronation deacidification tower 5 can carry out secondary deacidification to the remaining boric acid in the flue gas, and the flue gas passes through catalyst ceramic fiber filter tube denitration dust collector can further carry out the deacidification to make the flue gas reach preset emission standard. Because the denitration and dust removal device of the catalytic ceramic fiber filter tube can resist high temperature, the concentration of smoke dust after the smoke is treated by the dust remover can be lower than 10mg/Nm3 (dry basis, standard state and reference melting amount), and the ultralow emission is achieved.
In order to collect the particles conveniently, the denitration dust collector 18 is communicated with the waste bin 9 through a bin pump 8 to collect solid particles generated by denitration.
The purified flue gas generated by the denitration dust-removing device 18 is conveyed to the outlet flue 22, and a denitration induced draft fan 21 can be arranged between the denitration dust-removing device 18 and the outlet flue 22 in order to convey the flue gas to the outlet flue 22.
In this embodiment, optionally, the reducing agent may adopt ammonia water or liquid ammonia, and the reducing agent injection device 17 is adopted to inject the reducing agent into the flue gas, so that the flue gas can be sufficiently mixed with the reducing agent. Further optionally, the denitration unit further includes: the reducing agent storage tank 16 is connected with the reducing agent injection device 17 through a reducing agent pump 27, and the reducing agent pump 27 pumps the reducing agent in the reducing agent storage tank 16 into the reducing agent injection device 17 so as to realize continuous injection of the reducing agent.
Because the flue gas through after 15 burning heating of flue gas intensification burner, the temperature of flue gas is higher, in order to promote thermal utilization efficiency, optionally in this embodiment, borosilicate glass industry melting furnace flue gas dust pelletizing system still includes: the flue gas heat exchange device 12 is arranged between the denitration dust removal device 18 and the bag-type dust remover 7, the flue gas heat exchange device 12 is provided with a low-temperature pipeline and a high-temperature pipeline, flue gas output by the bag-type dust remover 7 is input to the flue gas heat exchange device 12 through the low-temperature pipeline, and purified gas output by the denitration dust removal device 18 is conveyed to an outlet flue 22 of the high borosilicate glass industrial melting furnace through the high-temperature pipeline.
The high-temperature purified flue gas output from the denitration dust removal device 18 enters the high-temperature pipeline from a high-temperature section inlet 19 of the flue gas heat exchange device 12, is used as a heat source of the flue gas heat exchange device 12, and is output to the outlet flue 22 through a high-temperature section outlet 20 of the flue gas heat exchange device 12; the flue gas from the bag-type dust collector 7 enters the low-temperature pipeline from a low-temperature section inlet 13 of the flue gas heat exchange device 12, is output through the low-temperature pipeline, and is conveyed to the flue gas temperature-rising combustion device 15 from a low-temperature section outlet 14 of the flue gas heat exchange device 12.
Among the flue gas heat transfer device 12, the purification flue gas in the high temperature pipeline with flue gas among the low temperature pipeline carries out the heat exchange to make the temperature of flue gas be higher than first preset temperature, through arranging the high temperature pipeline with the low temperature pipeline can make the flue gas be in heat up to about 240 ℃ among the flue gas heat transfer device 12, carry again to during flue gas intensification burner 15, the required heat of flue gas intensification can reduce relatively, helps reducing entire system's energy consumption. The heat replacement is carried out by using the purified flue gas after denitration and the flue gas before denitration, so that the natural gas consumption of the rear-end flue gas heating combustion device 15 is reduced, the energy is effectively saved, and the operation cost is reduced.
When the induced draft fan 11 for boron removal and deacidification is arranged, the induced draft fan 11 for boron removal and deacidification is arranged on a pipeline between the bag-type dust collector 7 and the flue gas heat exchange device 12; when being provided with denitration draught fan 21, denitration draught fan 21 sets up high temperature pipeline with between the export flue 22.
The invention also provides an embodiment of the flue gas dust removal process of the high borosilicate glass industrial melting furnace.
Referring to fig. 2, the flue gas dust removal process for the high borosilicate glass industrial melting furnace comprises the following steps:
s100: the flue gas is input into the cooling tower 2.
And the cooling tower 2 is communicated with an inlet flue 1 of the high borosilicate glass industrial melting furnace. And the flue gas needing to be dedusted is conveyed to the cooling tower 2 through the inlet flue 1. The cooling tower 2 is used for providing a flue gas storage space so as to conveniently cool the flue gas and output the flue gas.
S200: and cooling the flue gas input into the cooling tower 2 until the temperature of the flue gas is reduced to a first preset temperature, so that part of boric acid in the flue gas is cooled to be solid.
Adopt cooling device to cool off the flue gas that gets into cooling tower 2 to make the flue gas reach first preset temperature range, boric acid is below 300 ℃, is the liquid when 169 ℃ above, and when the temperature of flue gas was less than 169 ℃, the boric acid solidification in the flue gas was solid-state, first preset temperature is less than 160 degrees centigrade, so that the vast majority boric acid in the flue gas is solid particulate state.
S300: and conveying the cooled flue gas to a deboronation and deacidification tower 5, and spraying a neutralizing agent to the flue gas input to the deboronation and deacidification tower 5 so as to neutralize the residual boric acid and other acidic substances in the flue gas by using the neutralizing agent.
From the flue gas after the cooling tower 2 cools down contains and is solid-state boric acid to and the liquid boric acid of the remaining part, and solid-state boric acid and liquid boric acid enter into the deacidification tower 5 of taking off boron along with the flue gas, the deacidification tower 5 of taking off boron provides accommodation space for the flue gas to conveniently carry out further processing to the flue gas, and export the flue gas. The neutralizer injection device 6 is used for injecting a neutralizer, such as slaked lime and the like, so that the neutralizer and the liquid boric acid and other acidic substances in the flue gas entering the boron and acid removing tower 5 are subjected to neutralization reaction to form a deacidification reactant.
S400: the flue gas which is subjected to boron removal and deacidification in the boron and acid removal tower 5 is conveyed to a bag-type dust remover 7 to remove dust, solid boric acid and deacidification reactants in the flue gas.
The flue gas output from the deboronation and deacidification tower 5 comprises solid boric acid, deacidification reactants and partial neutralizer particles, the flue gas enters the bag-type dust remover 7, and particulate matters in the flue gas are removed through the bag-type dust remover 7 and are output.
S500: and heating the flue gas output by the bag-type dust collector 7 through a flue gas heating combustion device 15 so as to enable the flue gas to reach a second preset temperature.
Before the flue gas enters the denitration dust removal device 18, the flue gas is heated by a flue gas heating combustion device 15 so as to reach a second preset temperature, wherein the second preset temperature is not lower than 320 ℃.
S600: and injecting a reducing agent to the flue gas reaching the second preset temperature.
After the flue gas is heated, the reducing agent injection device 17 injects a reducing agent into the flue gas, so that the reducing agent and the flue gas are fully mixed and then enter the denitration dust removal device 18, and the reducing agent can adopt liquid ammonia or ammonia water.
S700: the flue gas mixed with the reducing agent is conveyed to a denitration dust removal device 18 to form purified flue gas after denitration.
The denitration dust removal device 18 carries out denitration treatment on the flue gas to form purified gas meeting the emission standard.
The denitration dust-removing device 18 is a catalyst ceramic filter tube denitration dust-removing device 18. The catalyst ceramic filter tube consists of a high-strength ceramic manufacturing body and a high-efficiency membrane separation layer, and catalyst components are added outside the high-efficiency membrane separation layer, so that the catalyst ceramic filter tube can filter particles and simultaneously achieve the effect of removing nitrogen oxides.
By adopting the denitration dust removal device with the catalyst ceramic fiber filter tube, the particle size of catalyst particles is nano-scale, the surface area of the filter tube is large, the active surface area and the reaction rate of the denitration catalyst can be increased, meanwhile, the retention time of flue gas is also increased, and the removal efficiency is increased. A small amount of acid, neutralizer and dust remain in the deacidified flue gas, the residual neutralizer particle dust in the flue gas forms a neutralizer particle layer cake in the dust deposition process of the ceramic fiber filter tube, the deacidification reaction is increased for the neutralizer particle layer cake, the flue gas is further deacidified, and the deacidification efficiency can be improved by 5-15%. Because the cooling tower 2 can make boric acid form solid particles, the deboronation deacidification tower 5 can carry out secondary deacidification to the remaining boric acid in the flue gas, and the flue gas passes through catalyst ceramic fiber filter tube denitration dust collector can further carry out the deacidification to make the flue gas reach preset emission standard. Because the denitration and dust removal device of the catalytic ceramic fiber filter tube can resist high temperature, the concentration of smoke dust after the smoke is treated by the dust remover can be lower than 10mg/Nm3 (dry basis, standard state and reference melting amount), and the ultralow emission is achieved.
Referring to fig. 3, in order to reduce the system energy consumption and realize the heat recycling, in this embodiment, the flue gas dust removal process of the high borosilicate glass industrial melting furnace further includes:
s710: and the flue gas output from the bag-type dust collector 7 is conveyed to a low-temperature pipeline in the flue gas heat exchange device 12, and the purified flue gas output from the denitration dust collector 18 is conveyed to a high-temperature pipeline in the flue gas heat exchange device 12, so that the high-temperature pipeline and the low-temperature pipeline exchange heat.
The high-temperature purified flue gas output from the denitration dust removal device 18 enters the high-temperature pipeline from a high-temperature section inlet 19 of the flue gas heat exchange device 12, is used as a heat source of the flue gas heat exchange device 12, and is output to the outlet flue 22 through a high-temperature section outlet 20 of the flue gas heat exchange device 12; the flue gas output from the bag-type dust collector 7 enters the low-temperature pipeline from a low-temperature section inlet 13 of the flue gas heat exchange device 12 and is output through the low-temperature pipeline, so that the high-temperature purified gas of the high-temperature pipeline and the flue gas to be denitrated of the low-temperature pipeline are subjected to heat exchange.
S720: and outputting the purified flue gas output by the high-temperature pipeline to an outlet flue 22 of the high borosilicate glass industrial melting furnace, and outputting the low-temperature flue gas output by the low-temperature pipeline to the flue gas temperature-rising combustion device 15.
Among the flue gas heat transfer device 12, the purification flue gas in the high temperature pipeline with flue gas among the low temperature pipeline carries out the heat exchange to make the temperature of flue gas be higher than first preset temperature, through arranging the high temperature pipeline with the low temperature pipeline can make the flue gas be in heat up to about 240 ℃ among the flue gas heat transfer device 12, carry again to during flue gas intensification burner 15, the required heat of flue gas intensification can reduce relatively, helps reducing entire system's energy consumption. The heat replacement is carried out by using the purified flue gas after denitration and the flue gas before denitration, so that the natural gas consumption of the rear-end flue gas heating combustion device 15 is reduced, the energy is effectively saved, and the operation cost is reduced.
The above description is only an alternative embodiment of the present invention, and not intended to limit the scope of the present invention, and all modifications and equivalents of the present invention, which are made by the contents of the present specification and the accompanying drawings, or directly/indirectly applied to other related technical fields, are included in the scope of the present invention.
Claims (10)
1. The utility model provides a borosilicate glass industry melting furnace flue gas dust pelletizing system for borosilicate glass industry melting furnace flue gas dust removal, a serial communication port, borosilicate glass industry melting furnace flue gas dust pelletizing system includes:
the cooling tower is communicated with an inlet flue of the high borosilicate glass industrial melting furnace;
the cooling device is arranged on the cooling tower and used for cooling the flue gas entering the cooling tower to a first preset temperature;
the deboronation deacidification tower is communicated with the cooling tower;
the neutralizer injection device is communicated with the deboration deacidification tower and is used for injecting a neutralizer to the flue gas input to the deboration deacidification tower;
the bag-type dust remover is communicated with the boron and acid removing tower and is used for removing dust from the flue gas output by the boron and acid removing tower; and
and the denitration unit is communicated with the boron and acid removing tower and is used for denitration of the flue gas output by the bag-type dust remover.
2. The flue gas dedusting system of the high borosilicate glass industrial melting furnace of claim 1, wherein the denitration unit comprises:
the denitration dust removal device is communicated with the bag-type dust remover;
the flue gas heating and burning device is communicated with the denitration and dust removal device and is used for heating the flue gas conveyed to the denitration and dust removal device from the bag-type dust remover to a second preset temperature; and
and the reducing agent injection device is communicated with the denitration and dust removal device and is used for injecting the reducing agent to the flue gas heated to the second preset temperature by the flue gas heating combustion device.
3. The flue gas dedusting system of the high borosilicate glass industrial melting furnace of claim 2, wherein the denitration dedusting device is a catalytic ceramic filter tube denitration dedusting device.
4. The high borosilicate glass industrial furnace flue gas dust removal system of claim 2, wherein said high borosilicate glass industrial furnace flue gas dust removal system further comprises:
the flue gas heat exchange device is arranged between the denitration dust removal device and the bag-type dust remover, the flue gas heat exchange device is provided with a low-temperature pipeline and a high-temperature pipeline, flue gas output by the bag-type dust remover is input to the flue gas heat exchange device through the low-temperature pipeline, and purified gas output by the denitration dust removal device is conveyed to an outlet flue of the high borosilicate glass industrial melting furnace through the high-temperature pipeline.
5. The flue gas dedusting system of the high borosilicate glass industrial melting furnace of claim 4, wherein a denitration induced draft fan is arranged between the outlet flue of the high borosilicate glass industrial melting furnace and the high temperature pipeline;
and/or a boron-removing and deacidifying draught fan is arranged between the bag-type dust collector and the flue gas heat exchange device.
6. The high borosilicate glass industrial furnace flue gas dust removal system of claim 2, wherein said high borosilicate glass industrial furnace flue gas dust removal system further comprises:
the bag-type dust collector and the denitration dust collector are respectively communicated with the waste bin through a bin pump.
7. The flue gas dedusting system for a high borosilicate glass industrial melting furnace according to claim 2, wherein the denitration unit further comprises:
the reducing agent storage tank is connected with the reducing agent injection device through a reducing agent pump, and the reducing agent is ammonia water or liquid ammonia.
8. The high borosilicate glass industrial furnace flue gas dedusting system of any of the claims 1 to 7, wherein the cooling device comprises:
a cooling water tank;
a cooling water pump; and
and the cooling water pump is respectively communicated with the cooling water tank and the cooling water spray gun and is used for pumping water in the cooling water tank into the cooling water spray gun.
9. A flue gas dust removal process for a high borosilicate glass industrial melting furnace is characterized by comprising the following steps:
inputting the flue gas into a cooling tower;
cooling the flue gas input into the cooling tower until the temperature of the flue gas is reduced to a first preset temperature, so that part of boric acid in the flue gas is cooled to be in a solid state;
conveying the cooled flue gas to a deboronation deacidification tower, and spraying a neutralizer to the flue gas input to the deboronation deacidification tower so as to neutralize residual boric acid and other acidic substances in the flue gas;
conveying the flue gas subjected to boron removal and deacidification in the boron and acid removal tower to a bag-type dust remover to remove dust, solid boric acid and deacidification reactants in the flue gas;
heating the flue gas output by the bag-type dust collector through a flue gas heating combustion device to enable the flue gas to reach a second preset temperature;
spraying a reducing agent to the flue gas reaching the second preset temperature; and
and conveying the flue gas mixed with the reducing agent to a denitration dust removal device to form purified flue gas after denitration.
10. The high borosilicate glass industrial furnace flue gas dedusting process according to claim 9, wherein the high borosilicate glass industrial furnace flue gas dedusting process further comprises:
conveying the flue gas output by the bag-type dust collector to a low-temperature pipeline in a flue gas heat exchange device, and conveying the purified flue gas output by the denitration dust removal device to a high-temperature pipeline in the flue gas heat exchange device so as to exchange heat between the high-temperature pipeline and the low-temperature pipeline; and
and outputting the purified flue gas output by the high-temperature pipeline to an outlet flue of the high borosilicate glass industrial melting furnace, and outputting the low-temperature flue gas output by the low-temperature pipeline to the flue gas temperature-rising combustion device.
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