CN213956022U - Rotary kiln flue gas treatment system - Google Patents
Rotary kiln flue gas treatment system Download PDFInfo
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- CN213956022U CN213956022U CN202022788621.4U CN202022788621U CN213956022U CN 213956022 U CN213956022 U CN 213956022U CN 202022788621 U CN202022788621 U CN 202022788621U CN 213956022 U CN213956022 U CN 213956022U
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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
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Abstract
The utility model discloses a rotary kiln flue gas treatment system, which comprises a rotary kiln, a secondary combustion chamber, a waste heat boiler, a quench tower, a dry deacidification tower, a dust remover, a washing tower, a wet deacidification tower and a diversion flue; the rotary kiln, the secondary combustion chamber, the waste heat boiler, the quench tower, the dry deacidification tower, the dust remover, the washing tower and the wet deacidification tower are sequentially connected along the advancing direction of the flue gas; the split-flow flue is connected between the dust remover and the washing tower. The utility model discloses burn the flue gas that produces to the rotary kiln and handle, make the flue gas satisfy the emission requirement, wherein through the heat tracing heat source of reposition of redundant personnel flue with flue gas heat group conduct liquid waste transport, solve the jam problem of rotary kiln liquid waste feeding, improve rotary kiln incineration efficiency.
Description
Technical Field
The utility model relates to a hazardous waste handles technical field, especially relates to a rotary kiln flue gas processing system.
Background
At present, the main types of furnaces used for burning hazardous wastes at home and abroad are rotary kiln incinerator, grate furnace, liquid injection incinerator, fluidized bed incinerator, multi-layer bed incinerator, pyrolysis incinerator and the like, the burning process of the hazardous wastes is complex, and the rotary kiln furnace is widely adopted due to the advantages of simple structure, strong adaptability to the hazardous wastes, stable control, easy operation, mature technology, long operation history and the like. The flue gas generated by incineration needs to be purified because of harmful substances such as sulfur dioxide, nitrogen oxides, hydrogen chloride, hydrogen fluoride, heavy metals, dust, dioxin and the like. The temperature of the incinerated flue gas reaches about 1100 ℃, the incinerated flue gas contains high heat, and how to efficiently utilize the heat of the flue gas needs to be considered, and meanwhile, harmful substances in the flue gas are reduced as much as possible.
The common flue gas treatment scheme is to treat sulfur dioxide, nitrogen oxide, hydrogen chloride, hydrogen fluoride, heavy metals and dust in the flue gas, and does not consider heat recovery to cause heat loss in the flue gas. The primary air of the rotary kiln comes from outside air, and the combustion efficiency is low. Meanwhile, in order to avoid the phenomenon of 'white smoke' of the smoke at the outlet of the exhaust chimney, the smoke after deacidification by the wet method is heated by external steam, so that energy waste is caused.
In addition, the liquid waste in partial areas can be blocked due to the fact that the environmental temperature is too low in winter before the liquid waste enters the rotary kiln to be incinerated, and potential safety hazards exist in operation.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to provide a rotary kiln flue gas processing system who realizes flue gas heat recovery.
The utility model provides a technical scheme that its technical problem adopted is: the rotary kiln flue gas treatment system comprises a rotary kiln for burning hazardous wastes and generating flue gas, a secondary combustion chamber for carrying out secondary combustion treatment on the flue gas to form high-temperature flue gas, a waste heat boiler for reducing the temperature of the high-temperature flue gas to generate steam and carrying out SNCR denitration in the steam, a quench tower for exchanging heat and reducing the temperature of the cooled flue gas, a dry deacidification tower for carrying out adsorption purification treatment on the flue gas, a dust remover for carrying out dust removal filtration treatment on the flue gas after the adsorption purification treatment, a washing tower for washing the flue gas after the dust removal filtration by using weak alkali washing liquid, a wet deacidification tower for carrying out deacidification treatment on the washed flue gas by using strong alkali liquid, and a diversion flue of a heat tracing heat source for conveying the flue gas serving as the liquid wastes of the hazardous wastes;
the rotary kiln, the secondary combustion chamber, the waste heat boiler, the quench tower, the dry deacidification tower, the dust remover, the washing tower and the wet deacidification tower are sequentially connected along the advancing direction of the flue gas; the split-flow flue is connected between the dust remover and the washing tower.
Preferably, the rotary kiln and the second combustion chamber are closely connected; the second combustion chamber is connected with an air inlet of the waste heat boiler through a first flue.
Preferably, the gas outlet of the waste heat boiler is connected with the quenching tower through a second flue;
the two-fluid spray head is arranged in the quenching tower, and the sprayed atomized liquid drops exchange heat with the flue gas entering the quenching tower to take away the heat of the flue gas.
Preferably, the dust collector is a bag collector.
Preferably, the bag filter comprises a filter body, an ash bucket connected to the bottom of the filter body, and a heating mechanism arranged on the ash bucket.
Preferably, the waste heat boiler is provided with a conveying device which is connected with the denitration spray gun and used for conveying the reducing agent;
a high-temperature-resistant sleeve is sleeved on the denitration spray gun, and a hot air cooling ring chamber is formed between the sleeve and the periphery of the denitration spray gun.
Preferably, the rotary kiln flue gas treatment system further comprises an air heater between the dust remover and the washing tower, and the air heater heats air by using the heat of the recovered flue gas and uses the heated air as combustion-supporting air of the rotary kiln;
the hot air ring chamber is connected with the air heater.
Preferably, the outlet of the dust remover is connected with the air heater through a third flue, and the air heater is connected with the washing tower through a fourth flue; one end of the shunting flue is connected with the outlet of the dust remover, and the other end of the shunting flue is connected with the washing tower or the fourth flue.
Preferably, the rotary kiln flue gas treatment system further comprises a flue gas heater; the first heat exchange channel of the flue gas heater is connected between the air heater and the washing tower, and flue gas output by the air heater enters the washing tower through the first heat exchange channel;
and the second heat exchange channel of the flue gas heater is connected with the wet deacidification tower, and the flue gas output by the wet deacidification tower enters the second heat exchange channel and exchanges heat with the flue gas in the first heat exchange channel.
Preferably, the rotary kiln flue gas treatment system further comprises a gas distribution cylinder; the steam distributing cylinder is connected with a steam outlet of the waste heat boiler and receives steam from the waste heat boiler.
The utility model has the advantages that: the flue gas generated by burning the rotary kiln is treated to enable the flue gas to meet the emission requirement, wherein the flue gas heat group is used as a heat tracing heat source for conveying liquid waste through the diversion flue, so that the problem of blockage of the liquid waste feeding of the rotary kiln is solved, and the burning efficiency of the rotary kiln is improved.
Through set up hot-blast cooling ring type on exhaust-heat boiler's denitration spray gun, solve denitration spray gun high temperature deformation, the problem of jam etc. Through the arrangement of the flue gas heater, the treated flue gas is heated and then sent to the chimney, and the problem of 'white smoke' discharged by the flue gas is effectively solved on the premise of not using an external heat source.
Drawings
The invention will be further explained with reference to the drawings and examples, wherein:
fig. 1 is a connection block diagram of a rotary kiln flue gas treatment system according to an embodiment of the present invention.
Detailed Description
In order to clearly understand the technical features, objects, and effects of the present invention, embodiments of the present invention will be described in detail with reference to the accompanying drawings.
The utility model discloses a rotary kiln flue gas processing system for the flue gas that produces is burned to dangerous waste to the rotary kiln is handled, carries out heat recovery and gets rid of harmful substance etc. wherein to the flue gas.
As shown in fig. 1, the rotary kiln flue gas treatment system according to an embodiment of the present invention includes a rotary kiln 10, a second combustion chamber 20, a waste heat boiler 30, a quench tower 40, a dry deacidification tower 50, a dust remover 60, a scrubber 70, a wet deacidification tower 80, and an air heater 90, which are sequentially connected along a traveling direction of flue gas.
Wherein, the rotary kiln 10 is used for burning hazardous wastes and generating flue gas; the secondary combustion chamber 20 is connected with the rotary kiln 10 and receives the flue gas from the rotary kiln 10, and the flue gas is combusted again to form high-temperature flue gas. The exhaust-heat boiler 30 is connected to the second combustion chamber 20 and receives the high-temperature flue gas from the second combustion chamber 20, and is used for performing selective non-catalytic reduction reaction on the high-temperature flue gas, recovering heat of the high-temperature flue gas, and generating steam. The quenching tower 40 is connected to the exhaust-heat boiler 30 and receives the cooled flue gas from the exhaust-heat boiler 30, and is used for exchanging heat and cooling the cooled flue gas therein. The dry deacidification tower 50 is connected with the quenching tower 40 and receives the flue gas from the quenching tower 40, and performs adsorption purification treatment on the flue gas. The dust collector 60 is used for performing dust removal and filtration treatment on the flue gas after adsorption and purification treatment. The washing tower 70 is used for washing the flue gas after dust removal and filtration by weak alkaline washing liquid. The wet deacidification tower 80 is used for deacidifying the washed flue gas by strong alkali liquor. The air heater 90 is connected between the dust collector 60 and the washing tower 70, recovers heat of the dust-removed and filtered flue gas, heats air with the recovered heat of the flue gas, and uses the heated air as combustion air for the rotary kiln 10.
In this embodiment, the rotary kiln 10 and the second combustion chamber 20 are closely connected. The flue gas in the rotary kiln 10 is directly sent into the second combustion chamber 20 in a closed space without leakage.
The rotary kiln 10 includes a kiln head, a body, a kiln tail, a transmission mechanism, etc. The kiln head mainly has the function of smoothly feeding materials (such as hazardous wastes), and an auxiliary fuel/liquid waste combined burner is arranged inside the kiln head. The lower part of the kiln head is provided with a waste collector for collecting waste leakage. The body of the rotary kiln 10 is a cylinder rolled from steel plate and lined with refractory material. The body is provided with two belt wheels and a large gear ring, the transmission mechanism drives the large gear ring on the body through a small gear, and then the rotary kiln 10 body is driven to rotate through the large gear ring. The kiln tail is a transition body which is connected with the rotary kiln 10 body and the secondary combustion chamber 20, and the main function of the kiln tail is to ensure the sealing of the kiln tail and the conveying channel of the smoke and the incineration residue.
Hazardous waste generally includes liquid waste and solid waste; the solid waste is pushed into the rotary kiln 10 through a hydraulic push rod; the liquid waste is conveyed to the head of the rotary kiln 10 through a pipeline by a conveying pump and then is sent into the body of the rotary kiln 10. The flue gas generated by burning in the rotary kiln 10 is conveyed to the secondary combustion chamber 20 for secondary combustion treatment, and the burned residues are discharged from the bottom for further treatment.
The secondary combustion chamber 20 performs a secondary combustion treatment on the flue gas to decompose dioxin and other harmful components in the flue gas. The size of the second combustion chamber 20 is set to ensure that the residence time of the flue gas is more than 2s at the temperature of over 1100 ℃; under this condition, 99.99% of dioxin and other harmful components in the flue gas can be decomposed. The lower part of the second combustion chamber 20 is provided with a required number of multifunctional burners, so that the temperature of the flue gas in the second combustion chamber 20 can meet the requirement, and the flue gas can be fully disturbed. The second combustion chamber 20 can be provided with a thermocouple to control the firepower of the multifunctional burner, so that the temperature of the second combustion chamber 20 is stabilized at a set value.
Before the smoke is subjected to the secondary combustion treatment, liquid waste is also input into the secondary combustion chamber 20. The liquid waste is conveyed to the multifunctional burner of the second combustion chamber 20 through a pipeline by a conveying pump and then enters the second combustion chamber 20. The rotary kiln 10 and the secondary combustion chamber 20 are respectively provided with an air inlet for respectively feeding combustion-supporting air.
Alternatively, the inner wall of the second combustion chamber 20 is a fire-resistant layer, and the outer wall is a heat-insulating layer and an outer protection plate in sequence. The internal working temperature of the second combustion chamber 20 is more than 1100 ℃, and the external surface temperature is less than or equal to 60 ℃.
The second combustion chamber 20 is connected to an air inlet of the waste heat boiler 30 through a first flue 21, and conveys high-temperature flue gas formed after re-combustion to the waste heat boiler 30 for selective non-catalytic reduction (SNCR). In the exhaust-heat boiler 30, reducing agents such as urea solution and the like react with nitrogen oxides in the high-temperature flue gas, so that the aim of removing the nitrogen oxides in the flue gas is fulfilled. Through SNCR, the heat of high temperature flue gas is retrieved by exhaust-heat boiler 30, can produce a large amount of steam, and the steam that produces can supply the inside and other users in factory of production line to use, avoids flue gas calorific loss.
Specifically, urea solution is uniformly sprayed on the water-cooled wall in the range of 900-1050 ℃ of the flue gas temperature in the waste heat boiler 30. Preferably, a high-pressure micron spraying denitration process is adopted, the urea solution is pressurized and conveyed through a pressurized conveying metering device, the conveying pressure can reach 10Mpa, so that the dominant kinetic energy is generated, the penetration rigidity of the reducing agent spraying is greatly improved, the areas of the flue gas and the urea solution are increased, and the denitration efficiency is improved.
The pressurizing conveying metering device comprises a precision filter, a high-pressure atomizing pump, a variable frequency motor, a regulating valve, an electromagnetic flowmeter, a pressure transmitter and the like. Metering device's urea pipeline is carried in pressurization and is connected with the denitration spray gun, because denitration spray gun operational environment is comparatively abominable, is in exhaust-heat boiler 30's high-temperature region, consequently for preventing that the denitration spray gun stretches into the furnace wall inside part can appear warping in the high-temperature region and lead to the spray gun jam or can't extract, the utility model discloses in, establish high temperature resistant sleeve pipe for the cover on the denitration spray gun, form a hot-blast cooling ring room between the periphery of sleeve pipe and denitration spray gun, hot-blast ring room is connected with air heater 90. Through introducing hot air (the temperature is about 160 ℃) generated by the air heater 90 into the hot air cooling ring chamber, the working temperature of the denitration spray gun is reduced, the denitration spray gun is protected, and low-temperature corrosion of acid under low load can be avoided. By the measures, the temperature of the working area of the denitration spray gun is about 400-500 ℃ under normal load, and the long-time continuous operation of the spray gun can be effectively ensured.
To the steam that exhaust-heat boiler 30 produced, the utility model discloses a rotary kiln flue gas processing system still can include steam-distributing cylinder 110, exhaust-heat boiler 30's steam outlet connection steam-distributing cylinder 110 to carry steam wherein to steam-distributing cylinder 110, carry other required places such as production line by steam-distributing cylinder 110 again.
After the high-temperature flue gas is treated by the waste heat boiler 30, the temperature can be reduced to 550 ℃ or below. An air outlet of the waste heat boiler 30 is connected with the quenching tower 40 through a second flue 31, and the flue gas is output from the air outlet of the waste heat boiler 30 and is conveyed to the quenching tower 40 through the second flue 31.
Flue gas enters the quench tower 40 primarily from above it. The two-fluid nozzle is arranged in the quenching tower 40, and the sprayed atomized liquid drops exchange heat with the flue gas entering the quenching tower 40 to take away the heat of the flue gas. Under the action of compressed air, the compressed air and cooling liquid (water) are beaten for a plurality of times in the spray head, the cooling liquid is atomized into liquid drops about 0.08mm, the atomized liquid drops exchange heat with high-temperature flue gas fully, the liquid drops are evaporated rapidly in a short time, heat is taken away, the temperature of the flue gas is instantly reduced to below 200 ℃, and the water content (mass ratio) is less than 3%. Because the residence time of the flue gas between 200 ℃ and 500 ℃ is less than 1s, the resynthesis of dioxin is prevented. A portion of the fly ash removed from the flue gas in the quench tower 40 is removed from the bottom of the quench tower 40 for collection and disposal.
Because the quenching tower 40 adopts a double-fluid nozzle, atomized particles of the cooling liquid are very fine, the total evaporation surface area of liquid drops is large, the evaporation time is short, 100 percent evaporation is ensured, and the bottom is not wet.
The quenched flue gas is conveyed from the quenching tower 40 to the dry deacidification tower 50 to be subjected to adsorption purification treatment. In order to meet the emission standard of waste incineration flue gas and ensure the emission standard of heavy metals (especially Hg), dioxin and furan, an auxiliary purification measure of activated carbon jet adsorption is usually adopted in a dry deacidification tower except that the incineration process and technical parameters are strictly controlled. Because the activated carbon has extremely large specific surface area, even a small amount of activated carbon can achieve high adsorption and purification efficiency as long as the activated carbon is uniformly mixed with the flue gas and the contact time is long enough.
The flue gas enters a dry-method deacidification tower 50 to be fully contacted with the mixed powder of hydrated lime, activated carbon and fly ash sprayed into the tower, and the flue gas reacts to form dust-shaped calcium salt, so that the aim of removing sulfur dioxide, hydrogen chloride and other acidic gases in the flue gas is fulfilled. The water content in the flue gas is Ca (OH)2Liquid phase ion reaction occurs between the particle surface and the acid gas, and the deacidification efficiency and the utilization rate of the absorbent are obviously improved.
The dust-containing flue gas output from the dry deacidification tower 50 is then conveyed to a dust remover 60 for dust removal and filtration. In this embodiment, the dust collector 60 is preferably a bag collector. The bag type dust collector comprises a dust collector body, an ash bucket connected to the bottom of the dust collector body, and a heating mechanism arranged on the ash bucket.
The dust-containing flue gas is sent into the bag type dust collector, is uniformly distributed through a guide plate in the bag type dust collector and enters each air chamber through an air inlet adjusting valve, coarse dust particles in the flue gas are settled to the bottom of the dust hopper, fine dust particles are turned upwards along with the air flow and enter a filter chamber, the dust is blocked on the surface of the filter bag, and the purified gas enters the cleaning chamber through the opening of the filter bag and is discharged from an air outlet.
With the operation of the bag type dust collector, dust and particles contained in the flue gas form filter cakes on the outer side surface of the filter bag due to inertial impact, direct interception, diffusion, electrostatic attraction and the like. When the system resistance is larger than a set value, pulse blowing is started to remove ash; the time setting and the pressure difference setting are simultaneously effective, and the ash removal is carried out by taking time as a main principle and adopting a pressure difference priority principle. Chloride in flue gas generated by burning hazardous wastes has strong water absorption, so a heating mechanism such as electric heating is added on an ash bucket of the bag type dust collector, the phenomena of acid condensation, ash bridging and hardening are avoided, and the temperature of the outer surface is ensured to be less than 60 ℃. The filter bag is made of high-efficiency polytetrafluoroethylene membrane filter material.
The outlet of the dust remover 60 is connected with the air heater 90 through the third flue 61, and the air heater 90 is connected with the washing tower 70 through the fourth flue 91, so that the flue gas output by the dust remover 60 firstly passes through the air heater 90 and then enters the washing tower 70. Since the flue gas output from the dust collector 60 has a certain temperature (high-temperature flue gas), it enters the air heater 90 as a heating source of the air heater 90, and exchanges heat with other media passing through the air heater 90 in the air heater 90. For example, the combustion-supporting air for the rotary kiln 10 passes through the air heater 90, is subjected to heat exchange with the flue gas in the air heater 90, is heated, and is then conveyed into the rotary kiln 10, so that the inlet air temperature of the rotary kiln 10 can be increased. The flue gas is cooled after heat exchange in the air heater 90 and then sent into the washing tower 70, so that the heat is recycled.
Particularly, the utility model also comprises a diversion flue 62 which is connected between the dust remover 60 and the washing tower 70 and is connected with the air heater 90 in parallel; the split flue 62 is used for flue gas passage and as a heat tracing source for liquid waste transport of hazardous waste.
Specifically, in the present embodiment, in addition, one end of the diversion flue 62 is connected to the outlet of the dust remover 60, and the other end is connected to the washing tower 70 or the fourth flue 91. The diversion flue 62 is provided with an openable flap 63 to close the flap 63 when heating of the liquid waste is not required.
The flue gas passes through an air heater 90 and enters the scrubber 70.
Optionally, two layers of weak alkaline washing liquid are arranged on the top of the washing tower 70, after dust in the flue gas is mixed with the weak alkaline washing liquid, a part of the flue gas and the weak alkaline washing liquid enter the bottom of the washing tower 70, and simultaneously, the temperature of the flue gas is reduced from 170 ℃ to about 90 ℃ and HCl, HF and SO in part of the flue gas are removed2(ii) a Weak alkaline washing liquid at the bottom of the washing tower 70 is pumped to the top of the washing tower 70 through a pump to continuously wash the flue gas.
After the washing is completed, the flue gas enters the wet deacidification tower 80 from the washing tower 70 for deacidification treatment. The wet deacidification tower 80 uses strong alkali solution such as NaOH solution to remove HCl, HF and SO in the flue gas2. In the rising process, the flue gas is mixed with NaOH solution sprayed from a spraying device at the upper part in the tower for contact reaction. The NaOH solution has strong alkalinity, SO the method can treat HCl, HF and SO in the flue gas2The removal rate of the catalyst is higher.
The wet deacidification tower 80 is internally provided with three layers of spraying devices, each spraying device consists of a spraying pipeline and a nozzle, the arrangement of the nozzles on each layer ensures that the section of the spraying liquid in the range of the spraying effective distance has no dead angle, the whole spraying coverage rate is more than 300 percent, the optimal contact area and mode are achieved, and the dissolution and reaction are fully absorbed. The purified flue gas rises to enter a demister in the wet-type deacidification tower 80, the demister is a baffle demister, the whole set of device comprises two layers of demisters and corresponding three layers of washing water devices, and the device is used for ensuring that the moisture content of the flue gas output by the wet-type deacidification tower 80 is not more than 75mg/Nm3. The inner wall of the wet deacidification tower 80 is used for glass flake corrosion prevention, so that the safety and the reliability of equipment are improvedAnd the operation period is prolonged.
The wastewater generated by the washing tower 70 and the wet deacidification tower 80 enters a wastewater treatment plant for treatment.
The temperature of the flue gas output by the wet deacidification tower 80 is about 60 ℃, and the output flue gas can be conveyed to a chimney 120 for discharge.
Furthermore, in order to avoid the occurrence of "white smoke" at the outlet of the chimney 120, the flue gas treatment system of the rotary kiln of the present invention further comprises a flue gas heater 100; the flue gas heater 100 is connected between the wet type deacidification tower 80 and the chimney 120, and the purified flue gas (for short, clean flue gas) output by the wet type deacidification tower 80 is heated by the flue gas heater 100, enters the chimney 120 and is discharged from the chimney 120.
In addition, the flue gas heater 100 is also connected between the air heater 90 and the washing tower 70, and is used for the flue gas output by the air heater 90 to pass through, and the heat of the passing flue gas is used as a heat source to heat the clean flue gas, so that external steam supply is not needed, and the economic efficiency is improved.
Specifically, the flue gas heater 100 has a first heat exchange channel and a second heat exchange channel; the first heat exchange channel is located on the tube side of the flue gas heater 100 and the second heat exchange channel is located on the shell side of the flue gas heater 100. The first heat exchange path is connected between the air heater 90 and the scrubber tower 70, and the second heat exchange path is connected between the wet deacidification tower 80 and the stack 120. The flue gas output by the air heater 90 enters the washing tower 70 through the first heat exchange channel; the flue gas output by the wet deacidification tower 80 enters the second heat exchange channel and exchanges heat with the flue gas in the first heat exchange channel, so that the clean flue gas is heated.
The heated clean flue gas is exhausted from the stack 120 under the drive of the fan 121.
In addition, in order to solve the corrosion problem of the flue gas heater 100, the flue gas heater 100 can be made of fluoroplastic steel, which is different from conventional stainless steel, and is not easy to corrode and has a long service life.
The above only is the embodiment of the present invention, not limiting the patent scope of the present invention, all the equivalent structures or equivalent processes that are used in the specification and the attached drawings or directly or indirectly applied to other related technical fields are included in the patent protection scope of the present invention.
Claims (10)
1. A rotary kiln flue gas treatment system is characterized by comprising a rotary kiln for burning hazardous wastes and generating flue gas, a secondary combustion chamber for carrying out secondary combustion treatment on the flue gas to form high-temperature flue gas, a waste heat boiler for cooling the high-temperature flue gas to generate steam and carrying out SNCR denitration in the steam, a quench tower for exchanging heat and cooling the cooled flue gas again, a dry deacidification tower for carrying out adsorption purification treatment on the flue gas, a dust remover for carrying out dust removal filtration treatment on the flue gas after the adsorption purification treatment, a washing tower for washing the flue gas after the dust removal filtration by weak alkaline washing liquid, a wet deacidification tower for carrying out deacidification treatment on the washed flue gas by strong alkaline liquid, and a diversion flue of a heat tracing heat source for conveying the liquid wastes as the hazardous wastes after the flue gas passes through the diversion flue gas;
the rotary kiln, the secondary combustion chamber, the waste heat boiler, the quench tower, the dry deacidification tower, the dust remover, the washing tower and the wet deacidification tower are sequentially connected along the advancing direction of the flue gas; the split-flow flue is connected between the dust remover and the washing tower.
2. The rotary kiln flue gas treatment system as claimed in claim 1, wherein the rotary kiln and the secondary combustion chamber are closely adjacent to each other; the second combustion chamber is connected with an air inlet of the waste heat boiler through a first flue.
3. The rotary kiln flue gas treatment system as claimed in claim 1, wherein the exhaust-heat boiler is connected with the quenching tower through a second flue at the outlet thereof;
the two-fluid spray head is arranged in the quenching tower, and the sprayed atomized liquid drops exchange heat with the flue gas entering the quenching tower to take away the heat of the flue gas.
4. The rotary kiln flue gas treatment system of claim 1, wherein the dust collector is a bag filter.
5. The rotary kiln flue gas treatment system according to claim 4, wherein the bag filter comprises a filter body, an ash hopper connected to the bottom of the filter body, and a heating mechanism arranged on the ash hopper.
6. The rotary kiln flue gas treatment system according to any one of claims 1 to 5, wherein the exhaust-heat boiler is provided with a conveying device which is connected with the denitration spray gun and used for conveying a reducing agent;
a high-temperature-resistant sleeve is sleeved on the denitration spray gun, and a hot air cooling ring chamber is formed between the sleeve and the periphery of the denitration spray gun.
7. The rotary kiln flue gas treatment system according to claim 6, further comprising an air heater between the dust remover and the scrubber, wherein the air heater heats air by using heat of the recovered flue gas as combustion-supporting air of the rotary kiln;
the hot air cooling ring chamber is connected with the air heater.
8. The rotary kiln flue gas treatment system as claimed in claim 7, wherein the outlet of the deduster is connected with the air heater through a third flue, and the air heater is connected with the scrubbing tower through a fourth flue; one end of the shunting flue is connected with the outlet of the dust remover, and the other end of the shunting flue is connected with the washing tower or the fourth flue.
9. The rotary kiln flue gas treatment system as claimed in claim 7, further comprising a flue gas heater; the first heat exchange channel of the flue gas heater is connected between the air heater and the washing tower, and flue gas output by the air heater enters the washing tower through the first heat exchange channel;
and the second heat exchange channel of the flue gas heater is connected with the wet deacidification tower, and the flue gas output by the wet deacidification tower enters the second heat exchange channel and exchanges heat with the flue gas in the first heat exchange channel.
10. The rotary kiln flue gas treatment system according to any one of claims 1 to 5, further comprising a gas separation cylinder; the steam distributing cylinder is connected with a steam outlet of the waste heat boiler and receives steam from the waste heat boiler.
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| CN202022788621.4U CN213956022U (en) | 2020-11-26 | 2020-11-26 | Rotary kiln flue gas treatment system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114177761A (en) * | 2022-02-16 | 2022-03-15 | 浙江百能科技有限公司 | Ultralow emission system and method for hazardous waste incineration flue gas pollutants |
| CN114177760A (en) * | 2022-02-16 | 2022-03-15 | 浙江百能科技有限公司 | System and method for oxidizing active oxygen in hazardous waste incineration flue gas and integrally discharging hazardous waste incineration flue gas in ultralow emission mode |
-
2020
- 2020-11-26 CN CN202022788621.4U patent/CN213956022U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114177761A (en) * | 2022-02-16 | 2022-03-15 | 浙江百能科技有限公司 | Ultralow emission system and method for hazardous waste incineration flue gas pollutants |
| CN114177760A (en) * | 2022-02-16 | 2022-03-15 | 浙江百能科技有限公司 | System and method for oxidizing active oxygen in hazardous waste incineration flue gas and integrally discharging hazardous waste incineration flue gas in ultralow emission mode |
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