CN213569979U - Domestic waste burns flying dust washing waste water decalcification pretreatment system - Google Patents
Domestic waste burns flying dust washing waste water decalcification pretreatment system Download PDFInfo
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- CN213569979U CN213569979U CN202022401705.8U CN202022401705U CN213569979U CN 213569979 U CN213569979 U CN 213569979U CN 202022401705 U CN202022401705 U CN 202022401705U CN 213569979 U CN213569979 U CN 213569979U
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- 239000002351 wastewater Substances 0.000 title claims abstract description 41
- 238000005406 washing Methods 0.000 title claims abstract description 32
- 239000010791 domestic waste Substances 0.000 title claims abstract description 7
- 239000000428 dust Substances 0.000 title abstract description 6
- 238000006243 chemical reaction Methods 0.000 claims abstract description 54
- 238000004062 sedimentation Methods 0.000 claims abstract description 34
- 239000010881 fly ash Substances 0.000 claims abstract description 32
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 18
- 230000001105 regulatory effect Effects 0.000 claims abstract description 17
- 238000010517 secondary reaction Methods 0.000 claims abstract description 16
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 12
- 239000003814 drug Substances 0.000 claims abstract description 11
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 8
- 229910052938 sodium sulfate Inorganic materials 0.000 claims abstract description 8
- 235000011152 sodium sulphate Nutrition 0.000 claims abstract description 8
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 108
- 238000001728 nano-filtration Methods 0.000 claims description 42
- 238000002425 crystallisation Methods 0.000 claims description 31
- 230000008025 crystallization Effects 0.000 claims description 30
- 238000001223 reverse osmosis Methods 0.000 claims description 30
- 239000012528 membrane Substances 0.000 claims description 24
- 238000000108 ultra-filtration Methods 0.000 claims description 19
- 239000010802 sludge Substances 0.000 claims description 14
- 150000003839 salts Chemical class 0.000 claims description 12
- 238000001704 evaporation Methods 0.000 claims description 11
- 230000008020 evaporation Effects 0.000 claims description 11
- 238000000926 separation method Methods 0.000 claims description 11
- 238000004064 recycling Methods 0.000 claims description 9
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 7
- 239000013505 freshwater Substances 0.000 claims description 6
- 238000000034 method Methods 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 claims description 2
- 239000002956 ash Substances 0.000 claims 1
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 abstract description 16
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 abstract description 8
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 abstract description 8
- 239000000347 magnesium hydroxide Substances 0.000 abstract description 8
- 229910001862 magnesium hydroxide Inorganic materials 0.000 abstract description 8
- 238000001556 precipitation Methods 0.000 abstract description 8
- 229910001424 calcium ion Inorganic materials 0.000 abstract description 7
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 abstract description 6
- 239000011575 calcium Substances 0.000 abstract description 6
- 230000000694 effects Effects 0.000 abstract description 6
- 229910001425 magnesium ion Inorganic materials 0.000 abstract description 6
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 abstract description 5
- 238000004056 waste incineration Methods 0.000 abstract description 5
- 229910000019 calcium carbonate Inorganic materials 0.000 abstract description 4
- 230000001737 promoting effect Effects 0.000 abstract description 3
- 229940079593 drug Drugs 0.000 abstract description 2
- 239000010440 gypsum Substances 0.000 abstract description 2
- 229910052602 gypsum Inorganic materials 0.000 abstract description 2
- 238000007781 pre-processing Methods 0.000 abstract description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 4
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 3
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000011591 potassium Substances 0.000 description 3
- 229910052700 potassium Inorganic materials 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 2
- 239000012267 brine Substances 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000000265 homogenisation Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 159000000000 sodium salts Chemical class 0.000 description 2
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- NIAGBSSWEZDNMT-UHFFFAOYSA-M tetraoxidosulfate(.1-) Chemical compound [O]S([O-])(=O)=O NIAGBSSWEZDNMT-UHFFFAOYSA-M 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000009388 chemical precipitation Methods 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 229910001414 potassium ion Inorganic materials 0.000 description 1
- 159000000001 potassium salts Chemical class 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
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Abstract
The utility model discloses a domestic waste burns flying dust washing waste water decalcification pretreatment system. The utility model discloses a soften preprocessing unit. The softening pretreatment unit comprises a first regulating tank, a first-stage reaction tank, a second-stage reaction tank, a primary sedimentation tank, a second regulating tank, a third-stage reaction tank and a final sedimentation tank which are connected in sequence; a dosing port of the first-stage reaction tank is connected to a sodium hydroxide medicine tank; the dosing port of the secondary reaction tank is connected to the sodium sulfate medicine tank. The dosing port of the third-stage reaction tank is connected to a sodium carbonate medicine tank. The utility model adopts a structure of three-stage softening and two-stage precipitation to remove calcium and magnesium ions in the waste incineration fly ash washing wastewater to obtain desulfurized gypsum and calcium carbonate products, and the products after adding the medicines in the first-stage reaction tank and the second-stage reaction tank are respectively magnesium hydroxide and calcium sulfate; because the magnesium hydroxide and the calcium sulfate have the effect of mutually promoting precipitation in the same system, calcium and magnesium ions can be removed more fully and quickly in the primary sedimentation tank 4.
Description
Technical Field
The utility model belongs to the technical field of waste incineration flying dust handles, concretely relates to domestic waste incineration flying dust washing wastewater decalcification pretreatment system.
Background
The fly ash washing wastewater generally has the characteristics of high salt content, high hardness, high heavy metal content and the like, the high-chloride wastewater generated by the fly ash washing can corrode subsequent cement kiln co-processing equipment in the production process, the high-hardness wastewater can block the structure of evaporative crystallization equipment, and untreated direct discharge can cause soil biology, plant dehydration death and soil alkalization. Therefore, the research on the advanced treatment process of the fly ash washing wastewater is attracting more and more attention.
Therefore, in order to reduce the pollution to the environment caused by the emission of the washing wastewater of the fly ash, corresponding technical measures are required to realize real zero emission and resource utilization. At present, the fly ash washing wastewater is treated by a chemical precipitation method at home and abroad, and the common process is a neutralization sedimentation-flocculation-clarification method (three-box method), which can effectively remove heavy metal ions and suspended matters, but a large amount of Ca still exists in the wastewater2+、Mg2+The precipitation effect is not good, the high-concentration soluble solid in the wastewater cannot be discharged and is difficult to recycle, the real zero emission is difficult to realize, and the corrosion of equipment in an evaporation system is caused,Pipeline blockage and the like. In order to solve the problems existing in the technology, the utility model is provided.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a domestic waste burns flying dust washing waste water decalcification pretreatment system.
The utility model discloses a soften preprocessing unit. The softening pretreatment unit comprises a first regulating tank, a first-stage reaction tank, a second-stage reaction tank, a primary sedimentation tank, a second regulating tank, a third-stage reaction tank and a final sedimentation tank which are connected in sequence; a dosing port of the first-stage reaction tank is connected to a sodium hydroxide medicine tank; the dosing port of the secondary reaction tank is connected to the sodium sulfate medicine tank. The dosing port of the third-stage reaction tank is connected to a sodium carbonate medicine tank.
Preferably, the utility model discloses still include the evaporation crystallization unit. The evaporative crystallization unit comprises a crystallization concentrated water tank and an evaporative crystallizer. The water inlet of the crystallization concentrated water tank receives the pretreated fly ash washing wastewater. And a water outlet of the crystallization concentrated water tank is connected with an input port of the evaporation crystallizer through a fifth lift pump.
Preferably, an ultrafiltration unit is arranged between the softening pretreatment unit and the evaporative crystallization unit. The ultrafiltration unit comprises an ultrafiltration water inlet tank and a tubular membrane system. The water inlet of the ultrafiltration water inlet tank is connected with the water outlet at the top of the final sedimentation tank. The water outlet of the ultrafiltration water inlet tank is connected with the input port of the tubular membrane system through a second lift pump.
Preferably, a nanofiltration salt separation unit is arranged between the ultrafiltration unit and the evaporation crystallization unit; the nanofiltration salt separation unit comprises a nanofiltration water inlet tank and a nanofiltration device. The water inlet of the nanofiltration water inlet tank is connected with the filtered water outlet of the tubular membrane system. A water outlet of the nanofiltration water inlet tank is connected with an input port of the nanofiltration device through a third lift pump; the concentrated water outlet of the nanofiltration device is connected to the water inlet of the secondary reaction tank through a nanofiltration sulfate radical recycling pipeline (11-1).
Preferably, a membrane concentration unit is arranged between the nanofiltration salt separation unit and the evaporative crystallization unit; the membrane concentration unit comprises a reverse osmosis water inlet tank and a high-pressure reverse osmosis device. The water inlet of the reverse osmosis water inlet tank is connected with the water outlet of the nanofiltration device. The water outlet of the reverse osmosis water inlet tank is connected with the input port of the high-pressure reverse osmosis device through a fourth lift pump; the fresh water outlet of the high-pressure reverse osmosis device is connected to the water inlet of the secondary reaction tank through a high-pressure reverse osmosis produced water recycling pipeline (13-1). The concentrated water outlet of the high-pressure reverse osmosis device is connected to the water inlet of the crystallization concentrated water tank.
Preferably, the first-stage reaction tank, the second-stage reaction tank and the third-stage reaction tank are internally provided with stirrers.
Preferably, the input port of the first regulating tank is connected with a fly ash washing wastewater inlet pipe.
Preferably, a first lift pump is arranged between the first regulating tank and the first-stage reaction tank.
Preferably, a bottom sludge outlet of the primary sedimentation tank is connected with a first plate-and-frame filter press through a first sludge pump.
Preferably, the bottom sludge outlet of the final sedimentation tank is connected with a second plate-and-frame filter press through a second sludge pump.
The utility model has the advantages that:
1. the utility model adopts a structure of three-stage softening and two-stage precipitation to remove calcium and magnesium ions in the waste incineration fly ash washing wastewater to obtain desulfurized gypsum and calcium carbonate products, and the products after adding the medicines in the first-stage reaction tank and the second-stage reaction tank are respectively magnesium hydroxide and calcium sulfate; because the magnesium hydroxide and the calcium sulfate have the effect of mutually promoting precipitation in the same system, calcium and magnesium ions can be removed more fully and quickly in the primary sedimentation tank 4.
2. The utility model discloses a nanofiltration is divided salt, membrane concentration, the recoverable high-quality industrial sodium salt of evaporative crystallization unit, realizes the zero release and the resource utilization of waste water.
3. The utility model discloses a receive and strain sulfate radical retrieval and utilization pipeline and flow back the sulfate radical ion to the second grade reaction tank in, avoided the sulfate radical ion as new pollutant output to play the effect of practicing thrift the sodium sulfate consumption.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
In the figure: 1-a first conditioning tank; 1-1-a fly ash washing wastewater inlet pipe; a-1-lift pump; 2-a first-stage reaction tank; 3-a secondary reaction tank; 4-primary settling tank; b-1-sludge pump; c-1-plate and frame filter press; 5-a second regulating reservoir; 6-third-stage reaction tank; 7-final sedimentation tank; b-2-sludge pump; c-2-plate and frame filter press; 8-ultrafiltration water inlet tank; a-2-lift pump; 9-a tubular membrane system; 10-nanofiltration water inlet tank; a-3-lift pump; 11-a nanofiltration device; an 11-1-nanofiltration sulfate radical recycling pipeline; 12-reverse osmosis water inlet tank; a-4-lift pump; 13-a high pressure reverse osmosis unit; 13-1-high pressure reverse osmosis produced water recycling pipeline; 14-crystallization concentrate tank; a-5-lift pump; 15-evaporative crystallizer.
Detailed Description
The technical solution of the present invention is described in detail and specifically by the following embodiments to make the present invention better understood, but the following embodiments do not limit the scope of the present invention.
As shown in fig. 1, a domestic waste incineration fly ash washing wastewater decalcification pretreatment system comprises a softening pretreatment unit, an ultrafiltration unit, a nanofiltration salt separation unit, a membrane concentration unit and an evaporation crystallization unit which are sequentially connected.
The softening pretreatment unit adopts a novel three-stage softening and two-stage precipitation system and comprises a first regulating tank 1, a first-stage reaction tank 2, a second-stage reaction tank 3, a primary settling tank 4, a second regulating tank 5, a third-stage reaction tank 6 and a final settling tank 7; stirrers are arranged in the first-stage reaction tank 2, the second-stage reaction tank 3 and the third-stage reaction tank 6. The input port of the first adjusting tank 1 is connected with a fly ash washing wastewater inlet pipe 1-1; the water outlet of the first regulating tank 1 is connected to the first-stage reaction tank 2 through a first lift pump A-1; a dosing port of the first-stage reaction tank 2 is connected to a sodium hydroxide pot and is used for dosing sodium hydroxide into the first-stage reaction tank 2 for magnesium removal; the water outlet of the first-stage reaction tank 2 is connected with the water inlet of the second-stage reaction tank 3; a dosing port of the second-stage reaction tank 3 is connected to a sodium sulfate dosing tank and is used for dosing sodium sulfate into the first-stage reaction tank 2 for decalcification; the water outlet of the secondary reaction tank 3 is connected with the water inlet of the primary sedimentation tank 4; the primary sedimentation tank 4 is used for carrying out solid-liquid separation on the wastewater from the primary reaction tank 2 and the secondary reaction tank 3, and the magnesium hydroxide and the calcium sulfate can mutually promote sedimentation in the primary sedimentation tank 4;
the bottom sludge outlet of the primary sedimentation tank 4 is connected with a first plate-and-frame filter press C-1 through a first sludge pump B-1; the first plate-and-frame filter press C-1 is used for dehydrating magnesium hydroxide and calcium sulfate which are precipitated and separated from the primary sedimentation tank 4. A water outlet at the top of the primary sedimentation tank 4 is connected with a water inlet of a second regulating tank 5; the water outlet of the second regulating tank 5 is connected with the water inlet of the third-stage reaction tank 6; a dosing port of the third-stage reaction tank 6 is connected to a sodium carbonate dosing tank and is used for dosing sodium carbonate into the first-stage reaction tank 2 for deep decalcification; the water outlet of the third-stage reaction tank 6 is connected with the final sedimentation tank 7; the bottom sludge outlet of the final sedimentation tank 7 is connected with a second plate-and-frame filter press C-2 through a second sludge pump B-2; and the second plate-and-frame filter press C-2 is used for dehydrating the calcium carbonate precipitated and separated from the final sedimentation tank 7.
The ultrafiltration unit comprises an ultrafiltration water inlet tank 8 and a tubular membrane system 9. The water inlet of the ultrafiltration water inlet tank 8 is connected with the water outlet at the top of the final sedimentation tank 7. The water outlet of the ultrafiltration water inlet tank 8 is connected with the input port of the tubular membrane system 9 through a second lift pump A-2; a tubular membrane system 9 is used to filter out residual solid particles.
The nanofiltration salt separation unit comprises a nanofiltration water inlet tank 10 and a nanofiltration device 11. The water inlet of the nanofiltration water inlet tank 10 is connected with the filtered water outlet of the tubular membrane system 9. A water outlet of the nanofiltration water inlet tank 10 is connected with an input port of the nanofiltration device 11 through a third lift pump A-3; a concentrated water outlet of the nanofiltration device 11 is connected to a water inlet of the secondary reaction tank 3 through a nanofiltration sulfate recycling pipeline 11-1. The nanofiltration membrane in the nanofiltration device 11 can prevent bivalent sulfate ions from passing through, but not monovalent sodium ions, monovalent potassium ions and monovalent chloride ions from passing through, so that residual sulfate ions can flow back to the secondary reaction tank 3 through the nanofiltration sulfate recycling pipeline 11-1, the sulfate ions are prevented from being output as new pollutants, and the effect of saving the consumption of sodium sulfate is achieved.
The membrane concentration unit comprises a reverse osmosis water inlet tank 12 and a high pressure reverse osmosis device 13. The water inlet of the reverse osmosis water inlet tank 12 is connected with the water outlet of the nanofiltration device 11. A water outlet of the reverse osmosis water inlet tank 12 is connected with an input port of the high-pressure reverse osmosis device 13 through a fourth lift pump A-4; the fresh water outlet of the high-pressure reverse osmosis device 13 is connected to the water inlet of the secondary reaction tank 3 through a high-pressure reverse osmosis produced water recycling pipeline 13-1.
When the fly ash washing liquid passes through the high-pressure reverse osmosis device 13, when the pressure applied to one side of the membrane exceeds the osmotic pressure of water, the water can reversely permeate against the natural permeation direction, so that the permeated fresh water is obtained at the low-pressure side of the membrane, the concentrated water containing sodium, potassium and chloride ions is obtained at the high-pressure side of the membrane, and the fresh water without sodium, potassium and chloride ions flows back into the secondary reaction tank 3 for reuse, thereby saving water and improving the efficiency of subsequent evaporative crystallization.
The evaporative crystallization unit includes a crystallization concentrate tank 14 and an evaporative crystallizer 15. The water inlet of the crystallization concentrate tank 14 is connected with the concentrate outlet of the high-pressure reverse osmosis device 13. A water outlet of the crystallization concentrated water tank 14 is connected with an input port of the evaporation crystallizer 15 through a fifth lift pump A-5; the evaporative crystallizer 15 performs evaporative crystallization on the input fly ash water washing liquid containing sodium, potassium and chloride ions to obtain industrial refined dry salts (sodium salts and potassium salts).
The working principle of the utility model is as follows:
the fly ash wastewater enters a first regulating tank 1 from a fly ash washing wastewater inlet pipe 1-1 for homogenization and uniform amount, then sequentially passes through a first-stage reaction tank 2 and a second-stage reaction tank 3, and enters a primary sedimentation tank 4 for sedimentation and separation; sodium hydroxide is continuously added into the first-stage reaction tank 2, sodium sulfate is continuously added into the second-stage reaction tank 3, so that magnesium hydroxide and calcium sulfate precipitate are formed in the primary sedimentation tank 4, and calcium and magnesium ions can be sufficiently and quickly removed from the primary sedimentation tank 4 because the magnesium hydroxide and the calcium sulfate have the effect of mutually promoting precipitation in the same system.
The fly ash wastewater output by the primary sedimentation tank 4 enters a second regulating tank 5 for homogenization and uniform amount, then sequentially passes through a third-stage reaction tank 6, and enters a final sedimentation tank 7 for sedimentation and separation; sodium carbonate is continuously added into the third-stage reaction tank 6, so that calcium ions which are not precipitated in the primary precipitation tank 4 are further combined with carbonate ions to form calcium carbonate precipitates, and the removal rate of the calcium ions is further improved.
The fly ash wastewater output by the final sedimentation tank 7 enters a tubular membrane system 9 through an ultrafiltration water inlet tank 8 to filter out residual solid particles in the wastewater;
the fly ash wastewater output by the tubular membrane system 9 enters a nanofiltration device 11 through a nanofiltration water inlet tank 10 to recover sulfate ions to a secondary reaction tank 3;
the fly ash wastewater output by the nanofiltration device 11 enters a high-pressure reverse osmosis device 13 through a reverse osmosis water inlet tank 12 to recover fresh water to a secondary reaction tank 3, and a strong brine solution is output to a crystallization strong brine tank 14.
The crystallization concentrated water tank 14 inputs the salt solution into an evaporative crystallizer 15 for evaporative crystallization, and industrial refined dry salt is recovered.
Claims (10)
1. A domestic waste burns the ash washing wastewater decalcification preconditioning system of fly ash, including softening the preconditioning unit; the method is characterized in that: the softening pretreatment unit comprises a first regulating tank (1), a first-stage reaction tank (2), a second-stage reaction tank (3), a primary sedimentation tank (4), a second regulating tank (5), a third-stage reaction tank (6) and a final sedimentation tank (7) which are connected in sequence; a dosing port of the first-stage reaction tank (2) is connected to a sodium hydroxide medicine tank; a dosing port of the secondary reaction tank (3) is connected to a sodium sulfate medicine tank; the dosing port of the third-stage reaction tank (6) is connected to a sodium carbonate medicine tank.
2. The system for decalcifying and pretreating washing wastewater of fly ash from incineration of household garbage according to claim 1, wherein: also comprises an evaporation crystallization unit; the evaporative crystallization unit comprises a crystallization concentrated water tank (14) and an evaporative crystallizer (15); a water inlet of the crystallization concentrated water tank (14) receives the pretreated fly ash washing wastewater; the water outlet of the crystallization concentrated water tank (14) is connected with the input port of the evaporation crystallizer (15) through a fifth lift pump (A-5).
3. The system for decalcifying and pretreating washing wastewater of fly ash from incineration of household garbage according to claim 2, wherein: an ultrafiltration unit is arranged between the softening pretreatment unit and the evaporation crystallization unit; the ultrafiltration unit comprises an ultrafiltration water inlet tank (8) and a tubular membrane system (9); the water inlet of the ultrafiltration water inlet tank (8) is connected with the water outlet at the top of the final sedimentation tank (7); the water outlet of the ultrafiltration water inlet tank (8) is connected with the input port of the tubular membrane system (9) through a second lift pump (A-2).
4. The system for decalcifying and pretreating washing wastewater of fly ash from incineration of household garbage according to claim 3, wherein: a nanofiltration salt separation unit is arranged between the ultrafiltration unit and the evaporation crystallization unit; the nanofiltration salt separation unit comprises a nanofiltration water inlet tank (10) and a nanofiltration device (11); a water inlet of the nanofiltration water inlet tank (10) is connected with a filtered water outlet of the tubular membrane system (9); a water outlet of the nanofiltration water inlet tank (10) is connected with an input port of the nanofiltration device (11) through a third lift pump (A-3); a concentrated water outlet of the nanofiltration device (11) is connected to a water inlet of the secondary reaction tank (3) through a nanofiltration sulfate recycling pipeline (11-1).
5. The system for decalcifying and pretreating washing wastewater of fly ash from incineration of household garbage according to claim 4, wherein: a membrane concentration unit is arranged between the nanofiltration salt separation unit and the evaporation crystallization unit; the membrane concentration unit comprises a reverse osmosis water inlet tank (12) and a high-pressure reverse osmosis device (13); a water inlet of the reverse osmosis water inlet tank (12) is connected with a water production outlet of the nanofiltration device (11); a water outlet of the reverse osmosis water inlet tank (12) is connected with an input port of the high-pressure reverse osmosis device (13) through a fourth lift pump (A-4); a fresh water outlet of the high-pressure reverse osmosis device (13) is connected to a water inlet of the secondary reaction tank (3) through a high-pressure reverse osmosis produced water recycling pipeline (13-1); the concentrated water outlet of the high-pressure reverse osmosis device (13) is connected to the water inlet of the crystallization concentrated water tank (14).
6. The system for decalcifying and pretreating washing wastewater of fly ash from incineration of household garbage according to claim 1, wherein: stirrers are arranged in the first-stage reaction tank (2), the second-stage reaction tank (3) and the third-stage reaction tank (6).
7. The system for decalcifying and pretreating washing wastewater of fly ash from incineration of household garbage according to claim 1, wherein: the input port of the first adjusting tank (1) is connected with a fly ash washing wastewater inlet pipe (1-1).
8. The system for decalcifying and pretreating washing wastewater of fly ash from incineration of household garbage according to claim 1, wherein: a first lift pump (A-1) is arranged between the first regulating tank (1) and the first-stage reaction tank (2).
9. The system for decalcifying and pretreating washing wastewater of fly ash from incineration of household garbage according to claim 1, wherein: and a sludge outlet at the bottom of the primary sedimentation tank (4) is connected with a first plate-and-frame filter press (C-1) through a first sludge pump (B-1).
10. The system for decalcifying and pretreating washing wastewater of fly ash from incineration of household garbage according to claim 1, wherein: and a sludge outlet at the bottom of the final sedimentation tank (7) is connected with a second plate-and-frame filter press (C-2) through a second sludge pump (B-2).
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114804439A (en) * | 2022-05-23 | 2022-07-29 | 安徽海螺环保集团有限公司 | Pretreatment system for fly ash washing liquid |
| CN115490355A (en) * | 2022-08-22 | 2022-12-20 | 安徽普朗膜技术有限公司 | Coal fired power plant desulfurization effluent treatment plant |
| CN115626731A (en) * | 2022-10-17 | 2023-01-20 | 北京中科国润环保科技有限公司 | System and method for reducing hardness of high-salinity wastewater by utilizing three-stage reaction |
| 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 |
-
2020
- 2020-10-26 CN CN202022401705.8U patent/CN213569979U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114804439A (en) * | 2022-05-23 | 2022-07-29 | 安徽海螺环保集团有限公司 | Pretreatment system for fly ash washing liquid |
| CN115490355A (en) * | 2022-08-22 | 2022-12-20 | 安徽普朗膜技术有限公司 | Coal fired power plant desulfurization effluent treatment plant |
| CN115626731A (en) * | 2022-10-17 | 2023-01-20 | 北京中科国润环保科技有限公司 | System and method for reducing hardness of high-salinity wastewater by utilizing three-stage reaction |
| 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 |
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