CN212204588U - Flue gas system of coal-fired boiler - Google Patents
Flue gas system of coal-fired boiler Download PDFInfo
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- CN212204588U CN212204588U CN202020168308.8U CN202020168308U CN212204588U CN 212204588 U CN212204588 U CN 212204588U CN 202020168308 U CN202020168308 U CN 202020168308U CN 212204588 U CN212204588 U CN 212204588U
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- 239000003546 flue gas Substances 0.000 title claims abstract description 126
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 125
- 239000003054 catalyst Substances 0.000 claims abstract description 40
- 239000000428 dust Substances 0.000 claims abstract description 37
- 238000001556 precipitation Methods 0.000 claims abstract description 25
- 239000003245 coal Substances 0.000 claims abstract description 15
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 13
- 230000023556 desulfurization Effects 0.000 claims abstract description 13
- 239000010881 fly ash Substances 0.000 claims abstract description 12
- 230000003197 catalytic effect Effects 0.000 claims abstract description 6
- 239000012717 electrostatic precipitator Substances 0.000 claims abstract description 4
- 238000006555 catalytic reaction Methods 0.000 claims abstract description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 7
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 5
- 238000009833 condensation Methods 0.000 description 5
- 230000005494 condensation Effects 0.000 description 5
- 238000009834 vaporization Methods 0.000 description 5
- 230000008016 vaporization Effects 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 238000009991 scouring Methods 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 229910052783 alkali metal Inorganic materials 0.000 description 3
- 150000001340 alkali metals Chemical class 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 230000000903 blocking effect Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 2
- 231100000572 poisoning Toxicity 0.000 description 2
- 230000000607 poisoning effect Effects 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
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- Chimneys And Flues (AREA)
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Abstract
The utility model discloses a coal fired boiler flue gas system, flue gas system include boiler economizer, high temperature electrostatic precipitator unit, SCR catalyst catalytic unit, air heater, GGH heat exchanger, low temperature heat exchanger and desulfurization system, characterized by: the flow of the high-temperature flue gas at 350-370 ℃ discharged from the rear of the boiler economizer is that the flue gas flows through a high-temperature electric precipitation unit, an SCR catalyst catalysis unit, an air preheater, a GGH heat exchanger, a low-temperature heat exchanger and a desulfurization system in sequence; the high-temperature electric precipitation unit is selected to reduce the content of fly ash in the flue gas subjected to high-temperature electric precipitation and dust removal to 0.3-0.5% of the original flue gas, and the low-temperature heat exchanger is selected to reduce the temperature of the flue gas subjected to the low-temperature heat exchanger to 75-80 ℃. The utility model discloses a coal fired power plant flue gas system, its SCR's life-span and active long, air heater and GGH heat exchanger are difficult for blockking up and the boiler is efficient.
Description
Technical Field
The utility model relates to a coal fired boiler flue gas system.
Background
At present, after the coal of a coal-fired power plant is combusted in a hearth of a boiler, the coal passes through a flue gas system, and then enters a desulfurization system and the like after sequentially passing through an SCR catalyst, an air preheater, a GGH heat exchanger and low-temperature electric dust removal. Because the flue gas containing a large amount of fly ash before electric precipitation respectively has the following problems when passing through the SCR catalyst and the air preheater:
1) SCR catalyst: the SCR catalyst mainly comprises an active component V2O5The carrier being TiO2The cocatalyst is WO3. The main structure types of the catalyst are honeycomb type, plate type and corrugated type, and the structures are designed to mainly increase the contact area of the catalyst so that the flue gas is fully contacted with the catalyst. However, the flue gas generated after the combustion of the coal contains a large amount of fly ash, which is the most important factor for the loss of the activity of the catalyst. The alkali metal contained in the fly ash contacts with the catalyst to cause the catalyst to be poisoned, and the activity of the catalyst is reduced. Also, when the micropores of the catalyst are clogged with the fly ash, the surface activity thereof is gradually lost, and the catalyst loses activity. In addition, the dust in the flue gas can strongly scour the catalyst when flowing at a high speed, so that the catalyst is lost and broken. The catalyst with reduced activity can generate waste strong acid or strong base waste liquid in treatment or recycling, and secondary pollution is generated to the environment.
2) An air preheater: the prior air preheater generally adopts two types of rotary regenerative type and tubular type. The temperature of the flue gas at the outlet of the air preheater is generally lower than 140 ℃, and because the SCR catalyst has an excessive phenomenon when ammonia gas is added, the excessive ammonia gas and H in the flue gas are reacted at 190-240 ℃ when the excessive ammonia gas passes through the air preheater2O、SO3Reaction to produce ammonium bisulfate (NH)4HSO4). Ammonium bisulfate condenses and adheres to the heat exchange element of the air preheater at the cold end part (177-232 ℃) of the air preheater, and captures the fly ash in the flue gas to form a hardened shape, so that the heat exchange element of the air preheater is blocked, the pressure difference of the air preheater is rapidly increased and uncontrollable, and the output of a coal-fired boiler is reduced.
3) When the flue gas containing the fly ash passes through the GGH heat exchanger before electric precipitation, the dust content in the flue gas is high, so that the heat exchange tubes of the heat exchanger are seriously washed, a large amount of heat exchange pipelines are leaked, the leaked water can capture the fly ash in the flue gas, a heat exchange channel blocked in the heat exchanger in a hardened manner is formed, the pressure difference of the heat exchanger is increased, and the heat exchange performance is sharply reduced.
4) When flue gas is dedusted by electric precipitation, the temperature of the flue gas subjected to electric precipitation is generally controlled to be not lower than 95 ℃ in order to avoid blockage of electric precipitation caused by high humidity. However, because the interior of the electric dust collector is in a negative pressure state, the temperature of the flue gas is generally controlled to still reach 100-105 ℃. At this time, the moisture contained in the flue gas still exists in a superheated steam state, and the latent heat of vaporization of the superheated steam contained in the moisture in the flue gas still cannot be utilized, so that the loss of the boiler exhaust smoke is increased, and the boiler efficiency is reduced.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem that a fire coal power plant flue gas system is provided exactly, its SCR's life-span and active long, air heater and GGH heat exchanger are difficult for blockking up and boiler efficiency is high.
Solve above-mentioned technical problem, the utility model discloses the technical scheme who adopts as follows:
the utility model provides a coal fired boiler flue gas system, flue gas system include boiler economizer, high temperature electrostatic precipitator unit, SCR catalyst catalytic unit, air heater, GGH heat exchanger, low temperature heat exchanger and desulfurization system, characterized by: and the flow of the high-temperature flue gas at 350-370 ℃ discharged from the rear of the boiler economizer is that the high-temperature flue gas flows through a high-temperature electric precipitation unit, an SCR catalyst catalysis unit, an air preheater, a GGH heat exchanger, a low-temperature heat exchanger and a desulfurization system in sequence.
Preferably, the high-temperature electric precipitation unit is selected so that the content of fly ash in the flue gas after the high-temperature flue gas is subjected to high-temperature electric precipitation for dust removal is reduced to 0.3% -0.5% of the original flue gas.
Preferably, the low-temperature heat exchanger is selected to reduce the temperature of the flue gas after the low-temperature heat exchanger to 75-80 ℃.
The principle of the utility model is as follows:
the utility model discloses at first remove dust through high temperature electrostatic precipitator with high temperature flue gas, get rid of the dust more than 99.6% in the former flue gas, fly ash content reduces to about 0.4% of former flue gas in the flue gas after the dust removal, directly purifies former flue gas into high temperature clean flue gas for flue gas dust content in getting into SCR catalyst, air heater, the GGH heat exchanger is extremely low, can not reduce equipment working property. The high-temperature clean flue gas respectively passes through an SCR catalyst and an air preheater to form primary low-temperature clean flue gas; and a low-temperature heat exchanger is additionally arranged behind the GGH heat exchanger to reduce the temperature of the flue gas to 75-80 ℃, so that superheated steam in the flue gas is condensed, latent heat of vaporization is released, and the loss of boiler exhaust smoke is greatly reduced. The first-stage low-temperature clean flue gas enters the GGH heat exchanger and the low-temperature heat exchanger, superheated steam in the flue gas is condensed to release latent heat of vaporization, and second-stage low-temperature clean flue gas is generated and enters the desulfurization system for desulfurization treatment.
The technical effects of the utility model are embodied as follows:
the system firstly makes full use of the characteristic that the specific resistance of dust is reduced along with the rise of the temperature after the temperature exceeds 180 ℃, high-temperature electric precipitation is used for replacing low-temperature electric precipitation, the dust removal efficiency of the high-temperature electric precipitation is higher than that of the low-temperature electric precipitation, and high-temperature clean flue gas is generated. The dust content in the high-temperature clean flue gas is low,in turn, theThe flue gas enters the SCR catalyst, the air preheater and the GGH heat exchanger to be respectively subjected to denitration and cooling treatment, so that the performance of the SCR catalyst can be better improved, the blocking probability of the air preheater is reduced, the GGH pressure difference is reduced, and the flue gas becomes first-stage low-temperature clean flue gas.
And after the first-stage clean flue gas enters the low-temperature heat exchanger, reducing the temperature of the clean flue gas to 75-80 ℃, condensing superheated steam in the flue gas and enabling the superheated steam to release latent heat of vaporization to form second-stage clean flue gas, and then, entering a desulfurization system. When the primary clean flue gas enters the low-temperature heat exchanger, due to the low dust content in the flue gas, the superheated steam is not mixed with dust to form hardening during condensation; water produced by condensation and SO in secondary clean flue gas3、SO2Reaction into H2SO4、H2SO3The dilute acid and the two dilute acids have strong corrosion to the inner shell of the heat exchanger, the heat exchange pipeline of the heat exchanger and the flue behind the heat exchanger, the material of the inner shell of the heat exchanger and the material of the heat exchange pipeline are made of sulfuric acid corrosion resistant stainless steel 00Cr25Ni6Mo2N, and the inner wall of the flue behind the heat exchanger is made of sulfuric acid corrosion resistant stainless steelThe corrosive heavy anti-corrosion coating is provided with enough gradient, so that the generated sulfuric acid automatically flows into the absorption tower of the desulfurization system, and is prevented from being accumulated in the heat exchanger and the flue.
The utility model discloses an in, overall system design can effectively improve dust collection efficiency, environmental protection equipment efficiency, the boiler efficiency of boiler flue gas system, has solved following problem: the problems of SCR catalyst poisoning, scouring and service life reduction, the problems of scouring damage and hardening blockage of heat exchange elements of the air preheater, the problems of GGH scouring and blockage and low boiler efficiency. The stability of the boiler efficiency in the change of coal types and the long-term high-efficiency operation of environment-friendly equipment are ensured.
Drawings
Fig. 1 is a flow chart of the whole system of the present invention.
In the figure: 1-high temperature electric precipitation unit; 2-SCR catalyst catalytic unit; 3-air preheater; 4-GGH heat exchanger; 5-low temperature heat exchanger.
The solid arrows indicate the direction of flue gas flow.
Detailed Description
As shown in FIG. 1, it is an embodiment of the flue gas system of the coal-fired boiler of the present invention. The coal-fired boiler flue gas system comprises a boiler economizer, a high-temperature electric precipitation unit 1, an SCR catalyst catalytic unit 2, an air preheater 3, a GGH heat exchanger 4, a low-temperature heat exchanger 5 and a desulfurization system. The flow of the high-temperature flue gas at 350-370 ℃ discharged from the rear of the boiler economizer is that the flue gas flows through a high-temperature electric precipitation unit 1, an SCR catalyst catalytic unit 2, an air preheater 3, a GGH heat exchanger 4, a low-temperature heat exchanger 5 and a desulfurization system in sequence.
The high-temperature electric precipitation unit 1 is selected to reduce the content of fly ash in the flue gas after the high-temperature flue gas is subjected to high-temperature electric precipitation for dust removal to 0.3% -0.5% of the original flue gas; the low-temperature heat exchanger 5 is selected to reduce the temperature of the flue gas after the low-temperature heat exchanger to 75-80 ℃.
The utility model discloses be applied to coal fired power plant flue gas system.
When the raw flue gas with the high temperature of 350-370 ℃ enters the high-temperature electric dust removal 1, dust in the flue gas is removed by electric dust removal, and the generated high-temperature clean flue gas enters the SCR catalyst 2 to remove NOx in the flue gas; and then the flue gas enters an air preheater 3 for heat exchange, the temperature of the flue gas is reduced to 130-150 ℃, the flue gas enters a GGH heat exchanger 4 for heat exchange, the temperature of the flue gas flowing out of the GGH heat exchanger 4 is reduced to 100-105 ℃, the flue gas becomes first-stage low-temperature clean flue gas, the first-stage low-temperature clean flue gas enters a low-temperature heat exchanger 5 for heating condensed water therein, the temperature is reduced to 80 ℃, the first-stage low-temperature clean flue gas becomes second-stage low-.
The utility model discloses a process and principle:
1. the high-temperature raw flue gas is subjected to high-temperature electric precipitation for dedusting treatment, so that the dust content in the flue gas is reduced, and the high-temperature clean flue gas is formed.
The high-temperature raw flue gas enters the high-temperature electric dust removal after being combed by the flow field, and the high-temperature electric dust removal has higher dust removal efficiency by utilizing the characteristics that the higher the dust temperature is and the smaller the specific resistance is, the higher the dust temperature is, the higher the specific resistance is. When high-temperature raw flue gas is subjected to high-temperature electric precipitation, more than 99.6% of dust in the flue gas can be removed, and the dust content in the high-temperature raw flue gas is reduced to be less than 0.4%, so that high-temperature clean flue gas is formed.
2. High-temperature clean flue gas enters the SCR catalyst for denitration treatment, so that poisoning and scouring damage of the catalyst are reduced.
High temperature clean flue gas carrying added NH3Gas enters an SCR catalyst, and NH is generated under the action of the catalyst3The reaction of the gas with NOx in the high temperature clean flue gas produces N2And H2And O, removing NOx in the flue gas. After the high-temperature clean flue gas is subjected to dust removal treatment, alkali metals contained in the high-temperature clean flue gas are basically removed, the residual trace dust carries trace alkali metals, the contact amount of the trace dust and a catalyst is reduced rapidly, and the catalyst is not poisoned; the dust content in the high-temperature clean flue gas is little, and the catalyst can not be scoured and damaged.
3. The high-temperature clean flue gas enters the air preheater to be cooled, and the pressure difference of the air preheater is reduced to become first-stage low-temperature clean flue gas.
The high temperature clean flue gas from the SCR catalyst carries excess NH due to ammonia injection3Gas, NH3The gas entering the airIn the cooling process after the preheater, when the temperature reaches 190-240 ℃, the SO in the high-temperature clean flue gas can be removed3The ammonium bisulfate is generated by reaction and is condensed at the cold end part (177-232 ℃) of the air preheater and is bonded on a heat exchange element of the air preheater, and because the dust content in the high-temperature clean flue gas is extremely low, the amount of the ammonium bisulfate bonded on the heat exchange element of the air preheater for capturing dust is small, the hardening phenomenon is not easy to occur, and the blocking probability of the air preheater is reduced; the cold end of the air preheater is flushed to more easily clean the ammonium bisulfate, and the pressure difference of the flue gas side is stabilized in a controllable range. And after the high-temperature clean flue gas of the air preheater is cooled, the temperature reaches 130-140 ℃ to become first-grade low-temperature clean flue gas.
4. The first-stage low-temperature clean flue gas enters the GGH heat exchanger to be cooled, and the washing of the heat exchanger is reduced.
And (3) enabling the primary low-temperature clean flue gas flowing out of the air preheater to enter a GGH heat exchanger for cooling, and reducing the temperature to 100-105 ℃. The dust content in the first-level low-temperature clean flue gas is low, the elements of the GGH heat exchanger are not washed, the working performance of the GGH can be kept stable, and the problem that the heat exchanger is blocked by accumulated dust is solved.
5. And the primary low-temperature clean flue gas enters a low-temperature heat exchanger, and superheated steam in the clean flue gas is condensed to release heat.
The clean flue gas of one-level low temperature flows out behind the GGH heat exchanger, get into low temperature heat exchanger, the condensation working medium adopts 35 ~ 40 ℃ condensate system's condensate water in the low temperature heat exchanger, make full use of the characteristics that condensate water specific heat capacity is big, cool down the clean flue gas of one-level low temperature to 75 ~ 80 ℃, superheated steam condensation in the clean flue gas, the latent heat of vaporization is released in the condensation process, the total moisture that contains in the fire coal is higher, the more the internal energy that low temperature heat exchanger absorbs, can say that boiler exhaust fume loss control is in a stable scope, the whole efficiency of boiler can not take place great change because of the change of coal-fired coal kind yet.
Claims (3)
1. The utility model provides a coal fired boiler flue gas system, flue gas system include boiler economizer, high temperature electrostatic precipitator unit, SCR catalyst catalytic unit, air heater, GGH heat exchanger, low temperature heat exchanger and desulfurization system, characterized by: and the flow of the high-temperature flue gas at 350-370 ℃ discharged from the rear of the boiler economizer is that the high-temperature flue gas flows through a high-temperature electric precipitation unit, an SCR catalyst catalysis unit, an air preheater, a GGH heat exchanger, a low-temperature heat exchanger and a desulfurization system in sequence.
2. The coal fired boiler flue gas system of claim 1, wherein: the high-temperature electric precipitation unit is selected to reduce the content of fly ash in the flue gas after the high-temperature flue gas is subjected to high-temperature electric precipitation for dust removal to 0.3-0.5% of the original flue gas.
3. The coal fired boiler flue gas system according to claim 1 or 2, characterized in that: the low-temperature heat exchanger is selected to reduce the temperature of the flue gas behind the low-temperature heat exchanger to 75-80 ℃.
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| CN202020168308.8U CN212204588U (en) | 2020-02-13 | 2020-02-13 | Flue gas system of coal-fired boiler |
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| CN202020168308.8U CN212204588U (en) | 2020-02-13 | 2020-02-13 | Flue gas system of coal-fired boiler |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111365726A (en) * | 2020-02-13 | 2020-07-03 | 广东粤电靖海发电有限公司 | Flue gas system of coal-fired boiler |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111365726A (en) * | 2020-02-13 | 2020-07-03 | 广东粤电靖海发电有限公司 | Flue gas system of coal-fired boiler |
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