CN113751214A - System and process for resourcefully treating waste incineration fly ash - Google Patents
System and process for resourcefully treating waste incineration fly ash Download PDFInfo
- Publication number
- CN113751214A CN113751214A CN202110919273.6A CN202110919273A CN113751214A CN 113751214 A CN113751214 A CN 113751214A CN 202110919273 A CN202110919273 A CN 202110919273A CN 113751214 A CN113751214 A CN 113751214A
- Authority
- CN
- China
- Prior art keywords
- fly ash
- cyclone separator
- flue gas
- solid
- outlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C5/00—Apparatus in which the axial direction of the vortex is reversed
- B04C5/24—Multiple arrangement thereof
- B04C5/26—Multiple arrangement thereof for series flow
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B7/00—Hydraulic cements
- C04B7/24—Cements from oil shales, residues or waste other than slag
- C04B7/28—Cements from oil shales, residues or waste other than slag from combustion residues, e.g. ashes or slags from waste incineration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
- B04C2009/002—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks with external filters
-
- 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
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Ceramic Engineering (AREA)
- Inorganic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Structural Engineering (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a system and a process for resourcefully treating waste incineration fly ash, which comprises a thermal desorption system, a water washing system and a drying system; the thermal desorption system is provided with a plurality of stages of cyclone separators, each stage of cyclone separator has the functions of gas-solid mixing, heat exchange and gas-solid separation, hot flue gas is introduced into a flue gas inlet of a last stage of cyclone separator, the flue gas and fly ash carry out heat exchange in the cyclone separator, and organic poisons such as dioxin in the fly ash are pyrolyzed and gasified at high temperature. The fly ash after thermal desorption treatment is firstly washed by a water washing system to remove insoluble salt, liquid enters a crystallization salt making system to be made into sodium chloride and potassium chloride products, and solid is dried by a drying system and then enters a cement making system to be made into a cement finished product. The system and the process are combined to realize the harmlessness, the reclamation and the reduction of the fly ash.
Description
Technical Field
The invention relates to the technical field of incineration disposal residue treatment, in particular to a system and a process for resourcefully treating waste incineration fly ash.
Background
The treatment modes of urban domestic garbage of various countries in the world mainly include 4 types of landfill, composting, incineration and gasification melting. The incineration treatment has become the urban garbage treatment technology widely adopted in the economically developed countries in the world nowadays due to the advantages of thorough harmless treatment, obvious reduction and the like, and the incineration fly ash is accompanied by heavy metal, so that great danger can be caused if the incineration fly ash is not properly treated. Along with the gradual popularization of incineration treatment, the incineration fly ash is properly treated.
There are many kinds of fly ash stabilizing treatment technologies, and the common technologies mainly include melting solidification, cement solidification, chemical agent stabilization and the like. The pure cement is low in curing cost, but the weight increment and the capacity increase are large, so that the storage capacity pressure of a landfill is increased; the volume reduction rate of melting and solidification is high, the stabilizing effect is good, but the process is complex, the treatment cost is high, the investment and the energy consumption are large, and in addition, the problem of secondary pollution exists; chemical agent stabilization organic chelating agents are commonly used to stabilize heavy metals, but the amount is difficult to control and the cost is high.
Disclosure of Invention
In order to overcome the defects of the prior art, one of the purposes of the invention is to provide a system for treating waste incineration fly ash in a recycling way, which can realize the recycling of soluble salt in the fly ash, and can remove organic poisons such as dioxin and the like in the fly ash by heating to modify tailings into cement; the second purpose of the invention is to provide a process for treating fly ash from waste incineration as a resource, which realizes the harmlessness, resource utilization and reduction of fly ash treatment.
One of the purposes of the invention is realized by adopting the following technical scheme:
a system for resourcefully treating waste incineration fly ash comprises a thermal desorption system, a water washing system and a crystallization salt making system; the thermal desorption system comprises a plurality of cyclone separators, a dust remover, a heating device and a circulating fan; each cyclone separator is provided with a feed inlet and a discharge outlet, and the discharge outlet of the upper stage cyclone separator is communicated with the feed inlet of the lower stage cyclone separator in sequence through a pipeline;
each cyclone separator is provided with a flue gas inlet and a flue gas outlet, a dust remover and a circulating fan are arranged between the flue gas outlet of the primary cyclone separator and the flue gas inlet of the heating device, the flue gas outlet of the heating device is connected with the flue gas inlet of the last-stage cyclone separator, and the flue gas outlet of the last-stage cyclone separator is communicated with the flue gas inlet of the upper-stage cyclone separator through a pipeline;
the discharge hole of the last-stage cyclone separator is connected with the feed inlet of the water washing system; the liquid outlet of the water washing system is connected with the crystallization salt preparation system.
Further, the water washing system comprises a first-stage water washing device, a second-stage water washing device and a third-stage water washing device which are sequentially connected; the discharge hole of the last-stage cyclone separator is connected with the slag inlet of the first-stage washing device, the sludge outlet of the third-stage washing device is connected with the sludge inlet of the drying device, and the liquid outlet of the first-stage washing device is connected with the liquid inlet of the crystallization salt-making system. A conductivity meter and a calcium and magnesium ion concentration measuring instrument are arranged in the first-stage water washing device; soluble carbonate is added into the secondary water washing device; and a flocculating agent is added in the third-stage washing device.
Still further, the system for resourcefully treating waste incineration fly ash further comprises a drying system and a cement manufacturing system, wherein a solid outlet of the water washing system is connected with the drying system, and a solid outlet of the drying system is connected with the cement manufacturing system.
Further, the crystallization salt preparation system comprises a cooling crystallization device, an evaporative crystallization device, a first solid-liquid separation device and a second solid-liquid separation device, wherein a liquid outlet of the water washing system is connected with a liquid inlet of the evaporative crystallization device, a liquid outlet of the evaporative crystallization device is connected with a liquid inlet of the cooling crystallization device, and a mixture outlet of the evaporative crystallization device is connected with the first solid-liquid separation device; a centrifugal liquid outlet of the first solid-liquid separation device is connected with a centrifugal liquid inlet of the cooling crystallization device; and a mixture outlet of the cooling crystallization device is connected with the second solid-liquid separation device. Wherein, the evaporative crystallization device comprises a crystallization separator and a thickener which are connected in sequence.
Further, the crystallization salt production system also comprises a first drying device and a second drying device, wherein a solid outlet of the first solid-liquid separation device is connected with the first drying device; and the second solid-liquid separation device is connected with the second drying device.
Still further, the dust remover is one of a cyclone dust remover, a bag-type dust remover, a ceramic dust remover or a metal film dust remover; the heating device is one of a fuel oil heating device, a fuel gas heating device or an electric heating device.
Furthermore, the system for treating waste incineration fly ash in a recycling manner also comprises a fly ash conveying device, and a fly ash outlet of the fly ash conveying device is connected with a fly ash inlet of the primary cyclone separator.
The second purpose of the invention is realized by adopting the following technical scheme:
a process for treating waste incineration fly ash in a recycling manner, which is based on the system for treating waste incineration fly ash in a recycling manner, comprises the following steps:
1) feeding incineration fly ash from a feed inlet of a primary cyclone separator, wherein the fly ash flows from top to bottom, smoke flows from bottom to top in sequence from a final cyclone separator, and the smoke and the fly ash perform heat exchange in the cyclone separator; after the flue gas subjected to heat exchange with the fly ash is discharged from the primary cyclone separator, the flue gas enters a heating device to be heated after dust is removed; the heating medium of the heating device is flue gas discharged by the primary cyclone separator;
2) introducing the fly ash heated in the step 1) into a washing system, adding clear water and mixing with solid to obtain a mixture;
3) separating the mixture obtained in the step 2), enabling the liquid to enter a crystallization salt-making system, and drying the solid by a drying system to be used as a regeneration material;
4) the crystallization salt-making system obtains sodium chloride and potassium chloride products by controlling the temperature.
Further, in the step 1), the temperature of the flue gas entering the final-stage cyclone separator is 500-900 ℃. Preferably 700 deg.c.
Compared with the prior art, the invention has the beneficial effects that:
(1) the system is provided with a thermal desorption system, a water washing system and a drying system, the thermal desorption system is provided with a plurality of stages of cyclone separators, each stage of cyclone separator has the functions of gas-solid mixing, heat exchange and gas-solid separation, flue gas heated by a heating device is introduced into a flue gas inlet of a last stage of cyclone separator, the flue gas enters from bottom to top and heats fly ash entering from top to bottom in the cyclone separator, and organic poisons such as dioxin in the fly ash are pyrolyzed and gasified at high temperature, so that the dioxin in the fly ash is effectively removed. The fly ash after thermal desorption treatment is firstly washed by water to remove insoluble salt, and the liquid enters a crystallization salt-making system to prepare sodium chloride and potassium chloride products. The system of the invention realizes the harmlessness, the resource utilization and the reduction of the fly ash.
(2) The system also comprises a drying system and a cement manufacturing system, wherein the solid passing through the water washing system can be used as a regeneration material after being dried by the drying system, and enters the cement manufacturing system to be manufactured into a cement finished product.
(2) The flue gas generated in the heating process of the cyclone separator in the thermal desorption system is treated by the dust remover and then is conveyed to the heating device by the circulating fan to be used as a supplementary heat source of the heating device, so that the production cost is reduced, and the energy is saved.
(3) According to the process, the fly ash passes through a multi-stage cyclone separator of a thermal desorption system to exchange heat with flue gas flowing through the cyclone separator, toxic organic matters such as dioxin and the like in the fly ash are removed, then the fly ash enters a water washing system to be washed, chlorine elements are separated from solids in a liquid form, the obtained solids do not contain dioxin and chlorine elements, the solids enter a cement manufacturing system to be manufactured into cement finished products, and the liquid enters a crystallization salt manufacturing system to obtain sodium chloride and potassium chloride products by controlling the temperature.
Drawings
FIG. 1 is a process flow diagram of the system of example 1;
FIG. 2 is a process flow diagram of the system of example 2;
FIG. 3 is a schematic diagram of the connection of the thermal desorption system;
FIG. 4 is a process flow diagram of the system of example 2.
In the figure: 1. a thermal desorption system; 11. a primary cyclone separator; 12. a final stage cyclone; 13. a dust remover; 14. a heating device; 15. a circulating fan; 16. a fly ash conveying device; 2. a water washing system; 21. a first-stage water washing device; 22. a secondary water washing device; 23. a third-stage washing device; 3. a drying system; 4. a cement production system; 5. a crystallization salt production system; 51. an evaporative crystallization device; 52. cooling the crystallization device; 53. a first solid-liquid separation device; 54. a second solid-liquid separation device; 55. a first drying device; 56. a second drying device.
Detailed Description
The present invention will be further described with reference to the accompanying drawings and the detailed description, and it should be noted that any combination of the embodiments or technical features described below can be used to form a new embodiment without conflict.
Example 1
As shown in fig. 1, a system for resource treatment of fly ash from waste incineration comprises a thermal desorption system 1, a water washing system 2 and a crystallization salt production system 5;
as shown in fig. 3, the thermal desorption system 1 includes a cyclone group (sequentially named as C1, C2 and C3 from top to bottom) in which three cyclones are connected in series through a pipeline, a fly ash conveying device 16, a dust collector 13, a heating device 14 and a circulating fan 15; each cyclone separator is provided with a feed inlet and a discharge outlet, and the discharge outlet of the upper stage cyclone separator is communicated with the feed inlet of the lower stage cyclone separator in sequence through a pipeline; namely, the flowing direction of fly ash is C1 → C2 → C3.
A fly ash outlet of the fly ash conveying device 16 is connected with a fly ash inlet of the primary cyclone separator 11; each cyclone separator is provided with a flue gas inlet and a flue gas outlet, the flue gas outlet of the primary cyclone separator 11 is connected with the flue gas inlet of the dust remover 13, the flue gas outlet of the dust remover 13 is connected with the flue gas inlet of the heating device 14 through the circulating fan 15, the flue gas outlet of the heating device 14 is connected with the flue gas inlet of the last-stage cyclone separator 12, and the flue gas outlet of the last-stage cyclone separator 12 is communicated with the flue gas inlet of the upper-stage cyclone separator through a heat exchange pipeline; the discharge hole of the final cyclone separator 12 is connected with the feed inlet of the water washing system 2; the liquid outlet of the water washing system 2 is connected with a crystallization salt preparation system 5. The temperature of the flue gas fed to the final cyclone 12(C3) was 900 ℃.
Most of heat exchange and reaction are completed in the pipeline, then fly ash enters a certain-grade cyclone separator at a high speed in a tangential direction along with flue gas from bottom to top, rotates downwards in the cyclone separator, and rotates upwards in a reflection manner to the bottom of the certain-grade cyclone separator, solid particles are thrown to the cylinder wall and collide with the cylinder wall under the action of centrifugal force, and are separated from the flue gas after stalling and falling down and sedimentation, and the solid particles are fed into a next-grade cyclone separator through a discharge port or are discharged. The gas is discharged through a smoke outlet of the cyclone separator. Most of heat exchange and reaction are completed in the pipeline, the tasks of dispersion, uniform distribution, heat exchange and reaction of the fly ash are undertaken, the air speed of the pipeline is 15-18 m/s, and the air speed of the cyclone separator is controlled to be 4-6 m/s. The heating device 14 is an electric heating device 14, and when the heating device is started to operate, air in the pipeline is firstly heated, and then the recovered flue gas is used as a supplementary heat source of the heating device 14.
Example 2
As shown in fig. 2, a system for recycling waste incineration fly ash comprises a thermal desorption system 1, a water washing system 2, a drying system 3, a cement production system 4 and a crystallization salt production system 5;
as shown in fig. 3, the thermal desorption system 1 includes a cyclone group (sequentially named as C1, C2 and C3 from top to bottom) in which three cyclones are connected in series through a pipeline, a fly ash conveying device 16, a dust collector 13, a heating device 14 and a circulating fan 15; each cyclone separator is provided with a feed inlet and a discharge outlet, and the discharge outlet of the upper stage cyclone separator is communicated with the feed inlet of the lower stage cyclone separator in sequence through a pipeline; namely, the flowing direction of fly ash is C1 → C2 → C3.
A fly ash outlet of the fly ash conveying device 16 is connected with a fly ash inlet of the primary cyclone separator 11; each cyclone separator is provided with a flue gas inlet and a flue gas outlet, the flue gas outlet of the primary cyclone separator 11 is connected with the flue gas inlet of the dust remover 13, the flue gas outlet of the dust remover 13 is connected with the flue gas inlet of the heating device 14 through the circulating fan 15, the flue gas outlet of the heating device 14 is connected with the flue gas inlet of the last-stage cyclone separator 12, and the flue gas outlet of the last-stage cyclone separator 12 is communicated with the flue gas inlet of the upper-stage cyclone separator through a heat exchange pipeline;
most of heat exchange and reaction are completed in the pipeline, then fly ash enters a certain-grade cyclone separator at a high speed in a tangential direction along with flue gas from bottom to top, rotates downwards in the cyclone separator, and rotates upwards in a reflection manner to the bottom of the certain-grade cyclone separator, solid particles are thrown to the cylinder wall and collide with the cylinder wall under the action of centrifugal force, and are separated from the flue gas after stalling and falling down and sedimentation, and the solid particles are fed into a next-grade cyclone separator through a discharge port or are discharged. The gas is discharged through a smoke outlet of the cyclone separator. Most of heat exchange and reaction are completed in the pipeline, the tasks of dispersion, uniform distribution, heat exchange and reaction of the fly ash are undertaken, the air speed of the pipeline is 15-18 m/s, and the air speed of the cyclone separator is controlled to be 4-6 m/s. The heating device 14 is a fuel oil heating device 14, and the recovered flue gas is used as a supplementary heat source of the heating device 14.
The discharge hole of the final cyclone separator 12 is connected with the feed inlet of the water washing system 2; the liquid outlet of washing system 2 is connected with crystallization salt system 5, and washing system 2's solid export is connected with drying system 3, and drying system 3's solid export is connected with cement preparation system 4.
A process for treating fly ash from waste incineration in a recycling way comprises the following steps:
1) the fly ash is fed from the feed inlet of the primary cyclone separator 11(C1) through a fly ash conveying device 16, is dispersed by hot flue gas from the C2 cyclone separator, is suspended in a heat exchange pipeline for heat exchange, is carried into the primary cyclone separator 11(C1) by the hot flue gas, is separated from the flue gas under the action of centrifugal force and gravity, and is settled to the bottom of a cone of the primary cyclone separator 11 (C1);
2) the fly ash is fed into a feed inlet of the C2 cyclone separator from a discharge port of the primary cyclone separator 11(C1) through a pipeline, is dispersed, suspended and heated by hot flue gas discharged from the final-stage cyclone separator 12(C3), and is carried into the C2 cyclone separator by the hot flue gas;
3) the fly ash is fed into a feed inlet of a last-stage cyclone separator 12(C3) from a discharge port of a C2 cyclone separator through a pipeline, is dispersed, suspended and heated by hot flue gas from a heating device 14, and is brought into the last-stage cyclone separator 12(C3) by the hot flue gas;
4) finally, the fly ash is separated from the flue gas in the final cyclone 12(C3), passes through the discharge outlet of C3, and enters the water washing system 2. The fly ash passes through a multistage cyclone separator in the cyclone separator and is heated for many times; the heated flue gas sequentially passes through C3, C2 and C1, heat exchange is carried out on the flue gas and fly ash, organic matters are pyrolyzed into waste gas, the waste gas carried by the flue gas is discharged from a primary cyclone separator 11(C1), and the outlet temperature of the flue gas is 200-350 ℃; after the flue gas is dedusted, the flue gas enters a heating device 14 to heat a gas medium, fly ash collected by a deduster 13 enters a final-stage cyclone separator 12(C3) from a feed inlet, and the heated flue gas enters the final-stage cyclone separator 12(C3) again at the temperature of 700 ℃;
5) introducing the fly ash heated in the step 4) into a washing system 2, adding clear water and mixing with solid to obtain a mixture;
6) separating the mixture obtained in the step 5), enabling the liquid to enter a crystallization salt production system 5, and enabling the solid to enter a cement production system 4 after being dried by a drying system 3;
7) the crystallization salt making system 5 obtains sodium chloride and potassium chloride products by controlling the temperature, obtains the potassium chloride product when the cooling crystallization temperature is 40-50 ℃, and obtains the sodium chloride product when the evaporation crystallization temperature is controlled to be 90-110 ℃;
8) drying the solid obtained in the step 6) by a drying system 3, and then allowing the dried solid to enter a cement manufacturing system 4 to solidify, wherein the method specifically comprises the following steps: the (residue) enters a raw material batching station → and raw materials such as sulfuric acid residue, river sand, limestone and the like sequentially enter a raw material mill → a homogenizing bank → a preheater → a decomposing furnace → a rotary kiln → a clinker bank → a cement mill (or directly added into the cement mill and the rotary kiln) → so as to prepare finished cement.
Example 3
As shown in fig. 4, a system for recycling waste incineration fly ash comprises a thermal desorption system 1, a water washing system 2, a drying system 3, a cement production system 4 and a crystallization salt production system 5;
the water washing system 2 comprises a first-stage water washing device 21, a second-stage water washing device 22 and a third-stage water washing device 23 which are connected in sequence; the discharge hole of the final cyclone separator 12 is connected with the slag inlet of the first-stage washing device 21, and a conductivity meter and a calcium and magnesium ion concentration measuring instrument are arranged in the first-stage washing device 21; soluble carbonate is added into the secondary water washing device 22; a flocculating agent is added into the tertiary washing device 23, a sludge outlet of the tertiary washing device 23 is connected with a sludge inlet of the drying device, and a liquid outlet of the tertiary washing device 23 is connected with a liquid inlet of the crystallization salt-making system 5.
The crystallization salt preparation system 5 comprises a cooling crystallization device 52, an evaporation crystallization device 51, a first solid-liquid separation device 53, a second solid-liquid separation device 54, a first drying device 55 and a second drying device 56, wherein a liquid outlet of the third-stage washing device 23 is connected with a liquid inlet of the evaporation crystallization device 51, a liquid outlet of the evaporation crystallization device 51 is connected with a liquid inlet of the cooling crystallization device 52, a mixture outlet of the evaporation crystallization device 51 is connected with the first solid-liquid separation device 53, and a solid outlet of the first solid-liquid separation device 53 is connected with the first drying device 55; a centrifugate outlet of the first solid-liquid separation device 53 is connected with a centrifugate inlet of the cooling crystallization device; the mixture outlet of the cooling crystallization device 52 is connected to a second solid-liquid separation device 54, and the second solid-liquid separation device 54 is connected to a second drying device 56.
As shown in fig. 3, the thermal desorption system 1 includes a cyclone group (sequentially named as C1, C2 and C3 from top to bottom) in which three cyclones are connected in series through a pipeline, a fly ash conveying device 16, a dust collector 13, a heating device 14 and a circulating fan 15; each cyclone separator is provided with a feed inlet and a discharge outlet, and the discharge outlet of the upper stage cyclone separator is communicated with the feed inlet of the lower stage cyclone separator in sequence through a pipeline; namely, the flowing direction of fly ash is C1 → C2 → C3.
A fly ash outlet of the fly ash conveying device 16 is connected with a fly ash inlet of the primary cyclone separator 11; each cyclone separator is provided with a flue gas inlet and a flue gas outlet, the flue gas outlet of the primary cyclone separator 11 is connected with the flue gas inlet of the dust remover 13, the flue gas outlet of the dust remover 13 is connected with the flue gas inlet of the heating device 14 through the circulating fan 15, the flue gas outlet of the heating device 14 is connected with the flue gas inlet of the last-stage cyclone separator 12, and the flue gas outlet of the last-stage cyclone separator 12 is communicated with the flue gas inlet of the upper-stage cyclone separator through a heat exchange pipeline;
most of heat exchange and reaction are completed in the pipeline, then fly ash enters a certain-grade cyclone separator at a high speed in a tangential direction along with flue gas from bottom to top, rotates downwards in the cyclone separator, and rotates upwards in a reflection manner to the bottom of the certain-grade cyclone separator, solid particles are thrown to the cylinder wall and collide with the cylinder wall under the action of centrifugal force, and are separated from the flue gas after stalling and falling down and sedimentation, and the solid particles are fed into a next-grade cyclone separator through a discharge port or are discharged. The gas is discharged through a smoke outlet of the cyclone separator. Most of heat exchange and reaction are completed in the pipeline, the tasks of dispersion, uniform distribution, heat exchange and reaction of the fly ash are undertaken, the air speed of the pipeline is 15-18 m/s, and the air speed of the cyclone separator is controlled to be 4-6 m/s. The heating device 14 is an oil heating device 14 or a gas heating device 14, and the recovered flue gas is used as a supplementary heat source of the heating device 14.
The discharge hole of the final cyclone separator 12 is connected with the feed inlet of the water washing system 2; the liquid outlet of washing system 2 is connected with crystallization salt system 5, and washing system 2's solid export is connected with drying system 3, and drying system 3's solid export is connected with cement preparation system 4.
A process for treating fly ash from waste incineration in a recycling way comprises the following steps:
1) the fly ash is fed from the feed inlet of the primary cyclone separator 11(C1) through a fly ash conveying device 16, is dispersed by hot flue gas from the C2 cyclone separator, is suspended in a heat exchange pipeline for heat exchange, is carried into the primary cyclone separator 11(C1) by the hot flue gas, is separated from the flue gas under the action of centrifugal force and gravity, and is settled to the bottom of a cone of the primary cyclone separator 11 (C1);
2) the fly ash is fed into a feed inlet of the C2 cyclone separator from a discharge port of the primary cyclone separator 11(C1) through a pipeline, is dispersed, suspended and heated by hot flue gas discharged from the final-stage cyclone separator 12(C3), and is carried into the C2 cyclone separator by the hot flue gas;
3) the fly ash is fed into a feed inlet of a last-stage cyclone separator 12(C3) from a discharge port of a C2 cyclone separator through a pipeline, hot flue gas heated to 650-850 ℃ enters from the last-stage cyclone separator 12(C3), and the fly ash is dispersed, suspended and heated by the hot flue gas from a heating device 14 and then is brought into the last-stage cyclone separator 12(C3) by the hot flue gas;
4) finally, the fly ash is separated from the flue gas in the final cyclone 12(C3), passes through the discharge outlet of C3, and enters the primary water washing device 21 of the water washing system 2. The fly ash passes through a multistage cyclone separator in the cyclone separator and is heated for many times; the heated flue gas sequentially passes through C3, C2 and C1, and after heat exchange with fly ash, the flue gas carrying waste gas is discharged from a primary cyclone separator 11(C1), and the outlet temperature of the flue gas is 200-350 ℃; after the flue gas is dedusted, the flue gas enters a heating device 14 to heat a gas medium, fly ash collected by a deduster 13 enters a final-stage cyclone separator 12(C3) from a feed inlet, and the flue gas at 500 ℃ after being heated enters the final-stage cyclone separator 12 (C3);
5) introducing the fly ash heated in the step 4) into a first-stage washing device 21 of a washing system 2, adding clear water to mix with the solid to obtain a mixture, measuring the conductivity and the calcium and magnesium ion concentration in the water body, introducing the mixture into a second-stage washing device 22, adding sodium carbonate according to the conductivity and the calcium and magnesium ion concentration, introducing into a third-stage washing device 23, adding PAM, and separating the solid from the liquid; the soluble carbonate is sodium carbonate, and the flocculant is PAC.
6) And (3) enabling the liquid obtained in the step 5) to enter an evaporative crystallization device 51 of a crystallization salt making system 5, and controlling the temperature of the evaporative crystallization device 51 at 55-60 ℃ to obtain salt mother liquor and solid. And (3) introducing the salt mother liquor into a cooling crystallization device 52, adding water into the solid, mixing, introducing the solid and the centrifugate into a first solid-liquid separation device 53 to obtain the solid and the centrifugate, introducing the centrifugate into the cooling crystallization device 52, introducing the solid into a first drying device 55, and controlling the temperature at 95-100 ℃ to obtain sodium chloride. After the liquid in the cooling crystallization device 52 passes through the second solid-liquid separation device 54, the solid enters the second drying device 56, and potassium chloride is obtained.
7) Drying the solid obtained in the step 6) by a drying system 3, and then allowing the dried solid to enter a cement manufacturing system 4 to solidify, wherein the method specifically comprises the following steps: the (residue) enters a raw material batching station → and raw materials such as sulfuric acid residue, river sand, limestone and the like sequentially enter a raw material mill → a homogenizing warehouse → a decomposing furnace → a rotary kiln → a clinker warehouse → a cement mill (or can be directly added into the cement mill and the rotary kiln) → so as to prepare finished cement.
Performance testing
Firstly, the sodium chloride and the potassium chloride obtained in the step 6) in the example 3 and the solid treated by the drying system 3 in the step 7) are taken to measure the water content, the chlorine content, the mercury content, the lead content and the dioxin content, and the following data are obtained:
TABLE 1 salts and residues after treatment and fly ash data before treatment
| Serial number | Test items | Unit of | Fly ash before treatment | Treated salts | Treated solid |
| 1 | Water content ratio | ％ | 3.6 | 0.28 | 2.1 |
| 2 | Chlorine | ％ | 17.83 | 67.29 | 0.42 |
| 3 | Mercury | mg/kg | 0.257 | / | 0.009 |
| 4 | Lead (II) | mg/kg | 712.44 | / | 556.38 |
| 5 | Dioxin (DIOXIN) | TEQμg/kg | 0.126 | / | / |
Secondly, the sodium chloride and the potassium chloride obtained in the step 6) in the example 3 are taken for testing, and the following data are obtained:
TABLE 2 Performance parameters of the sodium chloride obtained after the treatment
TABLE 3 Property parameters of the potassium chloride obtained after the treatment
| Quality index | Unit of | Standard (delicate industrial salt second level) | Actual measurement result |
| Potassium chloride | ％ | ≥97.5 | 98.85 |
| Moisture content | ％ | ≤0.8 | 0.13 |
| Water insoluble substance | ％ | ≤0.2 | 0.08 |
| Calcium magnesium ion | ％ | ≤0.6 | 0.01 |
| Sulfate ion | ％ | ≤0.9 | 0.026 |
As is clear from the data in table 1, the sodium chloride and the potassium chloride obtained in example 3 do not contain any heavy metal elements such as dioxin, lead, mercury, and the like; the treated solid does not contain dioxin, the residual chlorine element only accounts for 0.42%, and the residual mercury, lead and other toxic heavy metals are also contained, so that the method is proved that organic poisons such as dioxin and the like in the fly ash are effectively removed through the thermal desorption system 1, the chlorine element in the fly ash is effectively removed, the reduction is obvious, and the dried solid enters the cement manufacturing system 4 to be manufactured into a cement finished product.
As can be seen from the data in tables 2-3, the sodium chloride and potassium chloride obtained by the crystallization salt production system 5 meet the secondary standard of refining industrial salt, which indicates that the system of example 3 can effectively recover industrial salt.
The above embodiments are only preferred embodiments of the present invention, and the protection scope of the present invention is not limited thereby, and any insubstantial changes and substitutions made by those skilled in the art based on the present invention are within the protection scope of the present invention.
Claims (10)
1. A system for resourcefully treating waste incineration fly ash is characterized by comprising a thermal desorption system, a water washing system and a crystallization salt making system; the thermal desorption system comprises a plurality of cyclone separators, a dust remover, a heating device and a circulating fan; each cyclone separator is provided with a feed inlet and a discharge outlet, and the discharge outlet of the upper stage cyclone separator is communicated with the feed inlet of the lower stage cyclone separator in sequence through a pipeline;
each cyclone separator is provided with a flue gas inlet and a flue gas outlet, a dust remover and a circulating fan are arranged between the flue gas outlet of the primary cyclone separator and the flue gas inlet of the heating device, the flue gas outlet of the heating device is connected with the flue gas inlet of the last-stage cyclone separator, and the flue gas outlet of the last-stage cyclone separator is communicated with the flue gas inlet of the upper-stage cyclone separator through a pipeline;
the discharge hole of the last-stage cyclone separator is connected with the feed inlet of the water washing system; the liquid outlet of the water washing system is connected with the crystallization salt preparation system.
2. The system for resource treatment of fly ash from waste incineration according to claim 1, wherein the water washing system comprises a primary water washing device, a secondary water washing device and a tertiary water washing device which are connected in sequence; the discharge hole of the last-stage cyclone separator is connected with the slag inlet of the first-stage washing device, the sludge outlet of the third-stage washing device is connected with the sludge inlet of the drying device, and the liquid outlet of the first-stage washing device is connected with the liquid inlet of the crystallization salt-making system.
3. The system for recycling waste incineration fly ash according to claim 1, further comprising a drying system and a cement manufacturing system, wherein the solid outlet of the water washing system is connected with the drying system, and the solid outlet of the drying system is connected with the cement manufacturing system.
4. The system for resource utilization of waste incineration fly ash according to claim 1, wherein the crystallization salt preparation system comprises a cooling crystallization device, an evaporation crystallization device, a first solid-liquid separation device and a second solid-liquid separation device, a liquid outlet of the water washing system is connected with a liquid inlet of the evaporation crystallization device, a liquid outlet of the evaporation crystallization device is connected with a liquid inlet of the cooling crystallization device, and a mixture outlet of the evaporation crystallization device is connected with the first solid-liquid separation device; a centrifugal liquid outlet of the first solid-liquid separation device is connected with a centrifugal liquid inlet of the cooling crystallization device; and a mixture outlet of the cooling crystallization device is connected with the second solid-liquid separation device.
5. The system for resource recycling waste incineration fly ash according to claim 4, wherein the crystallization salt making system further comprises a first drying device and a second drying device, and the solid outlet of the first solid-liquid separation device is connected with the first drying device; and the second solid-liquid separation device is connected with the second drying device.
6. The system for resource utilization of fly ash from incineration of refuse according to claim 1, wherein the dust collector is one of a cyclone dust collector, a bag dust collector, a ceramic dust collector or a metal film dust collector; the heating device is one of a fuel oil heating device, a fuel gas heating device or an electric heating device.
7. The system for recycling waste incineration fly ash according to claim 1, further comprising a fly ash conveying device, wherein a fly ash outlet of the fly ash conveying device is connected to the fly ash inlet of the primary cyclone.
8. A process for recycling waste incineration fly ash, which is characterized in that the system for recycling waste incineration fly ash according to any one of claims 1 to 7 comprises the following steps:
1) feeding incineration fly ash from a feed inlet of a primary cyclone separator, wherein the fly ash flows from top to bottom, smoke flows from bottom to top in sequence from a final cyclone separator, and the smoke and the fly ash perform heat exchange in the cyclone separator; after the flue gas subjected to heat exchange with the fly ash is discharged from the primary cyclone separator, the flue gas enters a heating device to be heated after dust is removed; the heating medium of the heating device is flue gas discharged by the primary cyclone separator;
2) introducing the fly ash heated in the step 1) into a washing system, adding clear water and mixing with solid to obtain a mixture;
3) separating the mixture obtained in the step 2), enabling the liquid to enter a crystallization salt-making system, and drying the solid by a drying system to be used as a regeneration material;
4) the crystallization salt-making system obtains sodium chloride and potassium chloride products by controlling the temperature.
9. The process for resource utilization of waste incineration fly ash according to claim 8, wherein in the step 1), the temperature of the flue gas entering the final cyclone separator is 500-900 ℃.
10. The process according to claim 8, wherein in the step 2), after the mixture is obtained, the conductivity and the concentration of calcium and magnesium ions in the water are measured, soluble carbonate is added according to the conductivity and the concentration of calcium and magnesium ions, and then the flocculating agent is added to separate the solid from the liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110919273.6A CN113751214A (en) | 2021-08-11 | 2021-08-11 | System and process for resourcefully treating waste incineration fly ash |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110919273.6A CN113751214A (en) | 2021-08-11 | 2021-08-11 | System and process for resourcefully treating waste incineration fly ash |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113751214A true CN113751214A (en) | 2021-12-07 |
Family
ID=78788985
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110919273.6A Pending CN113751214A (en) | 2021-08-11 | 2021-08-11 | System and process for resourcefully treating waste incineration fly ash |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113751214A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114573005A (en) * | 2022-03-11 | 2022-06-03 | 苏州乔发环保科技股份有限公司 | Potassium-sodium salt recycling process for sintering machine head ash and garbage fly ash |
-
2021
- 2021-08-11 CN CN202110919273.6A patent/CN113751214A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114573005A (en) * | 2022-03-11 | 2022-06-03 | 苏州乔发环保科技股份有限公司 | Potassium-sodium salt recycling process for sintering machine head ash and garbage fly ash |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104289513B (en) | A kind of mercury contaminated soil thermal desorption processing means and processing method | |
| US4852269A (en) | Combined sewage and lime slude treatment process | |
| CN111100719B (en) | Preparation method of water-washed fly ash derived fuel | |
| CN101717208B (en) | Process method and process system of exhaust gas of cement calcination equipment | |
| CN113245342B (en) | Resource treatment method and treatment system for waste incineration fly ash water washing salt making based on seed crystal method | |
| TW200416211A (en) | Cement kiln chlorine sulfur bypass system | |
| CN113247932A (en) | System for preparing polyaluminum chloride from aluminum ash and manufacturing method of polyaluminum chloride | |
| CN114054469A (en) | Aluminum ash harmless treatment and resource recycling method and system | |
| CN113233798A (en) | Cement kiln dust/fly ash washing salt extraction treatment system and use method thereof | |
| CN109574451A (en) | A kind of method of sludge drying comprehensive utilization | |
| CN107388262B (en) | A kind of harmlessness disposing method of comprehensive utilization of high saliferous chemical engineering sludge | |
| CN112317517A (en) | Pretreatment system and method suitable for co-processing electrolytic aluminum overhaul residues in cement kiln | |
| CN215523357U (en) | Fly ash treatment device | |
| CN113751214A (en) | System and process for resourcefully treating waste incineration fly ash | |
| CN109420662A (en) | A kind of system of municipal administration and metallurgical difficult solid waste collaboration resource utilization | |
| CN105506292B (en) | A kind of heavy metal sewage sludge harmless treatment and resource utilization method | |
| CN216137437U (en) | System for resourceful treatment waste incineration fly ash | |
| CN212285251U (en) | Dust collecting system for steel plant disposed by mesh belt type suspension combined reduction furnace | |
| CN111282961B (en) | System and method for disposing dust collection ash of steel plant by using mesh belt type suspension combined reduction furnace | |
| CN108679628B (en) | System and method for disposing overhaul slag of aluminum electrolysis cell by cement kiln bypass incineration | |
| CN106006643A (en) | Method for preparing calcium carbide from yellow phosphorus tail gas and phosphogypsum | |
| CN207592409U (en) | A kind of system of municipal administration and metallurgical difficult solid waste collaboration recycling | |
| CN115710065A (en) | Method and equipment for treating desulfurization wastewater of flue gas desulfurization system | |
| CN210826301U (en) | Comprehensive utilization equipment system for gold smelting slag | |
| CN211527160U (en) | Drying system tail gas waste heat is from utilization system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |