CN217369706U - Waste incineration fly ash treatment system - Google Patents
Waste incineration fly ash treatment system Download PDFInfo
- Publication number
- CN217369706U CN217369706U CN202122737621.6U CN202122737621U CN217369706U CN 217369706 U CN217369706 U CN 217369706U CN 202122737621 U CN202122737621 U CN 202122737621U CN 217369706 U CN217369706 U CN 217369706U
- Authority
- CN
- China
- Prior art keywords
- washing
- tank
- stage
- fly ash
- ash
- 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.)
- Active
Links
Images
Classifications
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/91—Use of waste materials as fillers for mortars or concrete
Landscapes
- Processing Of Solid Wastes (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model provides a waste incineration fly ash treatment system, which belongs to the field of waste treatment and resource utilization, and comprises a multi-stage countercurrent washing dechlorination unit, a high-chlorine washing liquid water treatment unit and a sludge recycling zero discharge unit; the high-chlorine washing liquid water treatment unit comprises a regulating tank, a hardness removal reaction tank, a heavy metal removal reaction tank, a membrane filtration concentration tank, a tubular membrane filtration tank and a washing liquid cache tank which are sequentially connected; and the sludge recovery zero discharge unit is used for treating sludge slurry, the obtained filter residue is returned to the multi-stage countercurrent washing dechlorination unit for circular treatment, and the obtained filtrate is returned to the high-chlorine washing liquor water treatment unit for circular treatment. The utility model ensures that the final ash slag meets the feeding requirement of the cement kiln cooperative treatment by the comprehensive treatment of 'multi-stage countercurrent rinsing, tubular membrane softening and filtering and sludge recovery'; harmful components such as heavy metal, dioxin and the like are precipitated and retained to the maximum extent; and the generated sludge sediment is completely recycled, so that the aim of zero discharge of the water washing and water treatment process in the fly ash recycling process is fulfilled.
Description
Technical Field
The utility model belongs to the technical field of refuse treatment and resource utilization, concretely relates to waste incineration flying ash processing system.
Background
The garbage incineration fly ash is generally solid matter generated in the process of urban domestic garbage incineration and collected by a flue gas purification device, a flue gas pipeline, a dust remover and a separator.
At present, the effective treatment of the fly ash generated by burning the household garbage is divided into two types: one is landfill after stabilization treatment, and the other is resource treatment. In consideration of the requirement of environmental protection situation, the quantity of landfill sites and the engineering quality requirement are improved, the treatment prospect of the fly ash as hazardous waste for landfill is limited, and the resource treatment mode is imperative. The fly ash contains rich potassium salt, and the potassium salt is a deficient resource in China, and accounts for about 50% of the annual dependence on import, so the recovery of the potassium salt resource has practical significance on the environmental and resource problems in China. The reasonable recycling treatment mode can select washing dechlorination treatment and then cement kiln cooperative treatment or high-temperature calcination to prepare the gravel for building materials, but both the two modes need pretreatment, namely, the fly ash needs washing dechlorination treatment and then meets the feeding requirements of cement production and building materials.
The water treatment of the washing dechlorination salt extraction and the washing liquor is closely related to the quality of cement clinker treated by the cooperation of the cement kiln, and directly determines the quality of the recycled salt potassium extraction. The cement kiln is cooperatively treated to require that the chlorine content of the washed ash is less than 1%, the water treatment of washing liquor is used for removing heavy metals and suspended matters, the quality of salt potassium extracted by evaporation crystallization is directly determined, the sludge component generated in the water treatment softening process is mainly calcium salt and can be used as a material for cement feeding, but the chlorine content of the existing fly ash after the water washing dechlorination treatment is high, so that the ash, softened sludge and produced water after the water treatment cannot be directly recycled.
SUMMERY OF THE UTILITY MODEL
The embodiment of the utility model provides a waste incineration flying ash processing system aims at realizing that lime-ash, mud and the product water after the flying ash washing is handled can reach direct recycle, improves the recycle efficiency of resource.
In order to achieve the purpose, the utility model adopts the technical proposal that: provided is a waste incineration fly ash treatment system, including:
a multi-stage countercurrent washing dechlorination unit to obtain ash and high-chlorine washing liquor suitable for building material ingredients;
the high-chlorine washing liquid water treatment unit is used for treating the high-chlorine washing liquid to obtain chlorine salt washing liquid for resource recovery; the high-chlorine washing liquid water treatment unit comprises a regulating tank, a hardness removal reaction tank, a heavy metal removal reaction tank, a membrane filtration concentration tank, a tubular membrane filtration tank and a washing liquid cache tank which are connected in sequence; and
and the sludge recycling zero discharge unit is used for receiving and processing the sludge slurry deposited in the membrane filtration concentration tank, the obtained filter residue is returned to the multistage counter-current washing dechlorination unit for circular processing, and the obtained filtrate is returned to the regulating tank of the high-chlorine washing liquid water processing unit for circular processing.
In one possible implementation manner, the multistage countercurrent water washing dechlorination unit comprises a first-stage water washing dechlorination combination, a second-stage water washing dechlorination combination and a third-stage water washing dechlorination combination; the fly ash is subjected to the primary washing and dechlorinating combination, the obtained high-chlorine washing liquid enters the regulating tank, and the obtained primary ash slag enters the secondary washing and dechlorinating combination treatment; the intermediate chlorine washing liquor obtained by the secondary water washing dechlorination combination is returned to the primary water washing dechlorination combination for circular treatment, and the obtained secondary ash enters the tertiary water washing dechlorination combination for treatment; and the final ash is obtained by the combination of the third-stage water washing and dechlorination, and the obtained low-chlorine washing liquid returns to the second-stage water washing and dechlorination combination for circular treatment.
In one possible implementation mode, the primary water washing dechlorination combination comprises a primary pulping ash washing barrel and a primary solid-liquid separator, wherein the primary pulping ash washing barrel is provided with an acid-base dosing pump, and the primary solid-liquid separator is a horizontal screw centrifuge; the secondary water washing dechlorination combination comprises a secondary pulping ash washing barrel and a secondary solid-liquid separator, and the secondary solid-liquid separator is a horizontal screw centrifuge; the three-stage water washing and dechlorinating combination comprises a three-stage pulping and ash washing barrel and a three-stage solid-liquid separator, and the three-stage solid-liquid separator is a horizontal screw centrifuge; and a fresh water inlet is formed in the third-stage pulping ash washing barrel.
In a possible implementation mode, a spraying water nozzle is arranged on the primary pulping and ash washing barrel.
In one possible implementation manner, an acid-base adding port is arranged on the hardness removing reaction tank; and a flocculating agent adding port is arranged on the heavy metal removing reaction tank.
In a possible implementation manner, the tubular membrane filtration tank is provided with an acid-base adding port.
In a possible implementation manner, a washing liquid pump is arranged between the heavy metal removal reaction tank and the membrane filtration concentration tank.
In a possible implementation manner, a booster pump is arranged between the membrane filtration concentration tank and the tubular membrane filtration tank.
In a possible implementation mode, the sludge recycling zero discharge unit comprises a sludge storage tank and a four-stage solid-liquid separator, sludge slurry is pumped into the sludge storage tank for precipitation, slurry is pumped into the four-stage solid-liquid separator for separation, obtained filtrate is returned to the adjusting tank for circular treatment, and obtained filter residues are returned to the multistage countercurrent washing dechlorination unit for circular treatment.
In a possible realization mode, a lower discharge outlet discharge pump is arranged between the membrane filtration concentration tank and the sludge storage tank.
The utility model provides a waste incineration flying ash processing system compares with prior art, and beneficial effect lies in: through the comprehensive treatment of 'multi-stage countercurrent rinsing, tubular membrane softening and filtering and sludge recovery', heavy metals and dioxin can be rinsed out from washing liquor as little as possible under the rinsing condition with low water-ash ratio, and the chlorine content of final ash slag of the fly ash subjected to multi-stage water washing dechlorination is ensured to be less than 1%, so that the feeding requirement of cement kiln cooperative treatment is met; can deposit and retain harmful components such as heavy metal, dioxin and the like to the maximum extent in the water treatment process of the washing liquor; can completely recycle sludge sediment generated in the water treatment process, and realizes the aim of zero discharge of the water washing and water treatment processes in the fly ash recycling process.
Drawings
FIG. 1 is a schematic structural diagram of a waste incineration fly ash treatment system according to an embodiment of the present invention;
Detailed Description
In order to make the technical problem, technical solution and advantageous effects to be solved by the present invention more clearly understood, the following description is given in conjunction with the accompanying drawings and embodiments to illustrate the present invention in further detail. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the invention.
Referring to fig. 1, a garbage incineration fly ash treatment system according to the present invention will now be described. The waste incineration fly ash treatment system comprises a multi-stage countercurrent washing dechlorination unit, a high-chlorine washing liquor water treatment unit and a sludge recycling zero discharge unit, wherein the multi-stage countercurrent washing dechlorination unit is used for obtaining ash and high-chlorine washing liquor suitable for building material ingredients; the high-chlorine washing liquid water treatment unit is used for treating the high-chlorine washing liquid to obtain chlorine salt washing liquid for resource recovery; the high-chlorine washing liquid water treatment unit comprises a regulating tank, a hardness removal reaction tank, a heavy metal removal reaction tank, a membrane filtration concentration tank, a tubular membrane filtration tank and a washing liquid cache tank which are sequentially connected; the sludge recycling zero discharge unit is used for receiving and processing sludge slurry deposited by the membrane filtration concentration tank, the obtained filter residue is returned to the multistage countercurrent washing dechlorination unit for circular processing, and the obtained filtrate is returned to the regulating tank of the high-chlorine washing liquid water processing unit for circular processing.
Compared with the prior art, the waste incineration fly ash treatment system provided by the embodiment can rinse heavy metals and dioxin in a washing solution as little as possible under the rinsing condition of a low water-ash ratio through the comprehensive treatment of 'multi-stage countercurrent rinsing, tubular membrane softening and filtering and sludge recovery', ensure that the chlorine content of final ash slag of the fly ash subjected to multi-stage water washing dechlorination is less than 1%, and meet the feeding requirement of cement kiln cooperative treatment; can deposit and retain harmful components such as heavy metal, dioxin and the like to the maximum extent in the water treatment process of the washing liquor; can completely recycle sludge sediment generated in the water treatment process, and realizes the aim of zero discharge of the water washing and water treatment processes in the fly ash recycling process.
After the waste incineration fly ash treatment system provided by the embodiment is used for water washing treatment, 15% -40% of soluble substances such as sodium chloride, potassium chloride, calcium chloride, nitrate, a small amount of heavy metals and a small amount of dioxin adsorbed by scum in the fly ash can be transferred to water washing liquid, and the high-chlorine washing liquid is subjected to hardness removal, heavy metals removal and filtration treatment to obtain chlorine salt washing liquid, and the potassium salt in the washing liquid is subjected to resource extraction in a manner of 'high-temperature evaporation for sodium extraction, cooling crystallization for potassium extraction'.
As an embodiment of the waste incineration fly ash treatment system provided in this embodiment, please refer to fig. 1, the multistage counter-current water washing dechlorination unit employs three-stage counter-current water washing dechlorination, and the three-stage dechlorination structure is substantially the same, and specifically includes a first-stage water washing dechlorination combination, a second-stage water washing dechlorination combination, and a third-stage water washing dechlorination combination; the fly ash is subjected to primary washing dechlorination combination, the obtained high-chlorine washing liquid enters an adjusting tank, and the obtained primary ash slag enters secondary washing dechlorination combination treatment; the intermediate chlorine washing liquor obtained by the secondary washing dechlorination combination is returned to the primary washing dechlorination combination for circulating treatment, and the obtained secondary ash enters the tertiary washing dechlorination combination treatment; and (3) carrying out tertiary washing dechlorination combination to obtain final ash, and returning the obtained low-chlorine washing liquor to secondary washing dechlorination combination for circulating treatment. The fly ash is subjected to three-stage dechlorination, and finally obtained ash is sent to a cement kiln to be cooperatively treated with a certain proportion of main materials to be fired into cement clinker.
Based on the three-stage countercurrent washing dechlorination, the specific structure examples of each stage of the embodiment are as follows: the primary washing dechlorination combination comprises a primary pulping ash washing barrel and a primary solid-liquid separator, wherein the primary pulping ash washing barrel is provided with an acid-base dosing pump, and the primary solid-liquid separator is a horizontal screw centrifuge; the secondary washing dechlorination combination comprises a secondary pulping ash washing barrel and a secondary solid-liquid separator, wherein the secondary solid-liquid separator is a horizontal screw centrifuge; the three-stage water washing and dechlorinating combination comprises a three-stage pulping and ash washing barrel and a three-stage solid-liquid separator, wherein the three-stage solid-liquid separator is a horizontal screw centrifuge; the third-stage pulping ash-washing barrel is provided with a fresh water inlet.
Based on concrete structure and the sludge recovery zero discharge unit at different levels in foretell tertiary countercurrent washing dechlorination, as an embodiment of the waste incineration fly ash processing system that this embodiment provided, the system includes that one-level slurrying washes ash bucket, one-level solid-liquid separation machine, second grade slurrying washes ash bucket, second grade solid-liquid separation machine, third grade slurrying washes ash bucket, third grade solid-liquid separation machine, equalizing basin, except that hard reaction tank, heavy metal reaction tank, membrane filtration concentration pond, sludge storage tank, level four solid-liquid separation machine, tubular membrane filtration, wash liquor buffer memory pond etc. system connection constitutes.
In the above-mentioned embodiment, one-level slurrying ash washing bucket, second grade slurrying ash washing bucket and tertiary system slurrying ash washing bucket pass through the agitator and mix the slurrying rinsing, hydrochloric acid and the charge device of liquid caustic soda are all connected to the ash washing bucket of each grade, a lotion pH 10 ~ 11 in the ash washing bucket for adjusting each grade, under the high pH condition, the solubility of heavy metal and calcium magnesium ion in the lotion is low, dioxin is stable under strong acid strong alkali condition, be difficult to water, can only exist with the form that adsorbs on the suspended solid in a small amount, high pH condition can effectively prevent washing out of heavy metal, calcium magnesium and dioxin.
Wherein, the upper part of the first-stage pulping and ash-washing barrel is provided with spray water to prevent flying dust in the first-stage pulping and ash-washing process; the first-stage solid-liquid separator, the second-stage solid-liquid separator, the third-stage solid-liquid separator and the fourth-stage solid-liquid separator adopt horizontal spiral sedimentation centrifuges or horizontal spiral filtering centrifuges, the horizontal spiral centrifuges are generally called as horizontal spiral centrifuges, the horizontal spiral centrifuges do not have too high requirements on the uniformity of fed slag flocs, a large amount of flocculating agents are not required to be added in feeding, and stable and continuous operation under automatic control can be realized. Solid-liquid separation is carried out on the fly ash pulp washing by adopting a horizontal screw centrifuge for centrifugation, so that the water content of each level of fly ash pulp washing after centrifugal dehydration is less than or equal to 30 percent, the water adding amount in the washing process is reduced, and the water-cement ratio is 2: 1-4: within the range of 1, the chlorine content in the fly ash after the three-stage washing dechlorination is less than 1 percent, and the feeding requirement of the cement kiln cooperative treatment is met.
The structure and the function of each part in the high-chlorine washing liquid water treatment unit are as follows: the regulating tank can mix and homogenize the high-chlorine washing liquor and the centrifugal filtrate of the four-stage solid-liquid separator; the hardness removing reaction tank reacts with calcium and magnesium ions in washing liquor to generate insoluble substance precipitate by adding liquid alkali and sodium carbonate or removing hardness of flue gas; the heavy metal removing reaction tank is used for precipitating heavy metals in washing liquor by adding a vulcanizing agent or other medicaments; the membrane filtration concentration tank is used for storing washing liquid after heavy metal removal reaction and circulating concentrated liquid of tubular membrane filtration, and sludge slurry deposited at the bottom of the membrane filtration concentration tank is discharged to the sludge storage tank through a lower discharge outlet discharge pump; the sludge storage tank is used for temporarily storing sludge slurry discharged by the membrane filtration concentration tank and feeding the sludge slurry to four-stage centrifugal solid-liquid separation; the tubular membrane filtration adopts a tubular micro-filtration membrane or a tubular ultrafiltration membrane, the inner diameter flow channel of the tubular membrane is more than 6mm, and the operation mode of internal pressure type, large flow, high flow rate and cross flow interception is adopted, so that the addition of flocculating agent and coagulant aid is reduced or stopped in the reaction of removing hard heavy metals, and suspended matters in washing liquor are completely intercepted. Compared with the traditional softening, sand filtration and hollow fiber membrane ultrafiltration processes, the tubular membrane filtration does not need long-time flocculation precipitation and has short treatment time. Generally, pH after filtration and interception needs to be adjusted back, and the pH of the tubular membrane is adjusted back after membrane filtration, so that redissolution of calcium, magnesium ions and heavy metals and sand filtration and silicon dissolution under a high pH condition are effectively prevented, and the water quality condition is deteriorated; the water washing liquid buffer pool is used for storing washing liquid after flying back water washing dechlorination and water treatment.
Based on foretell tertiary countercurrent washing dechlorination, as the implementation mode of the waste incineration fly ash processing system that this embodiment provided, be equipped with the water injection mouth on the one-level slurrying ash washing bucket for water spray in the one-level slurrying ash washing bucket prevents that one-level slurrying ash washing in-process fly ash from raising dust.
Based on the three-stage countercurrent washing dechlorination, as an implementation mode of the waste incineration fly ash treatment system provided by the embodiment, an acid-base adding port is arranged on the hardness removal reaction tank; a flocculating agent feeding port is arranged on the heavy metal removing reaction tank.
As shown in fig. 1, on the basis of three-stage countercurrent water washing dechlorination, as an embodiment of the waste incineration fly ash treatment system provided in this embodiment, an acid-base addition port is provided on the tubular membrane filtration tank.
As shown in fig. 1, on the basis of three-stage countercurrent water washing dechlorination, as an embodiment of the waste incineration fly ash treatment system provided in this embodiment, a washing liquid pump is provided between the heavy metal removal reaction tank and the membrane filtration concentration tank.
As shown in fig. 1, on the basis of three-stage countercurrent water washing dechlorination, as an embodiment of the waste incineration fly ash treatment system provided in this embodiment, a booster pump is provided between the membrane filtration concentration tank and the tubular membrane filtration tank.
As shown in fig. 1, on the basis of three-stage countercurrent washing and dechlorinating, as an implementation manner of the waste incineration fly ash treatment system provided by the embodiment, the sludge recycling zero discharge unit includes a sludge storage tank and a four-stage solid-liquid separator, sludge slurry is pumped into the sludge storage tank for precipitation, slurry is pumped into the four-stage solid-liquid separator for separation, obtained filtrate is returned to the regulating tank for circular treatment, and obtained filter residue is returned to the multistage countercurrent washing and dechlorinating unit for circular treatment.
As shown in fig. 1, on the basis of three-stage countercurrent water washing and dechlorination, as an embodiment of the waste incineration fly ash treatment system provided by the embodiment, a lower discharge pump is arranged between the membrane filtration concentration tank and the sludge storage tank.
In the above embodiments, the descriptions of the respective embodiments have respective emphasis, and reference may be made to the related descriptions of other embodiments for parts that are not described or illustrated in a certain embodiment.
As shown in fig. 1, the treatment process of the waste incineration fly ash treatment system provided by the embodiment is as follows:
firstly, a multi-stage countercurrent fly ash washing dechlorination process comprises the following steps: municipal solid waste incineration fly ash passes through feed arrangement and carries to one-level slurrying ash washing bucket, go up cloth spray water and prevent slurrying in-process raise dust, the washing water in the one-level slurrying ash washing bucket comes from the well chlorine lotion of second grade centrifugation solid-liquid separation, add liquid caustic soda control pH 10 ~ 11 through adding the medicine pump, prevent that heavy metal and too much calcium ion from being washed out, the thick liquid after the ash is washed in the slurrying is arranged to one-level centrifugation solid-liquid separation, carry out centrifugal separation through horizontal screw centrifuge, high chlorine lotion is arranged to the regulation pond, the lime-ash is arranged to second grade slurrying ash washing bucket.
The wash water in the second-stage pulping ash washing barrel comes from the low-chlorine wash liquor of the third-stage centrifugal solid-liquid separation, the pH is controlled to be 10-11 by adding liquid caustic soda through a dosing pump, heavy metals and excessive calcium ions are prevented from being washed out, the pulp after the pulping ash washing is finished is discharged to the second-stage centrifugal solid-liquid separation, centrifugal separation is carried out through a horizontal screw centrifuge, the middle-chlorine wash liquor is conveyed to the first-stage pulping ash washing barrel, and ash residues are discharged to the third-stage pulping ash washing barrel.
The washing water in the three-stage pulping and ash washing barrel comes from a fresh water supply pipeline, liquid caustic soda is added through a dosing pump to control the pH value to be 10-11, heavy metals and excessive calcium ions are prevented from being washed out, the slurry after the pulping and ash washing is discharged to three-stage centrifugal solid-liquid separation, centrifugal separation is carried out through a horizontal screw centrifuge, low-chlorine washing liquid is conveyed to the two-stage pulping and ash washing barrel, ash is conveyed to a cement kiln to be cooperatively treated, and a certain main material is proportioned and burnt into cement clinker. After each level of fly ash slurry is centrifugally dewatered, the water content is less than or equal to 30 percent, and the water-cement ratio of water supply is 2: 1-4: 1, the chlorine content in the ash after the three-stage water washing dechlorination is less than 1 percent, and the concentration of the high-chlorine washing liquor is about 15 percent.
Secondly, the water treatment process of the fly ash washing liquid comprises the following steps: pumping high-chlorine washing liquor washed by fly ash into an adjusting tank, mixing the high-chlorine washing liquor with centrifugal filtrate subjected to four-stage centrifugal solid-liquid separation for homogenization, pumping the washing liquor after homogenization into a hardness removal reaction tank, adding liquid caustic soda, soda or flue gas and a small amount of flocculant to precipitate calcium and magnesium ions to form flocs, pumping the washing liquor after hardness removal reaction into a heavy metal removal reaction tank, adding agents such as vulcanizing agent and flocculant to perform heavy metal precipitation, pumping the washing liquor after heavy metal removal reaction into a membrane filtration concentration tank, pressurizing by a booster pump, pumping into a tubular membrane for filtration, returning circulating concentrated liquor of the tubular membrane to the membrane filtration concentration tank by adopting an operation mode of internal pressure type, large flow, high flow rate and cross flow interception, discharging sludge slurry deposited at the bottom of the membrane filtration concentration tank into a sludge storage tank for temporary storage by a lower discharge pump, feeding the sludge into a four-stage centrifugal separation after temporary storage, and returning the filtrate subjected to the adjusting tank after centrifugal separation by a horizontal screw centrifuge, the filter residue is returned to the first-stage pulping and ash washing barrel, the sludge is washed and recycled, the calcium content in the dry matter of the precipitated sludge formed by water treatment meets the feeding requirement that the CaO of the cement raw material is more than 50%, and the calcium content can be recycled and used as the feeding material of the cement kiln. The produced water filtered by the tubular membrane is added with hydrochloric acid and adjusted back to Ph being approximately equal to 7, and then the water is pumped to a water washing liquid cache pool, the main components of the washing liquid are about 15% of sodium chloride and potassium chloride, and the potassium salt in the washing liquid is subjected to resource extraction in a mode of further extracting the sodium by high-temperature evaporation and cooling crystallization and extracting the potassium salt.
The embodiment of the system for treating fly ash from waste incineration provided by the embodiment is as follows:
the waste incineration fly ash containing 30% soluble matters is conveyed to a first-stage pulping ash washing barrel through a feeding device, a small amount of spray water is distributed to inhibit dust raising, the washing water in the first-stage pulping ash washing barrel comes from a medium chlorine washing liquid of second-stage centrifugal solid-liquid separation, liquid caustic soda is added through a dosing pump to control the pH value to be 10-11, the slurry after the pulping ash washing is discharged to a first-stage horizontal screw centrifuge for centrifugal separation, the high chlorine washing liquid is discharged to an adjusting tank, and ash residues are discharged to the second-stage pulping ash washing barrel. Washing water in the second-stage pulping ash washing barrel comes from low-chlorine washing liquid obtained by three-stage centrifugal solid-liquid separation, liquid caustic soda is added through a dosing pump to control the pH value to be 10-11, the slurry after pulping ash washing is discharged to a first-stage horizontal screw centrifuge for centrifugal separation, the medium-chlorine washing liquid is conveyed to the first-stage pulping ash washing barrel, and ash residues are discharged to the third-stage pulping ash washing barrel. The washing water in the three-level pulping and ash washing barrel comes from a fresh water supply pipeline, and the water-ash ratio of water supply is 3: 1, adding liquid caustic soda through a dosing pump to control the pH value to be 10-11, discharging the slurry after the completion of pulping and ash washing to a second-stage horizontal screw centrifuge for centrifugal separation, conveying low-chlorine washing liquor to a second-stage pulping and ash washing barrel, conveying ash residues to a cement kiln as a feed ingredient, wherein the chlorine content in the ash residues after the third-stage dechlorination by washing is less than 1%, and the concentration of high-chlorine washing liquor is 12%.
Pumping a high-chlorine washing liquor with the concentration of 12% into an adjusting tank, mixing and homogenizing the high-chlorine washing liquor with a centrifugal filtrate obtained by four-stage centrifugal solid-liquid separation, pumping the homogenized washing liquor into a hardness removal reaction tank, adding liquid caustic soda, soda ash and a small amount of poly-iron to precipitate calcium and magnesium ions to form flocs, pumping the washing liquor obtained after the hardness removal reaction into a heavy metal removal reaction tank, adding an organic vulcanizing agent and poly-iron to perform heavy metal precipitation, pumping the washing liquor obtained after the heavy metal removal reaction into a membrane filtration concentration tank, pressurizing by a booster pump, pumping into a tubular membrane, passing through a membrane, refluxing the circulating concentrated liquor of the tubular membrane into the membrane filtration concentration tank, discharging sludge slurry deposited at the bottom of the membrane filtration concentration tank into a sludge temporary storage tank by a lower discharge port discharge pump, temporarily storing and feeding into a No. 4 horizontal screw centrifuge for centrifugal treatment, returning the treated filtrate to the adjusting tank, returning filter residue to a first-stage ash washing tank, adding hydrochloric acid into produced water obtained by tubular membrane filtration, returning Ph to a water washing liquor buffer tank after Ph is approximately 7, the main components of the washing solution at this time were 12% sodium chloride and potassium chloride.
The above is only the preferred embodiment of the present invention, and the present invention is not limited to the above, the comprehensive process of "multi-stage counter-current rinsing + tubular membrane softening and filtering + sludge recycling" set by the treatment system provided by the present embodiment is a reasonable set verified by the practical engineering of waste incineration fly ash washing liquid treatment, and any action of changing the number of counter-current rinsing stages, adding the type of chemicals, adding redundant process units, or changing the name of the system using the same principle is within the scope of protection right of the present invention.
Claims (10)
1. A waste incineration fly ash treatment system is characterized by comprising:
a multi-stage countercurrent washing dechlorination unit to obtain ash and high-chlorine washing liquor suitable for building material ingredients;
the high-chlorine washing liquid water treatment unit is used for treating the high-chlorine washing liquid to obtain chlorine salt washing liquid for resource recovery; the high-chlorine washing liquid water treatment unit comprises a regulating tank, a hardness removal reaction tank, a heavy metal removal reaction tank, a membrane filtration concentration tank, a tubular membrane filtration tank and a washing liquid cache tank which are sequentially connected; and
and the sludge recycling zero discharge unit is used for receiving and processing the sludge slurry deposited in the membrane filtration concentration tank, the obtained filter residue is returned to the multistage counter-current washing dechlorination unit for circular processing, and the obtained filtrate is returned to the regulating tank of the high-chlorine washing liquid water processing unit for circular processing.
2. The waste incineration fly ash treatment system of claim 1, wherein the multi-stage counter-current water washing dechlorination unit comprises a first-stage water washing dechlorination combination, a second-stage water washing dechlorination combination and a third-stage water washing dechlorination combination.
3. The waste incineration fly ash treatment system of claim 2, wherein the primary water washing dechlorination combination comprises a primary pulping and ash washing barrel and a primary solid-liquid separator, the primary pulping and ash washing barrel is provided with an acid-base dosing pump, and the primary solid-liquid separator is a horizontal screw centrifuge;
the secondary washing dechlorination combination comprises a secondary pulping ash washing barrel and a secondary solid-liquid separator, and the secondary solid-liquid separator is a horizontal screw centrifuge;
the three-stage washing and dechlorinating combination comprises a three-stage pulping and ash washing barrel and a three-stage solid-liquid separator, wherein the three-stage solid-liquid separator is a horizontal screw centrifuge; and a fresh water inlet is formed in the third-stage pulping ash washing barrel.
4. The waste incineration fly ash treatment system of claim 3, wherein the primary pulping and ash washing barrel is provided with a spray water nozzle.
5. The waste incineration fly ash treatment system of claim 1, wherein the hardness removal reaction tank is provided with an acid-base addition port; and a flocculating agent feeding port is arranged on the heavy metal removing reaction tank.
6. The waste incineration fly ash treatment system of claim 1, wherein the tubular membrane filtration tank is provided with an acid-base addition port.
7. The waste incineration fly ash treatment system of claim 1, wherein a washing liquid pump is arranged between the heavy metal removal reaction tank and the membrane filtration concentration tank.
8. The waste incineration fly ash treatment system of claim 1, wherein a booster pump is arranged between the membrane filtration concentration tank and the tubular membrane filtration tank.
9. The waste incineration fly ash treatment system of any one of claims 1 to 8, wherein the sludge recovery zero discharge unit includes a sludge storage tank and a four-stage solid-liquid separator.
10. The waste incineration fly ash treatment system according to claim 9, wherein a lower discharge pump is provided between the membrane filtration concentration tank and the sludge storage tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122737621.6U CN217369706U (en) | 2021-11-09 | 2021-11-09 | Waste incineration fly ash treatment system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122737621.6U CN217369706U (en) | 2021-11-09 | 2021-11-09 | Waste incineration fly ash treatment system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN217369706U true CN217369706U (en) | 2022-09-06 |
Family
ID=83083252
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202122737621.6U Active CN217369706U (en) | 2021-11-09 | 2021-11-09 | Waste incineration fly ash treatment system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN217369706U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116495911A (en) * | 2023-03-07 | 2023-07-28 | 重庆三峰科技有限公司 | Household garbage incineration fly ash washing wastewater pretreatment system and working method thereof |
-
2021
- 2021-11-09 CN CN202122737621.6U patent/CN217369706U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116495911A (en) * | 2023-03-07 | 2023-07-28 | 重庆三峰科技有限公司 | Household garbage incineration fly ash washing wastewater pretreatment system and working method thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN112077128A (en) | Water washing treatment system and method for fly ash | |
| CN106746124A (en) | Garbage flying ash water-washing pre-treatment and cement kiln collaboration disposal of resources system | |
| CN103073163B (en) | Treatment and sludge reduction device and method of de-sizing wastewater | |
| CN206359427U (en) | Garbage flying ash water-washing pre-treatment and cement kiln collaboration disposal of resources system | |
| CN212597897U (en) | Flying dust washing processing system | |
| CN105080936A (en) | Rubbish-fly-ash and cement-kiln cooperation treatment method | |
| CN109264898A (en) | A kind of flying dust multistage dechlorination and water lotion decalcification softening process and its system | |
| CN113479922B (en) | Water washing-plasma melting garbage incineration fly ash recycling device and method | |
| CN105107821A (en) | Co-processing and water reclamation method for garbage fly ash through cement kiln | |
| CN105293782A (en) | System for treating and recycling waste water resulting from lithium battery production | |
| CN110510780A (en) | It is a kind of that cigarette waste water recycling processing unit and method are washed using STRO device | |
| CN217369706U (en) | Waste incineration fly ash treatment system | |
| CN109368901A (en) | A kind of incineration of refuse flyash water washing treating system and method | |
| CN112321020A (en) | Efficient pretreatment system and method for circulating water sewage | |
| CN209583824U (en) | A kind of flying dust multistage dechlorination and water lotion decalcification melded system | |
| CN105859076A (en) | Ozone microbubble air floating concentration device and sludge conditioning and concentration method | |
| CN116283094A (en) | Cooperative treatment method and system for waste incineration fly ash and silicon-rich waste | |
| CN113402050A (en) | Domestic waste incineration fly ash washing liquid pretreatment system | |
| CN111548850B (en) | Method for treating and recycling cutting fluid and recovering precipitated sludge product | |
| CN205500983U (en) | Zero release of desulfurization waste water and resource integrated treatment retrieval and utilization equipment | |
| CN206359382U (en) | A kind of steel plant's high rigidity high alkalinity strong brine processing unit | |
| CN214422450U (en) | Membrane method coal gasification technology waste water treatment and resourceful device | |
| CN209338269U (en) | A kind of incineration of refuse flyash water lotion decalcification system | |
| CN209338311U (en) | A kind of incineration of refuse flyash water washing treating system | |
| CN109279758B (en) | Efficient green mud washing method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |