CN210814554U - System applied to oxygen-enriched combustion of coal-fired power plant boiler - Google Patents
System applied to oxygen-enriched combustion of coal-fired power plant boiler Download PDFInfo
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- CN210814554U CN210814554U CN201921294191.1U CN201921294191U CN210814554U CN 210814554 U CN210814554 U CN 210814554U CN 201921294191 U CN201921294191 U CN 201921294191U CN 210814554 U CN210814554 U CN 210814554U
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Abstract
The utility model belongs to the technical field of flue gas purification and utilization technique and specifically relates to a system for be applied to coal fired power plant boiler oxygen boosting burning. The utility model provides a system for be applied to coal fired power plant boiler oxygen boosting burning, including clean flue gas preliminary treatment subsystem, PSA carbon nitrogen separation subsystem, PSA system high-purity nitrogen subsystem and the dry intensification subsystem of oxygen boosting desorption gas, clean flue gas preliminary treatment subsystem is connected with PSA carbon nitrogen separation subsystem through first compressor, PSA carbon nitrogen separation subsystem is connected with PSA system high-purity nitrogen subsystem, PSA system high-purity nitrogen subsystem is connected with the dry intensification subsystem of oxygen boosting desorption gas. The utility model discloses a be applied to coal fired power plant boiler oxygen boosting burning's system greatly reduces the emission of flue gas, retrieves the oxygen in the flue gas, carries it to boiler furnace and carries out the oxygen boosting burning to reducible forced draught blower, draught fan are exerted oneself, save the electric quantity, reduce boiler coal-fired volume, simple structure, the flexibility is high, invests in for a short time, and the energy consumption is low, and the treatment effect is excellent.
Description
Technical Field
The utility model belongs to the technical field of flue gas purification and utilization technique and specifically relates to a system for be applied to coal fired power plant boiler oxygen boosting burning.
Background
With the development of the industrialization process, the number of various power plants in China is increasing day by day. Along with the combustion of the boiler fuel, a large amount of flue gas is generated. The emission of the flue gas brings great harm to the environment. Therefore, the control of the emission amount of the flue gas and the recovery and utilization of the emitted flue gas become very concerned problems in all countries of the world.
The flue gas of the boiler of the coal-fired power plant mainly comprises four types of gases of nitrogen, carbon dioxide, water and oxygen, and the discharge amount of the flue gas can be reduced by recovering the oxygen in the flue gas and sending the recovered oxygen into the boiler for oxygen-enriched combustion. The existing system applied to the oxygen-enriched combustion of the boiler of the coal-fired power plant has the advantages of complex structure, low flexibility, large investment, high energy consumption and improvement of treatment effect.
Therefore, the system applied to the oxygen-enriched combustion of the boiler in the coal-fired power plant is simple in structure, high in flexibility, low in investment, low in energy consumption and excellent in treatment effect, and the technical problem to be solved by technical personnel in the field is urgently needed.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a be applied to coal fired power plant boiler oxygen boosting burning's system overcomes the not enough of aforementioned prior art, and the flexibility is high, the investment is little, the energy consumption is low, the treatment effect is excellent.
The utility model provides a technical scheme that its technical problem adopted is:
a system applied to oxygen-enriched combustion of a boiler of a coal-fired power plant comprises a clean flue gas pretreatment subsystem, a PSA carbon-nitrogen separation subsystem, a PSA high-purity nitrogen preparation subsystem and an oxygen-enriched desorbed gas drying and heating subsystem, wherein the clean flue gas pretreatment subsystem is connected with the PSA carbon-nitrogen separation subsystem through a first compressor, the PSA carbon-nitrogen separation subsystem is connected with the PSA high-purity nitrogen preparation subsystem, and the PSA high-purity nitrogen preparation subsystem is connected with the oxygen-enriched desorbed gas drying and heating subsystem; the flue gas pretreatment subsystem is used for cooling and dehydrating clean flue gas subjected to desulfurization and denitration of boiler flue gas; the PSA carbon-nitrogen separation subsystem is used for pressure swing adsorption of the pretreated flue gas to obtain carbon dioxide desorption gas and discharge nitrogen and oxygen; the PSA high-purity nitrogen preparation subsystem performs pressure swing adsorption on the mixed gas containing nitrogen and oxygen discharged from the PSA carbon-nitrogen separation subsystem to obtain oxygen-enriched desorption gas and discharge high-purity nitrogen; the oxygen-enriched desorption gas drying and heating subsystem is used for recovering, drying and heating the waste heat of the oxygen-enriched desorption gas prepared by the PSA high-purity nitrogen preparation system, and then conveying the oxygen-enriched desorption gas to a boiler over-fire air layer for burning coal powder.
Further, clean flue gas preliminary treatment subsystem includes draught fan, first cooler and first water diversion jar, and the clean flue of desulfurizing tower is connected through the pipeline with the draught fan entry, and the draught fan export is connected with first cooler hot junction entry through the pipeline, and the export of first cooler hot section is connected with first water diversion jar through the pipeline, and the gas vent at first water diversion jar top is connected with the air inlet of first compressor through the pipeline.
Furthermore, the PSA carbon nitrogen separation subsystem is formed by a plurality of parallel adsorption towers, adsorbents are filled in the adsorption towers, the adsorption towers adsorb carbon dioxide and discharge oxygen and nitrogen from the tops of the adsorption towers to the mixed gas main pipe, and reverse desorption gas is discharged from the bottoms of the adsorption towers to the desorption gas main pipe; each adsorption tower in the PSA carbon-nitrogen separation subsystem needs to go through the working stages of adsorption, pressure equalization drop, reverse discharge, pressure equalization rise and final pressure rise, and according to the actual requirements, part of the adsorption towers in the PSA carbon-nitrogen separation subsystem are in the adsorption stage, and the other adsorption towers are in different stages of bed body regeneration.
Further, the outlet of the first compressor is connected with the PSA carbon-nitrogen separation subsystem air inlet main pipe through a pipeline.
Furthermore, the PSA system high-purity nitrogen subsystem is composed of a plurality of parallel adsorption towers, and carbon molecular sieves are filled in the adsorption towers of the PSA system high-purity nitrogen subsystem; the PSA high-purity nitrogen preparation subsystem is used for performing pressure swing adsorption on mixed gas discharged from the top of an adsorption tower of the PSA carbon-nitrogen separation subsystem, and the PSA high-purity nitrogen preparation subsystem can obtain high-purity nitrogen with the concentration of more than 98% and desorbed gas with the oxygen content of 32-36%.
Further, the PSA system high-purity nitrogen subsystem air inlet main pipe is connected with the PSA carbon-nitrogen separation subsystem mixed gas main pipe.
Furthermore, the oxygen-enriched desorption gas drying and heating subsystem comprises a buffer tank, a second compressor, a pressure stabilizing tank, a second cooler, a second water dividing tank, a drying bed, a raw flue heat exchanger, a water-melting workshop desalting water tank, a desalting water pump, a deaerator and a mixer, wherein an inlet of the buffer tank is connected with a desorption gas main pipe of the PSA high-purity nitrogen making subsystem through a pipeline, an outlet of the buffer tank is connected with an inlet of the second compressor through a pipeline, the buffer tank buffers the oxygen-enriched desorption gas from the PSA high-purity nitrogen making subsystem to reduce air flow fluctuation, the oxygen-enriched desorption gas is conveniently and stably conveyed to the second compressor, an outlet of the second compressor is connected with an inlet of the pressure stabilizing tank through a pipeline, an outlet of the pressure stabilizing tank is connected with a hot section inlet of the second cooler through a pipeline, an outlet of the hot section of the second cooler is connected with an inlet of the second water dividing tank through a pipeline, the pressure stabilizing tank stabilizes the oxygen-enriched desorption gas output by the second compressor, the second cooler cools the oxygen-enriched desorption gas conveyed by the second compressor, an exhaust port at the top of the second water dividing tank is connected with an inlet of a drying bed through a pipeline, the oxygen-enriched desorption gas with moisture separated out due to cooling is subjected to gas-liquid separation by the second water dividing tank, the oxygen-enriched desorption gas is subjected to primary drying, an outlet of the drying bed is connected with a cold section inlet of an original flue heat exchanger through a pipeline, the drying bed performs deep drying and water removal on the dried oxygen-enriched desorption gas to obtain dried oxygen-enriched desorption gas, the dried oxygen-enriched desorption gas cools flue gas of an original flue and enables the flue gas to be heated, the overall thermal efficiency of the boiler is improved, a cold end outlet of the original flue heat exchanger is connected with an inlet of a mixer, and an outlet of the mixer is connected with a boiler burnout air pipe; the bottom export of the demineralized water case of water melting workshop is connected with the entry of demineralized water pump, the export of demineralized water pump is connected with the cold junction entry of second cooler, the cold junction export of second cooler is connected with the entry of oxygen-eliminating device, regard demineralized water as the cold source of second cooler with water melting workshop, retrieve the heat of second cooler oxygen boosting desorption gas, make demineralized water when getting into the oxygen-eliminating device, the temperature obtains promoting, oxygen-eliminating device steam consumption has been reduced, and then boiler coal consumption has been reduced.
Furthermore, the mixer is a three-way mixer, one interface in the mixer is used for being connected with an outlet of a cold section of the original flue heat exchanger, one interface is used for being connected with an original over-fire air pipe of the boiler, and the other interface is used for being connected with an air port pipeline of an over-fire air layer of the boiler.
Furthermore, a drying bed in the oxygen-enriched desorption gas drying and purifying subsystem is complete equipment for dehydrating and drying carbon dioxide, and in order to ensure economy, the complete drying bed equipment is provided with auxiliary regeneration equipment to regenerate the filler in the drying bed.
Further, a buffer tank in the oxygen-enriched desorption gas drying and purifying subsystem is used for buffering and stabilizing the pressure of the desorption gas from the PSA high-purity nitrogen preparation subsystem.
Furthermore, the raw flue heat exchanger in the oxygen-enriched desorption gas drying and purifying subsystem can be a compartment (sub-compartment) on a boiler air preheater, and the compartment (sub-compartment) is used for heating the oxygen-enriched gas and adjusting the temperature of the exhaust smoke; the original flue gas heat exchanger can also be independently arranged, the flue gas at the front section of the air preheater is preferably selected as a heat source of the heat exchanger to heat the oxygen-enriched gas, and the flue gas after heat exchange can be guided to the original flue behind the air preheater.
The utility model has the advantages that: compared with the prior art, the utility model discloses a be applied to system of coal fired power plant boiler oxygen boosting burning greatly reduces the emission of flue gas, retrieves the oxygen in the flue gas, carries it to boiler furnace and carries out the oxygen boosting burning to reducible forced draught blower, draught fan are exerted oneself, save the electric quantity, reduce boiler coal-fired quantity, simple structure, the flexibility is high, and the investment is little, and the energy consumption is low, and the treatment effect is excellent.
Drawings
FIG. 1 is a system flow diagram of the present invention;
FIG. 2 is a flow chart of the flue gas pretreatment system of the present invention;
FIG. 3 is a flow chart of the oxygen-enriched desorption gas drying and heating system of the present invention;
wherein, 1 clean flue gas preliminary treatment subsystem, 101 draught fan, 102 first cooler, 103 first water diversion jar, 2 PSA carbon nitrogen separation subsystem, 3 PSA system high-purity nitrogen subsystem, 4 oxygen boosting desorption gas drying and heating subsystem, 401 buffer tank, 402 second compressor, 403 surge tank, 404 second cooler, 405 second water diversion jar, 406 drying bed, 407 former flue heat exchanger, 408 water melting workshop demineralized water tank, 409 demineralized water pump, 410 oxygen-eliminating device, 411 blender, 5 first compressor, 6 boiler burn-out air layer wind gap pipelines, 7 boiler burn-out tuber pipes.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the drawings in the embodiments of the present invention are combined below to clearly and completely describe the technical solutions in the embodiments of the present invention.
Example 1
In this embodiment, the clean flue gas conditions after desulfurization of the coal-fired boiler are as follows: the temperature of the flue gas is 50 ℃, the content of carbon dioxide in the flue gas is 13%, the content of nitrogen in the flue gas is 71%, the content of oxygen in the flue gas is 6%, the content of sulfur dioxide in the flue gas is 35mg/Nm3, the content of nitrogen oxide in the flue gas is 50mg/Nm3, and the content of water vapor in the flue gas is 12%.
As shown in fig. 1, a system applied to oxygen-enriched combustion of a boiler in a coal-fired power plant comprises a clean flue gas pretreatment subsystem 1, a PSA carbon nitrogen separation subsystem 2, a PSA high-purity nitrogen preparation subsystem 3 and an oxygen-enriched desorbed gas drying and heating subsystem 4, wherein the clean flue gas pretreatment subsystem 1 is connected with the PSA carbon nitrogen separation subsystem 2 through a first compressor 5, the PSA carbon nitrogen separation subsystem 2 is connected with the PSA high-purity nitrogen preparation subsystem 3, and the PSA high-purity nitrogen preparation subsystem 3 is connected with the oxygen-enriched desorbed gas drying and heating subsystem 4; the flue gas pretreatment subsystem 1 is used for cooling and dehydrating clean flue gas after desulfurization and denitration of boiler flue gas; the PSA carbon-nitrogen separation subsystem 2 is used for pressure swing adsorption of the pretreated flue gas to obtain carbon dioxide desorption gas and discharge nitrogen and oxygen; the PSA system high-purity nitrogen subsystem 3 carries out pressure swing adsorption on the flue gas containing nitrogen and oxygen discharged from the PSA carbon-nitrogen separation subsystem 2 to obtain oxygen-enriched desorption gas and remove high-purity nitrogen; the oxygen-enriched desorption gas drying and heating subsystem 4 is used for recovering, drying and heating the waste heat of the oxygen-enriched desorption gas prepared by the PSA high-purity nitrogen preparation subsystem 3, and then conveying the oxygen-enriched desorption gas to a boiler over-fire air layer for burning coal powder.
As shown in fig. 2, the clean flue gas pretreatment subsystem 1 comprises an induced draft fan 101, a first cooler 102 and a first water diversion tank 103, wherein a clean flue of the desulfurization tower is connected with an inlet of the induced draft fan 101 through a pipeline, an outlet of the induced draft fan 101 is connected with an inlet of a hot end of the first cooler 102 through a pipeline, flue gas is pressurized to 0.1Mpa by the induced draft fan 101 and introduced into the first cooler 102, the first cooler 102 is cooled by industrial circulating water, the temperature of the flue gas is reduced from 50 ℃ to 40 ℃ through the first cooler 102, the outlet of the hot section of the first cooler 102 is connected with the first water dividing tank 103 through a pipeline, the first water dividing tank 103 separates the moisture in the flue gas cooled by the first cooler 102, the exhaust port at the top of the first water dividing tank 103 is connected with the air inlet of the first compressor 5 through a pipeline, and the first compressor 5 pressurizes the dry flue gas discharged from the top of the first water dividing tank 103 to 1MPa and sends the dry flue gas into the adsorption tower of the PSA carbon nitrogen separation subsystem 2.
In this embodiment, the PSA carbon nitrogen separation subsystem 2 is composed of a plurality of adsorption towers arranged in parallel, and the adsorption towers are filled with an adsorbent and pressure swing adsorb the flue gas delivered from the first compressor 5. Adsorbing carbon dioxide by an adsorption tower, discharging oxygen and nitrogen from the top of the adsorption tower to a mixed gas main pipe (the mixed gas discharged from the top contains 3-5% of carbon dioxide gas), and discharging reverse desorption gas to a desorption gas main pipe from the bottom of the adsorption tower; each adsorption tower in the PSA carbon-nitrogen separation subsystem (2) needs to go through the working stages of adsorption, pressure drop equalization, reverse discharge, pressure rise equalization and final pressure rise.
In this embodiment, the outlet of the first compressor 5 is connected to the PSA carbon nitrogen separation subsystem inlet main pipe through a pipeline.
In this embodiment, the PSA high-purity nitrogen generation subsystem 3 is composed of a plurality of adsorption towers arranged in parallel, and the adsorption towers of the PSA high-purity nitrogen generation subsystem 3 are filled with carbon molecular sieves; the PSA high-purity nitrogen preparation subsystem 3 is used for performing pressure swing adsorption on mixed gas discharged from the top of the adsorption tower of the PSA carbon-nitrogen separation subsystem 2, and the PSA high-purity nitrogen preparation subsystem can obtain high-purity nitrogen with the concentration of more than 98% and desorbed gas with the oxygen content of 32-36%.
In this embodiment, the gas inlet main pipe of the PSA high-purity nitrogen generation subsystem 3 is connected to the mixed gas main pipe of the PSA carbon-nitrogen separation system 2.
As shown in fig. 3, the oxygen-enriched desorbed gas drying and heating subsystem 4 comprises a buffer tank 401, a second compressor 402, a surge tank 403, a second cooler 404, a second branched water tank 405, a drying bed 406, a raw flue heat exchanger 407, a water-chemical plant desalting water tank 408, a desalting water pump 409, a deaerator 410 and a mixer 411, wherein an inlet of the buffer tank 401 is connected with a desorbed gas pipeline of the last adsorption tower of the PSA high-purity nitrogen making subsystem 3, an outlet of the buffer tank 401 is connected with an inlet of the second compressor 402 through a pipeline, the buffer tank 401 buffers the oxygen-enriched desorbed gas from the PSA high-purity nitrogen making subsystem 3 to reduce gas flow fluctuation and facilitate stable delivery to the second compressor 402, an outlet of the second compressor 402 is connected with an inlet of the surge tank 403 through a pipeline, an outlet of the surge tank 403 is connected with a hot section inlet of the second cooler 404 through a pipeline, an outlet of the hot section of the second cooler 404 is connected with an inlet of the second branched water tank 405 through a pipeline, the pressure stabilizing tank 403 stabilizes the oxygen-enriched desorbed gas output by the second compressor 402, and is conveniently and stably conveyed into the second cooler 404, the second cooler 404 cools the oxygen-enriched desorbed gas conveyed by the second compressor 402, an exhaust port at the top of the second water dividing tank 405 is connected with an inlet of the drying bed 406 through a pipeline, the second water dividing tank 405 performs gas-liquid separation on the oxygen-enriched desorbed gas with moisture separated out due to cooling, and performs primary drying on the oxygen-enriched desorbed gas, an outlet of the drying bed 406 is connected with a cold section inlet of the original flue heat exchanger 407 through a pipeline, the drying bed 406 performs deep drying and water removal on the dried oxygen-enriched desorbed gas to obtain dried oxygen-enriched desorbed gas, the dried oxygen-enriched desorbed gas cools the flue gas of the original flue and heats the flue gas per se to improve the overall thermal efficiency of the boiler, an outlet at the cold end of the original flue heat exchanger 407 is connected with an inlet of the mixer 411, the outlet of the mixer 411 is connected with the air port pipeline 6 of the over-fire air layer of the boiler; the bottom export of the demineralized water workshop demineralized water tank 408 is connected with the entry of demineralized water pump 409, the export of demineralized water pump 409 is connected with the cold junction entry of second cooler 404, the cold junction export of second cooler 404 is connected with the entry of oxygen-eliminating device 410, use demineralized water workshop demineralized water 408 as the cold source of second cooler 404, retrieve the heat of second cooler 404 oxygen-enriched desorption gas, make demineralized water when getting into the oxygen-eliminating device, the temperature is promoted, oxygen-eliminating device 410 steam consumption has been reduced, and then boiler coal consumption has been reduced.
In this embodiment, the mixer 411 is a three-way mixer, one interface of the mixer is used for being connected with the outlet of the cold section of the raw flue heat exchanger 407, one interface is used for being connected with the raw over-fire air pipe 7 of the boiler, and one interface is used for being connected with the air port pipeline 6 of the over-fire air layer of the boiler, after the oxygen-enriched desorbed gas and the raw over-fire air of the boiler are mixed and heat-exchanged in the mixer, the oxygen-enriched desorbed gas is introduced into the air port pipeline of the over-fire air layer of the boiler and is sent into the hearth of the boiler, and the temperature of the mixed over-fire air is higher than that of the raw over-fire air.
In this embodiment, the drying bed 406 in the oxygen-rich desorbed gas drying and purifying subsystem 4 is a complete set of equipment for dehydrating and drying carbon dioxide, and in order to ensure economy, all the complete set of drying bed equipment have an attached regeneration device for regenerating the filler in the drying bed, in this embodiment, the regenerated exhaust gas is introduced into the original flue at the front section of the desulfurization tower; the co-drying bed 406 is designed as two cylindrical adsorption beds of the same volume, each adsorption bed is filled with equal weight of adsorbent, and the adsorption and regeneration processes of the two beds are operated alternately to keep the production continuous.
In this embodiment, the raw flue gas heat exchanger 407 in the oxygen-enriched desorption gas drying and purifying subsystem 4 is configured as a new sub-bin of a rotary boiler air preheater, and is used for heating oxygen-enriched gas and adjusting the temperature of exhaust gas, so that the oxygen-enriched gas is heated to above 320 ℃.
By the system applied to the oxygen-enriched combustion of the boiler in the coal-fired power plant, the discharge amount of the flue gas is greatly reduced, the oxygen in the flue gas is recovered and conveyed to the hearth of the boiler for oxygen-enriched combustion, the output of a blower and an induced draft fan is greatly reduced, and the electric quantity is saved; the coal burning amount of the boiler is reduced, so that the boiler flue gas is recycled.
The above embodiments are only specific cases of the present invention, and the protection scope of the present invention includes but is not limited to the forms and styles of the above embodiments, and any suitable changes or modifications made thereto by those skilled in the art according to the claims of the present invention shall fall within the protection scope of the present invention.
Claims (7)
1. The utility model provides a system for be applied to coal fired power plant boiler oxygen boosting burning which characterized in that: including clean flue gas preliminary treatment subsystem (1), PSA carbon nitrogen separation subsystem (2), PSA system high-purity nitrogen subsystem (3) and dry intensification subsystem of oxygen boosting desorption gas (4), clean flue gas preliminary treatment subsystem (1) is connected with PSA carbon nitrogen separation subsystem (2) through first compressor (5), and PSA carbon nitrogen separation subsystem (2) is connected with PSA system high-purity nitrogen subsystem (3), and PSA system high-purity nitrogen subsystem (3) are connected with dry intensification subsystem of oxygen boosting desorption gas (4).
2. The system of claim 1, wherein the system is applied to the oxygen-enriched combustion of the coal-fired power plant boiler, and is characterized in that: clean flue gas preliminary treatment subsystem (1) is including draught fan (101), first cooler (102) and first water diversion jar (103), and the clean flue of desulfurizing tower is connected through the pipeline with draught fan (101), and draught fan (101) export is connected with first cooler (102) hot junction entry through the pipeline, and first cooler (102) hot section export is connected with first water diversion jar (103) through the pipeline, and the gas vent at first water diversion jar (103) top is connected with the air inlet of first compressor (5) through the pipeline.
3. The system applied to the oxygen-enriched combustion of the coal-fired power plant boiler is characterized in that the PSA carbon-nitrogen separation subsystem (2) is composed of a plurality of parallel adsorption towers, the adsorption towers are filled with adsorbents, the adsorption towers adsorb carbon dioxide and discharge oxygen and nitrogen from the tops of the adsorption towers to a mixed gas main pipe, and reversely-released desorption gas is discharged from the bottoms of the adsorption towers to a desorption gas main pipe; each adsorption tower in the PSA carbon-nitrogen separation subsystem (2) needs to go through the working stages of adsorption, pressure drop equalization, reverse discharge, pressure rise equalization and final pressure rise.
4. The system of claim 1, wherein the system is applied to the oxygen-enriched combustion of the coal-fired power plant boiler, and is characterized in that: the outlet of the first compressor (5) is connected with a gas inlet main pipe of the PSA carbon-nitrogen separation subsystem (2) through a pipeline.
5. The system of claim 4, wherein the oxygen-enriched combustion system is applied to the boiler of the coal-fired power plant: the PSA high-purity nitrogen preparation subsystem (3) is formed by paralleling a plurality of adsorption towers, and carbon molecular sieves are filled in the adsorption towers of the PSA high-purity nitrogen preparation subsystem (3); an air inlet main pipe in the PSA high-purity nitrogen preparation subsystem (3) is connected with a mixed gas main pipe of the PSA carbon-nitrogen separation subsystem (2) through a pipeline, and the PSA high-purity nitrogen preparation subsystem (3) performs pressure swing adsorption on the mixed gas discharged from the top of an adsorption bed in the PSA carbon-nitrogen separation subsystem (2).
6. The system of claim 5, wherein the system is applied to the oxygen-enriched combustion of the coal-fired power plant boiler, and is characterized in that: the oxygen-enriched desorbed gas drying and heating subsystem (4) comprises a buffer tank (401), a second compressor (402), a pressure stabilizing tank (403), a second cooler (404), a second water dividing tank (405), a drying bed (406), a raw flue heat exchanger (407), a water-chemical workshop desalted water tank (408), a desalted water pump (409), a deaerator (410) and a mixer (411), wherein an inlet of the buffer tank (401) is connected with a desorbed gas main pipe of the PSA high-purity nitrogen making subsystem (3) through a pipeline, an outlet of the buffer tank (401) is connected with an inlet of the second compressor (402) through a pipeline, an outlet of the second compressor (402) is connected with an inlet of the pressure stabilizing tank (403) through a pipeline, an outlet of the pressure stabilizing tank (403) is connected with an inlet of a hot section of the second cooler (404) through a pipeline, an outlet of the hot section of the second cooler (404) is connected with an inlet of the second water dividing tank (405) through a pipeline, an exhaust port at the top of the second water dividing tank (405) is connected with an inlet of a drying bed (406) through a pipeline, an outlet of the drying bed (406) is connected with a cold section inlet of a raw flue heat exchanger (407) through a pipeline, a cold end outlet of the raw flue heat exchanger (407) is connected with an inlet of a mixer (411), and an outlet of the mixer (411) is connected with a tuyere pipeline (6) of an over-fired air layer of the boiler; the bottom outlet of the demineralized water tank (408) of the water melting workshop is connected with the inlet of a demineralized water pump (409), the outlet of the demineralized water pump (409) is connected with the cold end inlet of a second cooler (404), and the cold end outlet of the second cooler (404) is connected with the inlet of a deaerator (410).
7. The system of claim 6, wherein the oxygen-enriched combustion system comprises: the mixer (411) is a three-way mixer, one connector of the mixer (411) is used for being connected with a cold section outlet of the primary flue heat exchanger (407), one connector of the mixer is used for being connected with a primary overfire air pipe (7) of the boiler, and the other connector of the mixer is used for being connected with an air port pipeline (6) of an overfire air layer of the boiler.
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| CN201921294191.1U CN210814554U (en) | 2019-08-12 | 2019-08-12 | System applied to oxygen-enriched combustion of coal-fired power plant boiler |
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| CN201921294191.1U CN210814554U (en) | 2019-08-12 | 2019-08-12 | System applied to oxygen-enriched combustion of coal-fired power plant boiler |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113028844A (en) * | 2021-04-02 | 2021-06-25 | 攀枝花攀钢集团设计研究院有限公司 | Blast furnace hot blast stove flue gas waste heat recovery device and recovery method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113028844A (en) * | 2021-04-02 | 2021-06-25 | 攀枝花攀钢集团设计研究院有限公司 | Blast furnace hot blast stove flue gas waste heat recovery device and recovery method |
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