CN115212694B - Method and device for treating fly ash plasma fusion flue gas - Google Patents
Method and device for treating fly ash plasma fusion flue gas Download PDFInfo
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- CN115212694B CN115212694B CN202210860951.0A CN202210860951A CN115212694B CN 115212694 B CN115212694 B CN 115212694B CN 202210860951 A CN202210860951 A CN 202210860951A CN 115212694 B CN115212694 B CN 115212694B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/12—Preparation of double sulfates of magnesium with sodium or potassium
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/06—Contaminated groundwater or leachate
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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
- Y02E20/12—Heat utilisation in combustion or incineration of waste
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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 application discloses a method and a device for treating fly ash plasma melting smoke, which are used for treating smoke generated in plasma melting household garbage, and the method comprises the following steps: s1: exchanging heat between the flue gas and air through a high-temperature gas-phase heat exchanger; s2: carrying out heat transfer and mass transfer dust removal on the flue gas and the landfill leachate by a multistage mass transfer dust removal unit; s3: washing the flue gas by alkali liquor through an alkali washing tower to remove sulfur dioxide; s4: and removing dioxin and dust in the flue gas through a filtering and adsorbing unit and discharging. The fly ash plasma melting flue gas treatment method is used for treating the flue gas landfill leachate through cooperative treatment. The landfill leachate is further subjected to heat transfer concentration by combining with direct contact of hot air so as to treat the landfill leachate.
Description
Technical Field
The application belongs to the garbage incineration treatment technology, and particularly relates to a fly ash plasma melting flue gas treatment method and device.
Background
At present, incineration power generation has become one of the main treatment modes of household garbage, and the garbage incineration power generation process can be summarized by 'one inlet and four outlets', wherein the four outlets refer to slag, fly ash, percolate and flue gas. At present, the flue gas strictly executes national relevant standards and can be discharged up to the standard. The slag can be used as brick making or building material for comprehensive utilization. Considering the grate furnace of the domestic main stream, the fly ash production amount is about 3% -5% of the incoming garbage amount, and the main process is chelating landfill at present, so that a large amount of land resources are occupied, and the risk of secondary pollution is also caused. After the percolate is treated, about 20% -40% of concentrated solution is produced for pulping or back spraying, which can cause equipment corrosion and affect the service life of the equipment.
For the waste incineration fly ash, high-temperature plasma melting is one of the ultimate treatment means. As a technical means of high-temperature treatment, the plasma melting can realize harmless treatment of the fly ash of the incineration of the household garbage. When plasma melting treatment is carried out, volatile heavy metal components, low-melting salts (mainly alkali metal chlorides) and generated acid gases (mainly hydrogen chloride and sulfur dioxide) in the fly ash can volatilize into flue gas because the temperature of a plasma center is above 1500 ℃, and meanwhile, the flue gas can carry part of the unreacted and complete fly ash into a flue gas treatment system, so that certain secondary fly ash is generated. The secondary fly ash has high salt content and contains a large amount of heavy metals and dioxins, belongs to dangerous wastes, and generally needs to be buried, so that on one hand, the cost of the whole fly ash plasma melting process is increased, the popularization is not facilitated, and on the other hand, the thorough harmless and recycling of the fly ash cannot be realized. The landfill leachate concentrated solution is generally used for pulping or processing in a back spraying furnace in a landfill at present, so that corrosion of equipment in a landfill system can be aggravated, and the service life of the equipment is influenced.
CN 107998827A discloses a high-temperature acid-containing flue gas hydrogen chloride recovery system, which relates to the field of acid-containing flue gas recycling treatment. The high-temperature acid-containing flue gas is treated by the dynamic wave scrubber, the water washing tower and the alkali liquor tower in sequence and then is directly discharged; one side of the bottom of the dynamic wave washing tower is sequentially connected with a filter and a first reboiler through a delivery pump, the outlet end of the first reboiler is connected with a hydrochloric acid analysis tower, the conveying pump is used for conveying the high-temperature mixed wastewater containing hydrogen chloride and heavy metal salt at the bottom of the power washing tower into the hydrochloric acid desorption tower, and then flash evaporation is carried out through a first reboiler connected at the bottom of the hydrochloric acid desorption tower, so that the hydrogen chloride in the mixed solution is changed into gas to be separated out. According to the application, after the flue gas is washed, hydrochloric acid is resolved on the washing liquid to recover the hydrogen chloride gas from the flue gas, but the process chain is complex and lengthy, a large amount of 3-8 ℃ of chilled water is needed, a large amount of energy sources are consumed for refrigeration, and the energy consumption cost is high; in addition, because the heavy metal components and alkali metal salt components in the washing liquid cannot be controlled and separated, salt wall formation, sludge blockage and other conditions are easy to occur, so that the process is unstable and even crashed, and the waste of resources is also caused.
CN 106994284A discloses a process for purifying tail gas of melting fly ash, the tail gas of the melting fly ash is cooled to below 100 ℃ by a quenching device, then enters a crystal nucleus aggregation chamber, heavy metal chloride in the tail gas forms large-particle-size particles under the action of low-frequency sound waves to be separated out, the heavy metal chloride-removed tail gas is separated out by a two-phase separation device, HCl gas is continuously removed by a graphite falling film absorption tower, residual acid gas is removed by an acid gas washing tower, and finally clean tail gas emission is obtained. The heavy metal salt described in this patent is actually secondary fly ash in which salt components and heavy metal components are mixed, so that this patent fails to fundamentally solve the essence of secondary fly ash produced by melting, and further requires treatment such as safe landfill and the like, and does not realize recycling of valuable components in secondary fly ash.
Disclosure of Invention
The application provides a method and a device for treating fly ash plasma fusion flue gas, which are used for solving the problems of incomplete recycling of flue gas components and high energy consumption.
The application adopts the following technical scheme.
A method for treating fly ash plasma fusion flue gas for treating flue gas generated in plasma fusion household garbage, comprising:
s1: exchanging heat between the flue gas and air through a high-temperature gas-phase heat exchanger;
s2: carrying out heat transfer and mass transfer dust removal on the flue gas and the landfill leachate by a multistage mass transfer dust removal unit;
s3: washing the flue gas by alkali liquor through an alkali washing tower to remove sulfur dioxide;
s4: dioxin and dust in the flue gas are removed through a filtering and adsorbing unit, and the flue gas is discharged
Further, in step S1, the temperature of the flue gas before entering the high-temperature gas-phase heat exchanger is more than 1100 ℃, the flue gas is cooled to 480-520 ℃ within 1S through the high-temperature gas-phase heat exchanger, and the air is heated to 350-400 ℃ from normal temperature.
Further, in the step S2, the salt concentration of the landfill leachate is controlled to be 0.5-2%, the COD value is controlled to be 1000mg/L, the landfill leachate and the flue gas are subjected to countercurrent direct contact reaction, the leachate is evaporated and concentrated, HCl, heavy metals, alkali metal salts and dust in the flue gas are removed to form a washing liquid, the washing liquid of the multistage mass transfer dust removal unit is sprayed step by step from back to front, the washing liquid is discharged from a first-stage device, and the mixed salt concentration of discharged liquid of the washing liquid is controlled to be 10-20%.
Further, in the step S3, the temperature of the flue gas treated by the multistage mass transfer dust removal unit is controlled to be 90 ℃, the temperature of the flue gas at the outlet of the alkaline washing tower is controlled to be 60 ℃, the pH value of the circulating alkali liquor is controlled to be 7-9, and the concentration of discharged liquid salt is controlled to be 5-15%.
Further, the externally discharged washing liquid of the multistage mass transfer dust removal unit enters a precipitation neutralization unit, solid NaOH is added to neutralize the acidic components in the washing liquid, and solid Na is added 2 CO 3 The soluble calcium and magnesium ions in the precipitate form precipitate sludge, and the precipitate sludge is sent into a plasma furnace for remelting treatment; adding a flocculating agent to precipitate heavy metal components in the washing liquid to form heavy metal sludge, and smelting and extracting the heavy metal sludge as metal resources.
Further, the washing liquid after neutralization precipitation enters a bubbling evaporation cleaning unit, and high-temperature air generated by a high-temperature heat exchanger is directly connected into the washing liquid for contact type bubbling heat exchange evaporation, so that a crystallized mixed salt product is formed.
Further, the sulfite solution discharged from the alkaline washing tower is subjected to evaporation and crystallization to form a sodium sulfite product, or is utilized as a liquid-phase salt solution.
Further, the high-temperature heat exchanger is of a tube-array fin type, the flue gas passes through a tube pass, the air passes through a shell pass, the diameter range of the tube array is 30-100mm, and the heat exchanger adopts a shock wave auxiliary ash cleaning unit to clean the ash condensed during cooling.
The application also provides a device for the fly ash plasma melting flue gas treatment method, which comprises the following steps:
the high-temperature gas-phase heat exchanger is used for connecting the secondary combustion chamber to introduce smoke, and the high-temperature gas-phase heat exchanger is used for introducing air to exchange heat with the smoke;
the multistage mass transfer dust removal unit is connected with the high-temperature gas-phase heat exchanger, and the multistage mass transfer dust removal unit is communicated with landfill leachate to conduct heat transfer and mass transfer dust removal on the flue gas;
the alkaline washing tower is connected with the multistage mass transfer dust removal unit and is used for alkaline washing of the flue gas;
the filtering and adsorbing unit is connected with the alkaline washing tower to filter the flue gas;
and the chimney is connected with the filtering and adsorbing unit and is used for exhausting flue gas.
Further, the device further comprises:
the precipitation neutralization unit is connected with the multistage mass transfer dust removal unit and is used for carrying out precipitation neutralization reaction on the discharged liquid of the multistage mass transfer dust removal unit;
and the bubbling evaporation cleaning unit is connected with the precipitation neutralization unit and is used for performing contact bubbling heat exchange evaporation on the washing liquid discharged by the precipitation neutralization unit.
Advantageous effects
Compared with the prior art, the application has the beneficial effects that:
(1) The application introduces the landfill leachate to wash the flue gas, the landfill leachate is used as a medium for dust removal and mass transfer, the treatment difficulty of the landfill leachate concentrate is solved while water resources are saved, the back spraying of a hearth and the pulping of the concentrate are not needed, the thermal efficiency and the equipment stability of the garbage incinerator are improved, and the aim of treating waste by waste is achieved.
(2) Through the flue gas treatment process, acid gas, heavy metal, dust and salt components in the flue gas are removed through reverse flow mass transfer and dust removal of landfill leachate, enter washing liquid, are subjected to neutralization precipitation separation through subsequent processes, the dust and part of dioxin are returned to a plasma furnace for melting treatment, heavy metal components form heavy metal mud for recycling smelting, and salt components are evaporated to form mixed salt.
(3) The landfill leachate and the flue gas are cooperatively treated, and the landfill leachate is heated by hot air after heat exchange with the flue gas, so that other heat sources are not needed, and energy is saved. The percolate concentrate contains a small amount of COD, if steam tube array evaporation is adopted, wall formation can be caused, heat exchange efficiency is reduced until a heat exchange process is collapsed, and the high-temperature gas-phase heat exchanger is adopted to quench and cool the flue gas, and at the same time, the waste heat in the flue gas is recovered, so that the influence of the COD in the percolate on the process and equipment is avoided through a bubbling evaporation mode.
(4) The clean flue gas after multistage mass transfer and dust removal is subjected to alkaline washing, so that purer sulfite alkaline washing liquid can be formed, and the clean flue gas can be used as a sodium sulfite solution for preparing sodium sulfite products or is subjected to evaporation and cleaning;
(5) The smoke is filtered by the plate filter adsorption unit without secondary dust removal.
Drawings
Fig. 1 is a schematic block diagram of a fly ash plasma fusion flue gas treatment device of the present embodiment.
In the figure:
1. a high temperature gas phase heat exchanger; 2. a countercurrent concentration mass transfer dust removal unit; 3. a mass transfer dust removal unit; 4. an alkaline washing tower; 5. a filtering and adsorbing unit; 6. a chimney; 7. a precipitation neutralization unit; 8. an evaporation crystallization unit; 9. and a secondary combustion chamber.
Detailed Description
The application is further described below in connection with specific embodiments and the accompanying drawings.
Referring to fig. 1, a high temperature gas-phase heat exchanger 1 employed in the present application; a countercurrent concentration mass transfer dust removal unit 2; a mass transfer dust removal unit 3; an alkaline washing tower 4; a filtration and adsorption unit 5; a chimney 6; a precipitation neutralization unit 7; the evaporating crystallization unit 8 adopts conventional equipment in the field, and the structure and principle thereof are known to those skilled in the art, so that the internal structure thereof will not be described herein.
Referring to fig. 1, embodiment 1 of the present application provides a method for treating a flue gas generated in a plasma-melting household garbage, comprising:
s1: exchanging heat between the flue gas and air through a high-temperature gas-phase heat exchanger 1;
s2: carrying out heat transfer and mass transfer dust removal on the flue gas and the landfill leachate by a multistage mass transfer dust removal unit;
s3: washing the flue gas by alkali liquor through an alkali washing tower 4 to remove sulfur dioxide;
s4: dioxin and dust in the flue gas are removed through the filtering and adsorbing unit 5 and discharged.
The plasma melting of fly ash means that plasma is generated by a certain means to be used as a heat source, and the high temperature characteristic of the plasma is utilized to convert materials from solid phase to liquid phase, so that the plasma melting is a means for harmless disposal of the fly ash generated by incineration of household garbage.
The molten fume refers to the gas generated by the plasma melting of the fly ash, and the main pollutant components of the molten fume comprise volatile heavy metal components, low-melting salts (mainly comprising alkali metal chlorides), acid gases (mainly comprising hydrogen chloride and sulfur dioxide) and a part of the fly ash which is not completely reacted, and a certain amount of dioxin also exists in the molten fume.
The percolate concentrate refers to residual liquid trapped by a reverse osmosis membrane and a nanofiltration membrane in the advanced treatment process of the percolate after pretreatment and biochemical treatment of the landfill leachate.
The secondary fly ash refers to tiny particles trapped by various dust removing devices in a flue gas treatment system in the fly ash plasma melting treatment process.
The embodiment 2 of the application provides a method for treating fly ash plasma melting flue gas, which is used for treating flue gas generated in plasma melting household garbage and comprises the following steps:
s1: the flue gas exchanges heat with air through the high-temperature gas-phase heat exchanger 1.
The temperature of the fly ash plasma melting flue gas after passing through the secondary combustion chamber 9 is above 1100 ℃, and the high-temperature flue gas enters a high-temperature gas heat exchanger for quenching and cooling, and the heat exchange medium is normal-temperature air.
The flue gas is cooled to 480-520 ℃ in 1s by a high-temperature gas phase heat exchanger 1, the heat exchange time is preferably 0.3-0.7s, and the air is heated to 350-400 ℃ from normal temperature (room temperature).
In the step, the high-temperature heat exchanger is in the form of a tube-array fin type, the flue gas passes through a tube pass, the air passes through a shell pass, the diameter range of the tube array is 30-100mm, and the heat exchanger adopts a shock wave auxiliary ash removing unit to clean high ash (containing crystalline salt) which is cooled and condensed, so that wall formation and blockage are prevented.
S2: and carrying out heat transfer and mass transfer dust removal on the flue gas and the landfill leachate by a multistage mass transfer dust removal unit.
In the S1, the cooled flue gas enters a multistage mass transfer and dust removal unit, in the unit, the flue gas is subjected to countercurrent injection heat transfer and mass transfer by taking a landfill leachate concentrated solution as a washing solution, the salt concentration of the landfill leachate is controlled to be 0.5-2%, the COD value is controlled to be 1000mg/L, the leachate and the flue gas are subjected to countercurrent direct contact reaction, the leachate is evaporated and concentrated, HCl, heavy metals, alkali metal salts and dust in the flue gas are removed to form the washing solution, the countercurrent injection heat transfer and mass transfer stage number is 2-4, the washing solution of the multistage device is sprayed from back to front stage by stage, the washing solution is discharged from the first stage device, the liquid discharge mixed salt concentration of the washing solution is controlled to be 10-20%, and the optimal value is 15%.
In the embodiment shown in fig. 1, two groups of multistage mass transfer dust removal units are provided to repeatedly wash the flue gas. Wherein the introduced landfill leachate is partially evaporated and concentrated in the first group of multistage mass transfer dust removal units (countercurrent concentration mass transfer dust removal unit 2) due to higher flue gas temperature; the second group of multistage mass transfer dust removal units (mass transfer dust removal unit 3) is heated due to the lower temperature of the flue gas.
It will be appreciated that in other embodiments, only one set of multistage mass transfer and dust removal units may be provided.
S3: the flue gas is washed with an alkaline solution by means of an alkaline wash tower 4 for removal of sulphur dioxide.
The temperature of the flue gas subjected to multistage mass transfer and dust removal is controlled to be 90 ℃ and enters an alkaline washing tower 4, the residual sulfur dioxide is removed by washing with alkali liquor, the temperature of the flue gas at the outlet of the alkaline washing tower 4 is 60 ℃, the pH value of the circulating alkali liquor is controlled to be 7-9, the concentration of discharged liquor salt is controlled to be 5-15%, and the preferential value is 10%.
S4: dioxin and dust in the flue gas are removed through the filtering and adsorbing unit 5 and discharged.
And the residual dioxin and dust are removed from the flue gas at the outlet of the alkaline washing tower 4 through the plate-type filtering and adsorbing unit 5, and then the flue gas reaches the standard and is discharged.
S5: introducing the landfill leachate discharged in the step S2 into a precipitation neutralization unit 7, adding solid NaOH to neutralize acidic components in the landfill leachate, and adding solid Na 2 CO 3 Precipitating soluble calcium and magnesium ions therein to form precipitated sludge; adding a flocculating agent to precipitate heavy metal components in the washing liquid to form heavy metal sludge.
Wherein the acidic component mainly comprises HCl and SO 2 The method comprises the steps of carrying out a first treatment on the surface of the The flocculant can be PAM, etc.
The precipitated sludge contains part of dioxin and is sent into a plasma furnace for remelting treatment.
And smelting and extracting valuable metals by taking the heavy metal sludge as metal resources.
S6: and (3) performing contact type bubbling heat exchange evaporation on the landfill leachate after the reaction in the step (S5) and high-temperature air after heat exchange in the step (S1) through a bubbling evaporation cleaning unit to form a crystallized mixed salt product.
In this step, the amount of high temperature air is adjusted according to the evaporation amount of the clean washing liquid, and external heat source heat compensation is performed as necessary to maintain the stable evaporation process.
The percolate is only concentrated or heated to a certain degree in the mass transfer dust removal process, the main evaporation process occurs in the evaporation crystallization unit, and the long-term operation wall-forming phenomenon of the common indirect heat exchange evaporator cannot be realized because the percolate contains COD, so that the application combines the direct contact of hot air to carry out heat transfer concentration, and solves the problem.
S7: the sulfite solution discharged from the alkaline washing tower 4 in the step S3 is subjected to evaporation and crystallization to form a sodium sulfite product, or is utilized as a liquid-phase salt solution.
It can be understood that after step S2, steps S5 and S6 can be performed; after step S3, step S7 may be performed.
The steps S3 and S4 and the steps S5 and S6 are two independent steps, which can be implemented simultaneously.
Step S7 and step S4 are two independent steps, which can be performed simultaneously.
Embodiment 3 of the present application provides an apparatus used in embodiment 1 and embodiment 2, including:
the high-temperature gas-phase heat exchanger 1 is used for being connected with the secondary combustion chamber 9 to be introduced with smoke, and the high-temperature gas-phase heat exchanger 1 is introduced with air to exchange heat with the smoke;
the multistage mass transfer dust removal unit is connected with the high-temperature gas-phase heat exchanger 1, and the multistage mass transfer dust removal unit is communicated with landfill leachate to transfer heat and remove mass transfer dust to the flue gas;
the alkaline washing tower 4 is connected with the multistage mass transfer dust removal unit, and the alkaline washing tower 4 is used for alkaline washing of the flue gas;
a filtering and adsorbing unit 5 connected with the alkaline washing tower 4 to filter the flue gas;
a chimney 6 connected with the filtering and adsorbing unit 5 for exhausting flue gas;
the precipitation neutralization unit 7 is connected with the multistage mass transfer dust removal unit and is used for carrying out precipitation neutralization reaction on the discharged liquid of the multistage mass transfer dust removal unit;
and the bubbling evaporation cleaning unit 8 is connected with the precipitation neutralization unit 7 and is used for performing contact bubbling heat exchange evaporation on the washing liquid discharged from the precipitation neutralization unit 7.
The high-temperature heat exchanger is in the form of a tube-array fin type, the flue gas passes through a tube pass, the air passes through a shell pass, the diameter range of the tube array is 30-100mm, and the heat exchanger adopts a shock wave auxiliary ash removing unit to clean high ash (containing crystalline salt) which is cooled and condensed, so that wall formation and blockage are prevented.
The examples of the present application are merely for describing the preferred embodiments of the present application, and are not intended to limit the spirit and scope of the present application, and those skilled in the art should make various changes and modifications to the technical solution of the present application without departing from the spirit of the present application.
Claims (6)
1. A method for treating fly ash plasma fusion flue gas for treating flue gas generated in plasma fusion household garbage, comprising:
s1: exchanging heat between the flue gas and air through a high-temperature gas-phase heat exchanger, wherein the temperature of the flue gas before entering the high-temperature gas-phase heat exchanger is more than 1100 ℃, cooling the flue gas to 480-520 ℃ within 1s through the high-temperature gas-phase heat exchanger, and heating the air to 350-400 ℃ from normal temperature;
s2: carrying out heat transfer and mass transfer dust removal on the flue gas and the landfill leachate by a multistage mass transfer dust removal unit; the salt concentration of the landfill leachate is controlled to be 0.5-2%, the COD value is controlled to be 1000mg/L, the landfill leachate and the flue gas are subjected to countercurrent direct contact reaction, the leachate is partially evaporated and concentrated, HCl, heavy metals, alkali metal salts and dust in the flue gas are removed to form a washing liquid, the washing liquid of the multistage mass transfer dust removal unit is sprayed step by step from back to front and discharged from a primary device, and the mixed salt concentration of discharged liquid of the washing liquid is controlled to be 10-20%; the externally discharged washing liquid of the multistage mass transfer dust removal unit enters a precipitation neutralization unit, solid NaOH is added to neutralize acidic components in the washing liquid, and solid Na is added 2 CO 3 Precipitating soluble calcium and magnesium ions therein to form precipitated sludge; adding a flocculating agent to precipitate heavy metal components in the washing liquid to form heavy metal sludge; the washing liquid after neutralization precipitation enters a bubbling evaporation cleaning unit, and high-temperature air generated by a high-temperature heat exchanger is directly communicated with the washing liquid to carry out contact type bubbling heat exchange evaporation, so that a crystallization mixed salt product is formed;
s3: washing the flue gas by alkali liquor through an alkali washing tower to remove sulfur dioxide;
s4: and removing dioxin and dust in the flue gas through a filtering and adsorbing unit and discharging.
2. The method for treating fly ash plasma fusion flue gas according to claim 1, wherein in step S3, the flue gas treated by the multistage mass transfer dust removal unit is controlled to be at 90 ℃ and enters an alkaline washing tower, the flue gas temperature at the outlet of the alkaline washing tower is 60 ℃, the pH value of circulating alkali liquor is controlled to be 7-9, and the concentration of discharged liquid salt is controlled to be 5-15%.
3. A method of treating a molten flue gas from a fly ash plasma according to claim 1, wherein the sulfite solution exiting the caustic scrubber is evaporated to form a sodium sulfite product or is utilized as a liquid phase salt solution.
4. The method for treating the fly ash plasma melting flue gas according to claim 1, wherein the high-temperature heat exchanger is a tube fin type, the flue gas is passed through a tube pass, the air is passed through a shell pass, the diameter of the tube ranges from 30 mm to 100mm, and the heat exchanger adopts a shock wave auxiliary ash removing unit to clean the ash condensed after cooling.
5. An apparatus for use in the fly ash plasma fusion flue gas treatment process of claim 1, comprising:
the high-temperature gas-phase heat exchanger is used for connecting the secondary combustion chamber to introduce smoke, and the high-temperature gas-phase heat exchanger is used for introducing air to exchange heat with the smoke;
the multistage mass transfer dust removal unit is connected with the high-temperature gas-phase heat exchanger, and the multistage mass transfer dust removal unit is communicated with landfill leachate to conduct heat transfer and mass transfer dust removal on the flue gas;
the alkaline washing tower is connected with the multistage mass transfer dust removal unit and is used for alkaline washing of the flue gas;
the filtering and adsorbing unit is connected with the alkaline washing tower to filter the flue gas;
and the chimney is connected with the filtering and adsorbing unit and is used for exhausting flue gas.
6. The apparatus of claim 5, wherein the apparatus further comprises:
the precipitation neutralization unit is connected with the multistage mass transfer dust removal unit and is used for carrying out precipitation neutralization reaction on the discharged liquid of the multistage mass transfer dust removal unit;
and the bubbling evaporation cleaning unit is connected with the precipitation neutralization unit and the high-temperature gas-phase heat exchanger and is used for performing contact type bubbling heat exchange evaporation on the washing liquid discharged by the precipitation neutralization unit through high-temperature air discharged by the high-temperature gas-phase heat exchanger.
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