CN212142129U - Sintering desulfurization and denitrification system - Google Patents
Sintering desulfurization and denitrification system Download PDFInfo
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- CN212142129U CN212142129U CN202020289283.7U CN202020289283U CN212142129U CN 212142129 U CN212142129 U CN 212142129U CN 202020289283 U CN202020289283 U CN 202020289283U CN 212142129 U CN212142129 U CN 212142129U
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- heat exchanger
- desulfurization
- flue gas
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 36
- 230000023556 desulfurization Effects 0.000 title claims abstract description 36
- 238000005245 sintering Methods 0.000 title claims abstract description 15
- 239000000428 dust Substances 0.000 claims abstract description 42
- 239000003546 flue gas Substances 0.000 claims abstract description 38
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000007789 gas Substances 0.000 claims description 22
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 16
- 238000010521 absorption reaction Methods 0.000 claims description 15
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 14
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 239000000706 filtrate Substances 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 8
- 239000002002 slurry Substances 0.000 claims description 8
- 229910021529 ammonia Inorganic materials 0.000 claims description 7
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 5
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 5
- 239000004571 lime Substances 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 5
- 230000000630 rising effect Effects 0.000 claims description 5
- 230000002457 bidirectional effect Effects 0.000 claims description 4
- 239000012716 precipitator Substances 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 14
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000001816 cooling Methods 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 abstract description 3
- 238000006243 chemical reaction Methods 0.000 description 8
- 239000000779 smoke Substances 0.000 description 8
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulfur dioxide Inorganic materials O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 7
- 229910052815 sulfur oxide Inorganic materials 0.000 description 5
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 3
- 239000012065 filter cake Substances 0.000 description 3
- 238000006722 reduction reaction Methods 0.000 description 3
- 238000010531 catalytic reduction reaction Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 235000019738 Limestone Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000009851 ferrous metallurgy Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model discloses a sintering SOx/NOx control system mainly solves the problem that current flue gas SOx/NOx control system working costs is high, area is big, the energy consumption is high. The desulfurization and denitrification system comprises a primary dust removal unit, an external circulation heat exchange unit connected with the primary dust removal unit, a desulfurization unit and a denitrification unit connected with the external circulation heat exchange unit, and a secondary dust removal unit connected with the denitrification unit. Through the design, the utility model discloses combine the SOx/NOx control technology of flue gas, reduced the running cost of system, also reduced area simultaneously to utilize the step of intensification denitration through the desulfurated heat of extrinsic cycle heat transfer unit will cooling down, effectively utilize the heat, reduced the energy consumption, also carried out reuse to the heat of the flue gas after the denitration simultaneously, practiced thrift the energy. Therefore, the method is suitable for popularization and application.
Description
Technical Field
The utility model belongs to the technical field of the gas cleaning technique and specifically relates to a sintering SOx/NOx control system is related to.
Background
The sintering flue gas of ferrous metallurgy has complex components and contains SO2And NOxAnd the like. And the sintering flue gas volume is large, and SO in the flue gas2And NOxThe concentration is higher.
At present, a commonly used method for desulfurization and denitrification of flue gas is step-by-step desulfurization and denitrification, namely, two sets of equipment are respectively used for desulfurization and denitrification and are carried out step by step. Common processes of the method comprise SCR denitration and limestone/lime/gypsum wet desulphurization, SNCR/SCR combined denitration and ammonia desulphurization and the like. As is well known, the step-by-step method has high investment and operation cost and large occupied area. In addition, in a desulfurization and denitrification system, the reaction temperature of flue gas is inconsistent, the desulfurization is slowly cooled, and the denitrated catalyst loses activity at low temperature, so that the temperature needs to be raised, the flue gas can be better purified only by the process of desulfurization firstly and denitrification, the heat dissipated in the desulfurization cannot be effectively utilized in the prior art, the energy waste is caused, the energy consumption is increased, and the flue gas purification cost is increased.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a sintering SOx/NOx control system mainly solves the problem that current flue gas SOx/NOx control system working costs is high, area is big, the energy consumption is high.
In order to achieve the above object, the utility model adopts the following technical scheme:
a sintering desulfurization and denitrification system comprises a primary dust removal unit, an external circulation heat exchange unit connected with the primary dust removal unit, a desulfurization unit and a denitrification unit connected with the external circulation heat exchange unit, and a secondary dust removal unit connected with the denitrification unit; the denitration unit comprises an internal circulation flue gas heat exchanger with an air inlet end connected with the external circulation heat exchange unit and an air outlet end connected with the secondary dust removal unit, a heating furnace connected with the internal circulation flue gas heat exchanger, an SCR (selective catalytic reduction) reactor connected with the heating furnace, and an ammonia adding unit connected with the SCR reactor; and the air outlet end of the SCR reactor is connected with an internal circulation flue gas heat exchanger.
Furthermore, the external circulation heat exchange unit comprises a heat reduction heat exchanger connected with the primary dust removal unit and a heat rising heat exchanger connected with the primary dust removal unit through a bidirectional water circulation pipeline; the air outlet end of the heat-reducing heat exchanger is connected with the desulfurization unit, the air inlet end of the heat-raising heat exchanger is connected with the air outlet end of the desulfurization unit, and the air outlet end of the heat-raising heat exchanger is connected with the air inlet end of the internal circulation flue gas heat exchanger.
Further, the desulfurization unit comprises an absorption tower connected with the gas outlet end of the heat-reducing heat exchanger, a slurry tank communicated with the absorption tower and used for adding lime slurry, a filtrate tank connected with the liquid outlet of the absorption tower, a plate-and-frame filter press matched with the filtrate tank, and a flue gas condenser communicated with the gas outlet of the absorption tower; and the gas outlet end of the flue gas condenser is connected with the gas inlet end of the heat rising heat exchanger.
Further, the ammonia adding unit comprises an ammonia water storage tank and an ammonia water evaporator connected with the ammonia water storage tank; and the gas outlet end of the ammonia water evaporator is connected with the SCR reactor.
Preferably, the primary dust removal unit adopts an electric dust remover.
Preferably, the secondary dust removal unit adopts a bag-type dust remover.
Compared with the prior art, the utility model discloses following beneficial effect has:
(1) the utility model discloses a combine the SOx/NOx control technology of flue gas, reduced the running cost of system, also reduced area simultaneously to utilize the step of intensification denitration through the desulfurated heat of extrinsic cycle heat transfer unit will cooling down, effectively utilize the heat, reduced the energy consumption, also carried out reuse to the heat of the flue gas after the denitration simultaneously, practiced thrift the energy.
(2) The utility model discloses a set up filtrating pond and plate and frame filter press, make and absorb SO through the absorption tower2The calcium sulfate formed later is separated more thoroughly, so that the solid content of the filter cake is higher, the filtrate is clearer, and secondary pollution is avoided.
Drawings
Fig. 1 is a system block diagram of the present invention.
Wherein, the names corresponding to the reference numbers are:
1-a primary dust removal unit, 2-a secondary dust removal unit, 3-an internal circulation flue gas heat exchanger, 4-a heating furnace, 5-an SCR reactor, 6-a heat-reducing heat exchanger, 7-a bidirectional water circulation pipeline, 8-a heat-raising heat exchanger, 9-an absorption tower, 10-a slurry tank, 11-a filtrate tank, 12-a plate-and-frame filter press, 13-a flue gas condenser, 14-an ammonia water storage tank and 15-an ammonia water evaporator.
Detailed Description
The present invention will be further described with reference to the following description and examples, which include but are not limited to the following examples.
Examples
As shown in fig. 1, the utility model discloses a sintering desulfurization and denitrification system, which comprises a primary dust removal unit 1, an external circulation heat exchange unit connected with the primary dust removal unit 1, a desulfurization unit and a denitrification unit connected with the external circulation heat exchange unit, and a secondary dust removal unit 2 connected with the denitrification unit; the denitration unit comprises an internal circulation flue gas heat exchanger 3, a heating furnace 4, an SCR reactor 5 and an ammonia adding unit, wherein the gas inlet end of the internal circulation flue gas heat exchanger 3 is connected with the external circulation heat exchange unit, and the gas outlet end of the internal circulation flue gas heat exchanger 3 is connected with the secondary dust removal unit 2; and the air outlet end of the SCR reactor 5 is connected with the internal circulation flue gas heat exchanger 3. The ammonia adding unit comprises an ammonia water storage tank 14 and an ammonia water evaporator 15 connected with the ammonia water storage tank; wherein, the air outlet end of the ammonia water evaporator 15 is connected with the SCR reactor 5. The ammonia gas generated after evaporation and the smoke gas passing through the heating furnace enter the SCR reactor 5 together, and a medium-high temperature honeycomb catalyst is added into the SCR reactor to promote the chemical reaction denitration in the reaction furnace. In the present embodiment, the primary dust removal unit 1 employs an electric dust remover. The secondary dust removal unit 2 adopts a bag-type dust remover.
In the embodiment, the external circulation heat exchange unit comprises a heat reduction heat exchanger 6 connected with the primary dust removal unit 1 and a heat rising heat exchanger 8 connected with the primary dust removal unit through a bidirectional water circulation pipeline 7; the air outlet end of the heat-reducing heat exchanger 6 is connected with the desulfurization unit, the air inlet end of the heat-raising heat exchanger 8 is connected with the air outlet end of the desulfurization unit, and the air outlet end of the heat-raising heat exchanger 8 is connected with the air inlet end of the internal circulation flue gas heat exchanger 3. The heat exchange medium of the heat-reducing heat exchanger 6 and the heat-raising heat exchanger 8 is water. During desulfurization, smoke dust which is just coming out of the boiler and has a large amount of heat is introduced into the heat-reducing heat exchanger 6 to exchange heat, then water with heat enters the heat-raising heat exchanger 8 through a water circulation pipeline, desulfurized lower-temperature gas enters the heat-raising heat exchanger 8, water with heat in the heat-raising heat exchanger 8 is exchanged into smoke dust gas, then the smoke dust gas enters a high-temperature denitration process, the water after heat exchange enters the heat-reducing heat exchanger 6 through a water circulation pipeline, and the circulation is carried out so as to achieve waste heat utilization. In the actual process, the cold water circulating pipeline can be set to be spiral to increase the backflow time, so that the water cooling amplitude is large, and more heat can be better taken away in the heat exchanger.
In this embodiment, the desulfurization process employs a chemical reaction in which calcium hydroxide absorbs sulfur dioxide to perform desulfurization. The desulfurization unit comprises an absorption tower 9 connected with the air outlet end of the heat-reducing heat exchanger 6, a slurry tank 10 communicated with the absorption tower 9 and used for adding lime slurry, a filtrate pool 11 connected with the liquid outlet of the absorption tower 9, a plate-and-frame filter press 12 matched with the filtrate pool 11, and a flue gas condenser 13 communicated with the air outlet of the absorption tower 9; wherein, the gas outlet end of the flue gas condenser 13 is connected with the gas inlet end of the heat rising heat exchanger 8. The flue gas condenser is used for taking away moisture in flue gas in the desulfurization process. Filtering liquid pool and plate-and-frame filter press for absorbing SO by absorption tower2The calcium sulfate formed later is separated more thoroughly, so that the solid content of the filter cake is higher, the filtrate is clearer, and secondary pollution is avoided.
The working principle of the utility model is as follows;
the method comprises the following steps that smoke dust with large heat energy from boiler reaction is subjected to preliminary dust removal through an electric dust remover and then enters a heat-reducing heat exchanger for heat exchange and temperature reduction, the smoke dust is subjected to low-temperature desulfurization, sulfur dioxide is absorbed by adding lime slurry into a reaction tower, on one hand, desulfurized gas enters a heat-raising heat exchanger for temperature rise through a smoke dust condenser and then is sent into a denitration process, ammonia gas generated after evaporation and smoke dust gas passing through a heating furnace enter an SCR (selective catalytic reduction) reactor together, medium-high temperature honeycomb type catalysts are added into the SCR reactor to promote chemical reaction denitration in the reaction furnace, and the denitrated gas is subjected to secondary dust removal through a bag type dust remover after heat exchange through an internal circulation heat exchanger and then is discharged. And on the other hand, the turbid liquid generated after the sulfur dioxide is absorbed is precipitated and separated, and a filter cake is pressed by a plate-and-frame filter press.
Through the design, the utility model discloses combine the SOx/NOx control technology of flue gas, reduced the running cost of system, also reduced area simultaneously to utilize the step of intensification denitration through the desulfurated heat of extrinsic cycle heat transfer unit will cooling down, effectively utilize the heat, reduced the energy consumption, also carried out reuse to the heat of the flue gas after the denitration simultaneously, practiced thrift the energy. Therefore, the method has high use value and popularization value.
The above embodiment is only one of the preferred embodiments of the present invention, and should not be used to limit the protection scope of the present invention, but all the insubstantial changes or modifications made in the spirit and the idea of the main design of the present invention, the technical problems solved by the embodiment are still consistent with the present invention, and all should be included in the protection scope of the present invention.
Claims (6)
1. A sintering desulfurization and denitrification system is characterized by comprising a primary dust removal unit (1), an external circulation heat exchange unit connected with the primary dust removal unit (1), a desulfurization unit and a denitrification unit connected with the external circulation heat exchange unit, and a secondary dust removal unit (2) connected with the denitrification unit; the denitration unit comprises an internal circulation flue gas heat exchanger (3) with a gas inlet end connected with the external circulation heat exchange unit and a gas outlet end connected with the secondary dust removal unit (2), a heating furnace (4) connected with the internal circulation flue gas heat exchanger (3), an SCR reactor (5) connected with the heating furnace (4), and an ammonia adding unit connected with the SCR reactor (5); and the air outlet end of the SCR reactor (5) is connected with the internal circulation flue gas heat exchanger (3).
2. The sintering desulfurization and denitrification system according to claim 1, wherein the external circulation heat exchange unit comprises a heat-reducing heat exchanger (6) connected with the primary dedusting unit (1), and a heat-raising heat exchanger (8) connected with a bidirectional water circulation pipeline (7); the air outlet end of the heat-reducing heat exchanger (6) is connected with the desulfurization unit, the air inlet end of the heat-raising heat exchanger (8) is connected with the air outlet end of the desulfurization unit, and the air outlet end of the heat-raising heat exchanger (8) is connected with the air inlet end of the internal circulation flue gas heat exchanger (3).
3. The sintering desulfurization and denitrification system according to claim 2, wherein the desulfurization unit comprises an absorption tower (9) connected with the gas outlet end of the heat-reducing heat exchanger (6), a slurry tank (10) communicated with the absorption tower (9) and used for adding lime slurry, a filtrate tank (11) connected with the liquid outlet of the absorption tower (9), a plate-and-frame filter press (12) matched with the filtrate tank (11), and a flue gas condenser (13) communicated with the gas outlet of the absorption tower (9); and the air outlet end of the flue gas condenser (13) is connected with the air inlet end of the heat rising heat exchanger (8).
4. The system for sintering, desulfurization and denitrification according to claim 1, wherein the ammonia adding unit comprises an ammonia water storage tank (14) and an ammonia water evaporator (15) connected with the ammonia water storage tank; wherein the gas outlet end of the ammonia water evaporator (15) is connected with the SCR reactor (5).
5. The sintering desulfurization and denitrification system according to claim 1, wherein the primary dedusting unit (1) adopts an electric precipitator.
6. The sintering desulfurization and denitrification system according to claim 1, wherein the secondary dust removal unit (2) is a bag-type dust remover.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202020289283.7U CN212142129U (en) | 2020-03-10 | 2020-03-10 | Sintering desulfurization and denitrification system |
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| CN202020289283.7U CN212142129U (en) | 2020-03-10 | 2020-03-10 | Sintering desulfurization and denitrification system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113083014A (en) * | 2021-02-23 | 2021-07-09 | 王洪 | Be applied to lime wash cyclic utilization's of flue gas treatment SOx/NOx control device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113083014A (en) * | 2021-02-23 | 2021-07-09 | 王洪 | Be applied to lime wash cyclic utilization's of flue gas treatment SOx/NOx control device |
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