CN211345334U - Purification system for hazardous waste incineration flue gas - Google Patents
Purification system for hazardous waste incineration flue gas Download PDFInfo
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- CN211345334U CN211345334U CN201922027363.5U CN201922027363U CN211345334U CN 211345334 U CN211345334 U CN 211345334U CN 201922027363 U CN201922027363 U CN 201922027363U CN 211345334 U CN211345334 U CN 211345334U
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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
Abstract
The utility model discloses a danger is useless burns flue gas purification system, include: the inlet of the waste heat boiler is connected with a flue gas source, the waste heat boiler is internally provided with a superheater, and the outlet end of the waste heat boiler is provided with a coal economizer; the semidry desulfurization tower is connected to the outlet end of the waste heat boiler and is provided with a spraying layer, and the spraying layer is connected with a lime water source; the dust remover is connected to the downstream of the semi-dry desulfurization tower; the heat exchanger is internally provided with a first channel and a second channel, the second channel surrounds the outer side of the first channel, the inlet of the first channel is connected with the superheater, and the inlet of the second channel is connected with the gas outlet of the dust remover; a flue gas inlet of the denitration tower is connected with an outlet of the second channel; and the chimney is connected with the flue gas outlet of the denitration tower through the induced draft fan. The flue gas purification system has the advantages of simple structure, low cost, high purification efficiency, full utilization of flue gas sensible heat, reduction of water resource usage and ultralow emission of nitrogen oxides in hazardous waste incineration flue gas.
Description
Technical Field
The utility model belongs to the technical field of the environmental protection, concretely relates to danger is useless burns flue gas purification system.
Background
The information disclosed in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be taken as an acknowledgement or any form of suggestion that this information constitutes prior art that is already known to a person skilled in the art.
At present, a hazardous waste incineration flue gas purification system basically adopts a flue gas combined treatment process, a quench tower is adopted to spray water and quench the flue gas for cooling, the dioxin is prevented from being resynthesized, activated carbon is used for spraying and adsorbing the dioxin, a bag type dust collector is used for removing dust, and finally wet desulphurization is adopted. The combined process has some inevitable defects in the technology, the quenching tower is adopted for water spraying and quenching to reduce the temperature of the flue gas from 500 ℃ to 200 ℃, the cooling speed is less than 1s, and the sensible heat of the flue gas is not utilized in the cooling process, so that a great deal of energy is wasted; the water spray quenching causes the increase of the moisture of the flue gas, and increases the bag pasting possibility of the bag-type dust remover, the white feather phenomenon of the flue gas and the corrosion of equipment; along with the more and more strict national regulation on environmental protection, the emission standard of domestic hazardous waste incineration tail gas is developed towards the trend of ultralow emission, a matched SCR denitration process technical measure is needed in the process flow, the flue gas temperature after conventional purification is difficult to meet the SCR denitration temperature requirement, and the denitration effect is influenced.
Disclosure of Invention
To the technical problem who exists among the above prior art, the utility model aims at providing a useless flue gas purification system that burns of danger. The flue gas purification system has the advantages of simple structure, low cost, high purification efficiency, full utilization of flue gas sensible heat, reduction of water resource usage and ultralow emission of nitrogen oxides in hazardous waste incineration flue gas.
In order to solve the technical problem, the technical scheme of the utility model is that:
a dangerous waste incineration flue gas purification system comprises:
the inlet of the waste heat boiler is connected with a flue gas source, the waste heat boiler is internally provided with a superheater, and the outlet end of the waste heat boiler is provided with a coal economizer;
the semidry desulfurization tower is connected to the outlet end of the waste heat boiler and is provided with a spraying layer, and the spraying layer is connected with a lime water source;
the dust remover is connected to the downstream of the semi-dry desulfurization tower;
the heat exchanger is internally provided with a first channel and a second channel, the second channel surrounds the outer side of the first channel, the inlet of the first channel is connected with the superheater, and the inlet of the second channel is connected with the gas outlet of the dust remover;
a flue gas inlet of the denitration tower is connected with an outlet of the second channel;
and the chimney is connected with the flue gas outlet of the denitration tower through the induced draft fan.
In some embodiments, the flue gas heat exchanger is further included, and the hot medium channel is a flue gas channel, and the cold medium channel is a cold water channel.
Further, an outlet of the cold medium channel is connected with a waste heat boiler.
The boiler feed water exchanges heat with the flue gas in the flue gas heat exchanger for preheating, so that the temperature of the boiler feed water can be increased, and the temperature of the hot water or the flow of the hot water can be increased when heat recovery is carried out in the waste heat boiler.
In some embodiments, an atomizing spray head is arranged downstream of the economizer and is connected with a cold water source.
In some embodiments, the outer side of the side wall between the first channel and the second channel of the heat exchanger is provided with fins.
The heat exchange area can be increased by the arrangement of the fins, and the heat exchange effect is further improved.
Further, the first channel and the second channel are serpentine channels. On the premise of ensuring the heat exchange effect, the volume of the heat exchanger can be reduced.
In some embodiments, an activated carbon injection device is arranged on the flue gas pipeline between the semi-dry desulfurization tower and the dust remover, and the activated carbon injection device is connected with an activated carbon source. The dioxin in the flue gas exists in a granular state, an aerosol state or a gaseous state, and the dioxin in the solid state and the gaseous state can be adsorbed simultaneously by utilizing the huge surface area and the good adsorbability of the activated carbon, and then most of the dioxin in the flue gas can be removed by cloth bag dust removal interception.
In some embodiments, the denitration tower is an SCR denitration tower.
The utility model has the advantages that:
the useless incineration flue gas of danger carries out the heat transfer cooling with the water in the boiler in exhaust-heat boiler, and simultaneously, the saturated steam heating in the high temperature flue gas will the over heater generates superheated steam, and superheated steam can heat with the lower flue gas of temperature through the pipeline flow direction heat exchanger in, with the flue gas heating to the suitable temperature of denitration to improve the denitration effect of flue gas. Because the heat source of the flue gas is superheated steam from the superheater, a large amount of energy consumption can be saved.
The economizer is arranged at the outlet end of the waste heat boiler and is used for rapidly cooling the flue gas, so that the time for cooling the flue gas from 500 ℃ to 180 ℃ is shorter than 1s, the regeneration of dioxin can be effectively inhibited, and the content of the dioxin in the flue gas is reduced; the coolant in the economizer is boiler feed water and is not directly contacted with the flue gas, so that sensible heat in the flue gas is fully utilized, the boiler feed water temperature is increased, the steam yield in the system can be increased, and secondary waste or pollutants generated in the waste gas treatment process are effectively avoided.
Drawings
The accompanying drawings, which form a part of the specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without unduly limiting the scope of the invention.
Fig. 1 is the utility model discloses danger is useless burns flue gas treatment process flow chart.
The system comprises a waste heat boiler 1, a superheater 2, an economizer 3, a semi-dry desulfurization tower 4, an activated carbon injection device 5, a bag-type dust remover 6, a flue gas fin heater 7, an SCR denitration tower 8, a flue gas heat exchanger 9, an induced draft fan 10 and a chimney 11.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments in accordance with the invention. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
As shown in fig. 1, a hazardous waste incineration flue gas purification system comprises a waste heat boiler 1, a superheater 2, a connecting economizer 3, a semidry desulfurization tower 4, an activated carbon injection device 5, a bag-type dust remover 6, a flue gas fin heater 7, an SCR denitration system 8, a flue gas heat exchanger 9, an induced draft fan 10 and a chimney 11 which are connected in sequence;
the waste heat boiler 1 is characterized in that a superheater 2 is arranged in a hearth, the superheater 2 is used for heating part of boiler outlet saturated steam, and the heated saturated steam is changed into superheated steam; the superheated steam can be used for heating the flue gas from the flue gas outlet of the bag-type dust collector 6 to meet the requirement of a subsequent SCR denitration system 8 on the temperature of the flue gas, the heat of the flue gas is utilized in the process, an external heat source is not required to be introduced, the superheated steam is changed into saturated steam after heating the flue gas, and the saturated steam can be merged into a steam system again, so that the structure is compact, and the energy is saved;
the quenching section-economizer 3 is connected to the outlet flue of the waste heat boiler 1 and has the function of rapidly cooling the flue gas, so that the time for cooling the flue gas from 500 ℃ to 180 ℃ is shorter than 1s, the regeneration of dioxin can be effectively inhibited, and the content of the dioxin in the flue gas is reduced; compared with the traditional quench tower, the economizer 3 has obvious advantages, wherein the refrigerant in the economizer is boiler feed water and is not directly contacted with the flue gas, so that sensible heat in the flue gas is fully utilized, the boiler feed water temperature is raised, the steam yield in the system can be increased, and secondary waste or pollutants generated in the waste gas treatment process are effectively avoided; the economizer 3 is provided with a high-temperature flue gas inlet end and a low-temperature flue gas outlet end, the high-temperature flue gas inlet end is connected with the exhaust port of the waste heat boiler 1, the waste heat boiler 1 is provided with a superheater 2, and the low-temperature flue gas outlet end is connected with the semi-dry desulfurization tower 4.
The cross section of the economizer 3 is designed to ensure that the numerical value of the flue gas flow velocity (m/s) per second is larger than the numerical value of the actual circulation length (m) of the quenching section, the flue gas is reduced to 180 ℃ within 1s from 500 ℃, the generation of dioxin is avoided to the maximum extent, and a cold water atomizing nozzle is arranged at the low-temperature flue gas outlet end of the economizer 3 and serves as an emergency cooling standby device;
the economizer 2 is provided with an upper collecting box and a lower collecting box, softened water is provided by a boiler water feeding pump to be used as a refrigerant for quenching and cooling, temperature sensors are arranged at a flue gas inlet and a flue gas outlet to facilitate real-time monitoring and control of the flue gas temperature, the inlet temperature sensor monitors the flue gas temperature from a boiler, and the outlet temperature sensor monitors the flue gas temperature after quenching, so that system control is realized and the economizer is interlocked with an emergency cooling standby device;
the inlet end of the semidry desulfurization tower 4 is connected with the outlet of the economizer 3, and the outlet end of the semidry desulfurization tower is connected with the bag-type dust collector 6, so that the system can decompose oxysulfide in the flue gas and reduce the content of oxysulfide in the flue gas;
the semi-dry desulfurization tower 4 is added in a wet state, and water in the slurry is evaporated by utilizing the sensible heat of the flue gas. In the drying process, the desulfurizer reacts with oxysulfide in the flue gas to generate a dry powder product, and the bag-type dust remover is matched to ensure that the desulfurization efficiency reaches more than 98%.
The semi-dry desulfurization tower 4 is provided with a hot air distributor and a desulfurizer atomizer, the desulfurizer is quantitatively fed into the atomizer at the top of the desulfurization tower by a slurry pump according to the concentration of sulfur oxides in inlet flue gas, the slurry is atomized into droplets by the atomizer and sprayed from the top of the desulfurization tower, and the droplets are formed to contact with the flue gas in the tower and then undergo chemical reaction, so that the sulfur oxides in the flue gas are absorbed.
The activated carbon injection device 5 is arranged on a flue gas pipeline from a dry desulfurization system to bag-type dust removal, is an important process for treating dioxin and heavy metals in a flue gas purification system, and can remove most of the dioxin and heavy metals in the flue gas by matching with the bag-type dust removal device 6, so that the emission values of the dioxin and heavy metals are controlled within a standard allowable range. The dioxin in the flue gas exists in a granular state, an aerosol state or a gaseous state, and the dioxin in the solid state and the gaseous state can be adsorbed simultaneously by utilizing the huge surface area and the good adsorbability of the activated carbon, and then most of the dioxin in the flue gas can be removed by cloth bag dust removal interception. The activated carbon injection device 5 includes a storage unit, a conveying unit, and an injection unit, and different numbers of conveying units can be designed according to the needs.
The cloth bag dust collector 6 mainly utilizes filter materials (fabrics or felts) to filter dust-containing gas so as to achieve the purpose of dust removal. The inlet end is connected with the dry desulfurization outlet, and the outlet end is connected with the inlet of the flue gas fin heater. The device is provided with a flue gas inlet and outlet, an ash hopper, a filtering device, an ash removing device and the like.
The flue gas fin heater 7 is used for heating flue gas at the outlet of the bag-type dust collector 6 by using superheated steam (the superheated steam is from the superheated steam heated by a superheater in a boiler hearth), so that the flue gas temperature required by a subsequent SCR denitration system is provided, and the denitration effect is ensured; in the process, the superheated steam is changed into saturated steam and can be re-merged into the branch cylinder to meet the use requirement of the steam.
The flue gas fin heater 7 is in a gas-gas heat exchange mode, a core heat transfer component is composed of a spiral fin tube bundle, and the fin tube can be formed by winding a corrugated steel strip on a seamless steel tube and is spiral, so that the heat transfer area can be increased, and the heat transfer coefficient can be increased.
The SCR denitration tower 8 is connected with a flue gas outlet of the fin heater, and is used for reducing agent NH under the action of a low-temperature catalyst3Selective reduction of nitrogen oxides to N at a temperature2While almost no NH occurs3And O2Thereby realizing the aim of denitration; compared with the conventional catalyst, the low-temperature denitration catalyst has lower required working temperature and can complete the reaction at 220 ℃.
The core process of the SCR denitration tower 8 is catalytic reaction and is provided with NH3The nozzle and the powder ash blowing device are used, and the flue gas enters the SCR reactor loaded with the low-temperature catalyst along the flue. The catalyst is the key of the whole SCR denitration system, and the design and the selection of the catalyst are determined by the flue gas condition and the components.
After the hazardous waste is gasified by the gasification furnace and incinerated by the incinerator, the waste gas enters the waste heat boiler 1 for waste heat recovery to generate steam. The superheater 2 is arranged in the hearth of the waste heat boiler 1, and the flue gas in the hearth is used for heating the saturated steam generated by the waste heat boiler 1, so that the saturated steam is changed into superheated steam for a subsequent system (for heating the flue gas before denitration). A quenching section (economizer) 3 is arranged at the outlet of the boiler and used for cooling the flue gas, the temperature of the flue gas is quenched from 500 ℃ in 1s to 180 ℃, the dioxin can be effectively prevented from being resynthesized, and a cooling medium of the quenching section is boiler softened water which is subjected to heat exchange and temperature rise by the quenching section and then is supplied to the boiler; compared with the traditional quench tower, the process can fully utilize the heat energy of the flue gas, and is energy-saving and environment-friendly. A flue gas outlet of the quenching section is connected with a semi-dry desulfurization system 4, and sulfur oxides in the flue gas can be removed by the system; an active carbon injection device 5 is arranged at the flue gas outlet pipeline of the desulfurization system, and dioxin and heavy metal substances in the flue gas can be adsorbed by the device; the flue gas outlet pipeline of the semidry desulfurization system 4 is connected with a bag-type dust remover 6, and the bag-type dust remover 6 can remove small-particle fine dust, adsorb dioxin and heavy substances in flue gasActivated carbon behind metal species; at this point the flue gas passes through a desulfurization and dedusting system, and the temperature drops to about 160 ℃. The temperature can not meet the requirement of a subsequent SCR denitration system 8 on the temperature of the flue gas, so a flue gas fin heater 7 is arranged at the outlet of a bag-type dust remover and used for heating the flue gas to ensure that the temperature of the flue gas is raised to 220 ℃ and the requirement of denitration on the temperature of the flue gas is met, a heat source of a heat exchanger is superheated steam generated after being heated by a superheater 2 in a waste heat boiler hearth, the superheated steam is cooled and becomes saturated steam, and the saturated steam can be merged into a branch cylinder and enters a steam supply system; the flue gas enters an SCR denitration system 8 after being heated, and a reducing agent NH is added under the action of a low-temperature catalyst3Selectively chemically reacting with nitrogen oxide at 220 deg.C to obtain NH3Itself hardly reacts with O2Reaction is carried out, thereby realizing the aim of flue gas denitration. At the moment, the flue gas is changed into clean gas after dust removal, desulfurization and denitration, but the temperature is still 220 ℃, and partial sensible heat is not utilized, so that a flue gas heat exchanger 9 is arranged at a flue gas outlet of the SCR denitration system 7, and the purpose is to fully utilize the sensible heat of the flue gas; the refrigerant of the flue gas heat exchanger 9 is softened boiler feed water, so that the temperature of the boiler feed water is increased, the temperature of flue gas is reduced, and energy conservation and emission reduction are realized; at the moment, the temperature of the flue gas is reduced to 150 ℃, and then the flue gas is pressurized by the induced draft fan 10 and discharged to the atmosphere through the chimney 11.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. The utility model provides a useless incineration flue gas clean system of danger which characterized in that: the method comprises the following steps:
the inlet of the waste heat boiler is connected with a flue gas source, the waste heat boiler is internally provided with a superheater, and the outlet end of the waste heat boiler is provided with a coal economizer;
the semidry desulfurization tower is connected to the outlet end of the waste heat boiler and is provided with a spraying layer, and the spraying layer is connected with a lime water source;
the dust remover is connected to the downstream of the semi-dry desulfurization tower;
the heat exchanger is internally provided with a first channel and a second channel, the second channel surrounds the outer side of the first channel, the inlet of the first channel is connected with the superheater, and the inlet of the second channel is connected with the gas outlet of the dust remover;
a flue gas inlet of the denitration tower is connected with an outlet of the second channel;
and the chimney is connected with the flue gas outlet of the denitration tower through the induced draft fan.
2. The hazardous waste incineration flue gas purification system of claim 1, characterized in that: the heat exchange device also comprises a flue gas heat exchanger, wherein the hot medium channel is a flue gas channel, and the cold medium channel is a cold water channel.
3. The hazardous waste incineration flue gas purification system of claim 2, characterized in that: and the outlet of the cold medium channel is connected with a waste heat boiler.
4. The hazardous waste incineration flue gas purification system of claim 1, characterized in that: and an atomizing nozzle is arranged at the downstream of the economizer and is connected with a cold water source.
5. The hazardous waste incineration flue gas purification system of claim 1, characterized in that: fins are arranged on the outer side of the side wall between the first channel and the second channel of the heat exchanger.
6. The hazardous waste incineration flue gas purification system of claim 5, characterized in that: the first and second channels are serpentine channels.
7. The hazardous waste incineration flue gas purification system of claim 1, characterized in that: and a spray head is arranged on a flue gas pipeline between the semi-dry desulfurization tower and the dust remover, and the spray head is connected with an active carbon source.
8. The hazardous waste incineration flue gas purification system of claim 1, characterized in that: the denitration tower is an SCR denitration tower.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201922027363.5U CN211345334U (en) | 2019-11-19 | 2019-11-19 | Purification system for hazardous waste incineration flue gas |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201922027363.5U CN211345334U (en) | 2019-11-19 | 2019-11-19 | Purification system for hazardous waste incineration flue gas |
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| CN211345334U true CN211345334U (en) | 2020-08-25 |
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