CN118373430A - Resource utilization treatment method and system based on biomass combustion fly ash - Google Patents
Resource utilization treatment method and system based on biomass combustion fly ash Download PDFInfo
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- CN118373430A CN118373430A CN202311858720.7A CN202311858720A CN118373430A CN 118373430 A CN118373430 A CN 118373430A CN 202311858720 A CN202311858720 A CN 202311858720A CN 118373430 A CN118373430 A CN 118373430A
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- 239000002028 Biomass Substances 0.000 title claims abstract description 93
- 238000002485 combustion reaction Methods 0.000 title claims abstract description 87
- 238000000034 method Methods 0.000 title claims abstract description 43
- 239000010881 fly ash Substances 0.000 title claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 93
- 238000001704 evaporation Methods 0.000 claims abstract description 80
- 239000012047 saturated solution Substances 0.000 claims abstract description 75
- 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 claims abstract description 74
- 239000011734 sodium Substances 0.000 claims abstract description 74
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 74
- 239000000243 solution Substances 0.000 claims abstract description 67
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 60
- 239000013078 crystal Substances 0.000 claims abstract description 54
- BITYAPCSNKJESK-UHFFFAOYSA-N potassiosodium Chemical compound [Na].[K] BITYAPCSNKJESK-UHFFFAOYSA-N 0.000 claims abstract description 53
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000011591 potassium Substances 0.000 claims abstract description 50
- 229910052700 potassium Inorganic materials 0.000 claims abstract description 50
- 239000007788 liquid Substances 0.000 claims abstract description 47
- XAEFZNCEHLXOMS-UHFFFAOYSA-M potassium benzoate Chemical compound [K+].[O-]C(=O)C1=CC=CC=C1 XAEFZNCEHLXOMS-UHFFFAOYSA-M 0.000 claims abstract description 43
- 238000005406 washing Methods 0.000 claims abstract description 43
- 239000007864 aqueous solution Substances 0.000 claims abstract description 34
- 239000000377 silicon dioxide Substances 0.000 claims abstract description 30
- 235000012239 silicon dioxide Nutrition 0.000 claims abstract description 30
- 159000000000 sodium salts Chemical class 0.000 claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 21
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000000292 calcium oxide Substances 0.000 claims abstract description 20
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims abstract description 20
- 239000000395 magnesium oxide Substances 0.000 claims abstract description 18
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims abstract description 18
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000012535 impurity Substances 0.000 claims abstract description 11
- 238000009388 chemical precipitation Methods 0.000 claims abstract description 7
- 230000008020 evaporation Effects 0.000 claims description 69
- 239000002956 ash Substances 0.000 claims description 63
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 48
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 46
- 238000004062 sedimentation Methods 0.000 claims description 28
- 239000001103 potassium chloride Substances 0.000 claims description 24
- 235000011164 potassium chloride Nutrition 0.000 claims description 24
- 239000011780 sodium chloride Substances 0.000 claims description 23
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims description 18
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 claims description 18
- 239000000126 substance Substances 0.000 claims description 16
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 15
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 12
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 10
- 238000007599 discharging Methods 0.000 claims description 9
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 claims description 6
- CHWRSCGUEQEHOH-UHFFFAOYSA-N potassium oxide Chemical compound [O-2].[K+].[K+] CHWRSCGUEQEHOH-UHFFFAOYSA-N 0.000 claims description 6
- 229910001950 potassium oxide Inorganic materials 0.000 claims description 6
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 claims description 6
- 229910001948 sodium oxide Inorganic materials 0.000 claims description 6
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 5
- 239000000920 calcium hydroxide Substances 0.000 claims description 5
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 5
- 229910052742 iron Inorganic materials 0.000 claims description 5
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims description 5
- 239000000347 magnesium hydroxide Substances 0.000 claims description 5
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims description 5
- 238000003672 processing method Methods 0.000 claims description 5
- 230000002378 acidificating effect Effects 0.000 claims description 4
- 239000012459 cleaning agent Substances 0.000 claims description 4
- 230000008569 process Effects 0.000 description 13
- 239000000446 fuel Substances 0.000 description 9
- 229920006395 saturated elastomer Polymers 0.000 description 7
- 241000196324 Embryophyta Species 0.000 description 6
- 238000000605 extraction Methods 0.000 description 5
- 239000002154 agricultural waste Substances 0.000 description 4
- 239000003513 alkali Substances 0.000 description 4
- 229910052500 inorganic mineral Inorganic materials 0.000 description 4
- 235000010755 mineral Nutrition 0.000 description 4
- 239000011707 mineral Substances 0.000 description 4
- 238000001556 precipitation Methods 0.000 description 4
- 239000003337 fertilizer Substances 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 239000008367 deionised water Substances 0.000 description 2
- 229910021641 deionized water Inorganic materials 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000465 moulding Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- -1 sawdust Substances 0.000 description 2
- 241000609240 Ambelania acida Species 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 229910001579 aluminosilicate mineral Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000010905 bagasse Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000002551 biofuel Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 239000012024 dehydrating agents Substances 0.000 description 1
- 239000002274 desiccant Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000010409 ironing Methods 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 description 1
- 229910052939 potassium sulfate Inorganic materials 0.000 description 1
- 235000011151 potassium sulphates Nutrition 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
Classifications
-
- 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
- C01D3/08—Preparation by working up natural or industrial salt mixtures or siliceous minerals
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/70—Chemical treatment, e.g. pH adjustment or oxidation
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/113—Silicon oxides; Hydrates thereof
- C01B33/12—Silica; Hydrates thereof, e.g. lepidoic silicic acid
- C01B33/18—Preparation of finely divided silica neither in sol nor in gel form; After-treatment thereof
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/20—Silicates
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Toxicology (AREA)
- Health & Medical Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Materials Engineering (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention relates to the technical field of biomass combustion ash resource utilization, and particularly discloses a resource utilization treatment method and a system based on biomass combustion ash, wherein the method comprises the following steps: s1, carrying out water washing treatment on biomass combustion ash, dissolving part of biomass combustion ash into water, and generating chemical reaction to obtain an aqueous solution; s2, removing impurities from the aqueous solution obtained in the step S1 by a chemical precipitation method, and removing calcium oxide and magnesium oxide in the aqueous solution to obtain a potassium-sodium solution; s3, evaporating and concentrating the potassium-sodium solution obtained in the step S2 to obtain a saturated solution containing potassium and sodium; s4, carrying out solid-liquid separation on the saturated solution containing potassium and sodium obtained in the step S3 to obtain potassium salt crystals and a saturated solution containing sodium respectively; s5, obtaining sodium salt crystals after the saturated solution containing sodium in the S4 is subjected to the S3, and effectively extracting potassium salt crystals, sodium salt crystals and silicon dioxide from biomass combustion ash, so that the biomass combustion ash is comprehensively extracted by utilizing resources.
Description
Technical Field
The invention relates to the technical field of biomass combustion ash resource utilization, in particular to a resource utilization treatment method and a system based on biomass combustion ash.
Background
The potassium salt is a mineral containing potassium and is divided into a soluble potassium salt mineral and an insoluble potassium containing aluminosilicate mineral, wherein the main products of the potassium salt product used as potassium fertilizer comprise potassium chloride and potassium sulfate, the potassium salt product is one of three fertilizers which are indispensable to agriculture, only a small amount of the potassium salt product is used as a chemical raw material, and the potassium salt product is applied to industry, and the potassium salt resource reserve is not large and the requirement of agriculture on the potassium fertilizer is difficult to meet, so the potassium salt mineral is classified as one of the urgent mineral types by China.
Biomass fuel is characterized in that biomass materials are combusted to be used as fuel, generally agricultural and forestry waste (such as straw, sawdust, bagasse and rice chaff) is mainly different from fossil fuel, in the application of biomass fuel, biomass molding fuel is mainly used as raw material, agricultural and forestry waste is used as raw material, various molding novel clean fuel which can be directly combusted is prepared through processes of crushing, mixing, extrusion, drying and the like, direct combustion is a most common, direct and commercially feasible way for extracting energy from biomass, and various types of biofuels are almost utilized from energy supply plants to agricultural residues and waste materials in a combustion system, and in the combustion process, the method is generally divided into 4 processes:
(1) The evaporation process of water in biomass, the cell structure of agricultural waste still contains 15% -20% of water;
(2) The release of gas/vaporising components from the biomass, not just gases released in the stack, but also part of the vapour mixture available for combustion and vaporised tar;
(3) The released gas burns with oxygen in the air at high temperature and produces a jet of pyrolysis products;
(4) The remainder of the agricultural waste (mainly carbon) burns and under complete combustion conditions, the energy in the agricultural waste is completely released and the agricultural waste is completely converted to ash.
However, the biomass fuel is treated by the direct combustion method, and excessive ashes are generated, so that the biomass fuel belongs to high-pollution fuel.
For example, the Chinese patent with the patent name of "method for comprehensively utilizing plant ash of biomass power plant" has the issued publication number of CN102744238A, and discloses a method for comprehensively utilizing plant ash of biomass power plant, which comprises the steps of extracting potassium salt and preparing adsorbent, firstly, leaching plant ash generated by combustion of the power plant by deionized water, dissolving soluble potassium salt in the plant ash, carrying out solid-liquid separation, and evaporating and crystallizing potassium-sodium solution to obtain potassium salt; then, the plant ash residue after potassium salt extraction is activated by alkali, washed to be neutral by acid or deionized water, dried, milled, screened and granulated to prepare the adsorbent.
How to comprehensively utilize the resources of the ashes generated after the combustion of the biomass fuel is a technical problem which needs to be solved by the current technicians.
Disclosure of Invention
The invention aims to provide a resource utilization treatment method and a system based on biomass combustion fly ash, which solve the problems in the background technology.
In order to achieve the above object, the first aspect of the present application provides a method for resource utilization treatment based on biomass combustion fly ash, comprising the steps of:
S1, carrying out water washing treatment on biomass combustion ash, dissolving part of the biomass combustion ash into water, and obtaining a dissolved part as an aqueous solution after chemical reaction; the undissolved part is an insoluble substance, the insoluble substance comprises silicon dioxide and ferric oxide, the insoluble substance is added with an acidic cleaning agent to remove the ferric oxide to obtain high-purity silicon dioxide, and the high-purity silicon dioxide is added with an alkaline element to generate silicate and water;
S2, removing impurities from the aqueous solution obtained in the step S1 by a chemical precipitation method, and removing calcium oxide and magnesium oxide in the aqueous solution to obtain a potassium-sodium solution;
s3, evaporating and concentrating the potassium-sodium solution obtained in the step S2 to obtain a saturated solution containing potassium and sodium;
s4, carrying out solid-liquid separation on the saturated solution containing potassium and sodium obtained in the step S3 to obtain potassium salt crystals and a saturated solution containing sodium respectively;
s5, carrying out the S3 on the saturated solution containing sodium in the S4 again to obtain sodium salt crystals.
Preferably, in S1, the main component of the aqueous solution includes potassium hydroxide, sodium hydroxide, calcium hydroxide and magnesium hydroxide.
Preferably, in the step S1, the main components of the biomass combustion ash include the following components in percentage by mass: 55% -60% of silicon dioxide, 4% -9% of calcium oxide, 15% -23% of potassium oxide, 1% -6% of ferric oxide, 3% -4% of magnesium oxide and 1% of sodium oxide.
Preferably, in the step S2, the main components of the potassium-sodium solution include sodium chloride and potassium chloride.
Preferably, in the step S3, the main components of the saturated solution containing potassium and sodium are 90% of potassium chloride and 4.5% of sodium chloride by mass percent.
Preferably, the main component of the saturated solution containing potassium and sodium is consistent with the main component of the potassium and sodium solution, and the concentration of the saturated solution containing potassium and sodium is higher than the concentration of the potassium and sodium solution.
The second aspect of the present application provides a resource utilization processing system based on biomass combustion fly ash, the resource utilization processing system being configured to implement the above-described resource utilization processing method, the resource utilization processing system comprising: a water washing tank, a reaction tank, a sedimentation tank, an evaporation crystallizer and a solid-liquid separator;
The washing tank is used for carrying out washing treatment on biomass combustion ash to enable partial components of the biomass combustion ash to generate chemical reaction with water, wherein a water solution is formed by a dissolved part of the biomass combustion ash, undissolved parts of the biomass combustion ash are discharged into the reaction tank to be subjected to iron removal treatment, the water solution is discharged into the sedimentation tank, the sedimentation tank is used for carrying out chemical sedimentation on the water solution to remove calcium oxide and magnesium oxide and obtain potassium sodium solution, the potassium sodium solution is discharged into the evaporation crystallizer, the evaporation crystallizer is used for carrying out evaporation concentration on the potassium sodium solution to obtain saturated solution containing potassium sodium, a liquid outlet of the evaporation crystallizer is communicated with the solid-liquid separator, the solid-liquid separator is used for carrying out solid-liquid separation on the saturated solution containing potassium sodium to obtain potassium salt crystals and saturated solution containing sodium after separation, and the saturated solution containing sodium is discharged into the evaporation crystallizer again to obtain sodium salt crystals after evaporation concentration.
Preferably, a first outlet and a second outlet are respectively arranged outside the washing tank, the first outlet is used for discharging the aqueous solution into the sedimentation tank, and the second outlet is used for discharging insoluble matters into the reaction tank.
Preferably, the evaporation crystallizer is respectively provided with a heater, a temperature detector and a temperature sensor, the temperature detector is used for detecting the internal temperature of the evaporation crystallizer, the heater is used for heating the inside of the evaporation crystallizer, the temperature sensor is used for sensing and controlling the heater to heat or stop heating, and the highest heating temperature of the heater is 100 ℃.
Preferably, the resource utilization treatment system further comprises a condensate water processor, wherein a water inlet of the condensate water processor is communicated with the evaporation crystallizer, and a water outlet of the condensate water processor is respectively communicated with the water washing tank and the sedimentation tank.
Compared with the prior art, the invention provides a resource utilization treatment method and a system based on biomass combustion fly ash, and the method has the beneficial effects that: the method comprises the steps of washing biomass combustion ash with water in a water washing tank, dissolving part to obtain aqueous solution, chemically precipitating the aqueous solution in a precipitation tank to remove impurities to obtain potassium sodium solution, removing impurities of calcium oxide and ferric oxide in the potassium sodium solution in the chemical precipitation process, introducing the potassium sodium solution with the impurities of the calcium oxide and the ferric oxide removed into an evaporation crystallizer to carry out evaporation crystallization treatment, evaporating and concentrating the potassium sodium solution by the evaporation crystallizer to obtain saturated solution containing potassium sodium, discharging the saturated solution of potassium sodium into a solid-liquid separator to carry out solid-liquid separation to obtain potassium salt crystals and saturated solution containing sodium, extracting the potassium salt crystals from the biomass combustion ash, evaporating and concentrating the saturated solution containing sodium again by the evaporation crystallizer to obtain sodium salt crystals, extracting the sodium salt crystals from the biomass combustion ash, wherein in the water washing and dissolving process, the insoluble part is insoluble containing the following silicon dioxide and ferric oxide, removing the ferric oxide after the acid washing treatment to obtain high-purity silicon dioxide, thereby realizing the extraction of silicon dioxide in the biomass combustion ash, adding the saturated solution of potassium sodium salt crystals into a solid-liquid separator to carry out solid-liquid separation to obtain the potassium salt crystals and the saturated solution, and carrying out the extraction of the alkali silicon dioxide to obtain the sodium salt crystals, thereby realizing the full extraction of the potassium salt crystals in the biomass combustion ash and the biomass combustion ash.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings that are needed in the embodiments or the description of the prior art will be briefly described below, it being obvious that the drawings in the following description are only some embodiments of the present invention, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a flow chart of a resource utilization processing method of the present invention.
FIG. 2 is a schematic diagram of a resource utilization processing system of the present invention.
Detailed Description
Preferred embodiments of the present application will be described in more detail below with reference to the accompanying drawings. While the preferred embodiments of the present application have been illustrated in the drawings, it should be understood that the present application may be embodied in various forms and should not be limited to the embodiments set forth herein, but rather, these embodiments are provided so that this application will be thorough and complete, and will fully convey the scope of the application to those skilled in the art.
The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the application. As used in this specification and the appended claims, the singular forms "a," "an," and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise. It should also be understood that the term "and/or" as used herein refers to and encompasses any or all possible combinations of one or more of the associated listed items.
It will be understood that when an element is referred to as being "mounted" or "disposed" on another element, it can be directly on the other element or be indirectly on the other element. When an element is referred to as being "connected to" another element, it can be directly connected to the other element or be indirectly connected to the other element.
In the description of the present application, it should be understood that the terms "thickness," "upper," "lower," "front," "rear," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like indicate or are based on the orientation or positional relationship shown in the drawings, merely to facilitate description of the present application and simplify the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as limiting the present application; furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated; thus, the definition of "first", "second" is for descriptive purposes only and is not to be construed as indicating or implying relative importance or implicitly including one or more such features.
In the description of the present application, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communicated with the inside of two elements or the interaction relationship of the two elements. The specific meaning of the above terms in the present application can be understood by those of ordinary skill in the art according to the specific circumstances.
The following describes the technical scheme of the embodiment of the present application in detail with reference to the accompanying drawings.
Referring to fig. 1 to 2, a resource utilization treatment method based on biomass combustion fly ash includes the steps of:
S1, carrying out water washing treatment on biomass combustion ash, dissolving part of the biomass combustion ash into water, and obtaining a dissolved part as an aqueous solution after chemical reaction; the undissolved part is an insoluble substance, the insoluble substance comprises silicon dioxide and ferric oxide, the insoluble substance is added with an acidic cleaning agent to remove the ferric oxide to obtain high-purity silicon dioxide, and the high-purity silicon dioxide is added with an alkaline element to generate silicate and water;
S2, removing impurities from the aqueous solution obtained in the step S1 by a chemical precipitation method, and removing calcium oxide and magnesium oxide in the aqueous solution to obtain a potassium-sodium solution;
s3, evaporating and concentrating the potassium-sodium solution obtained in the step S2 to obtain a saturated solution containing potassium and sodium;
s4, carrying out solid-liquid separation on the saturated solution containing potassium and sodium obtained in the step S3 to obtain potassium salt crystals and a saturated solution containing sodium respectively;
s5, carrying out the S3 on the saturated solution containing sodium in the S4 again to obtain sodium salt crystals.
Specifically, in S1, the main components of the aqueous solution are potassium hydroxide, sodium hydroxide, calcium hydroxide, and magnesium hydroxide.
Specifically, in the step S1, the main components of the biomass combustion ash include the following components in percentage by mass: 55% -60% of silicon dioxide, 4% -9% of calcium oxide, 15% -23% of potassium oxide, 1% -6% of ferric oxide, 3% -4% of magnesium oxide and 1% of sodium oxide.
Specifically, in the step S2, the main components of the potassium-sodium solution include sodium chloride and potassium chloride.
Specifically, in the step S3, the main components of the saturated solution containing potassium and sodium are 90% of potassium chloride and 4.5% of sodium chloride by mass percent.
Specifically, the main component of the saturated solution containing potassium and sodium is consistent with the main component of the potassium and sodium solution, and the concentration of the saturated solution containing potassium and sodium is higher than that of the potassium and sodium solution.
A biomass combustion fly ash-based resource utilization processing system for implementing the above-described resource utilization processing method, the resource utilization processing system comprising: a water washing tank, a reaction tank, a sedimentation tank, an evaporation crystallizer and a solid-liquid separator;
The washing tank is used for carrying out washing treatment on biomass combustion ash to enable partial components of the biomass combustion ash to generate chemical reaction with water, wherein a water solution is formed by a dissolved part of the biomass combustion ash, undissolved parts of the biomass combustion ash are discharged into the reaction tank to be subjected to iron removal treatment, the water solution is discharged into the sedimentation tank, the sedimentation tank is used for carrying out chemical sedimentation on the water solution to remove calcium oxide and magnesium oxide and obtain potassium sodium solution, the potassium sodium solution is discharged into the evaporation crystallizer, the evaporation crystallizer is used for carrying out evaporation concentration on the potassium sodium solution to obtain saturated solution containing potassium sodium, a liquid outlet of the evaporation crystallizer is communicated with the solid-liquid separator, the solid-liquid separator is used for carrying out solid-liquid separation on the saturated solution containing potassium sodium to obtain potassium salt crystals and saturated solution containing sodium after separation, and the saturated solution containing sodium is discharged into the evaporation crystallizer again to obtain sodium salt crystals after evaporation concentration.
Specifically, the outside of the washing tank is respectively provided with a first outlet and a second outlet, the first outlet is used for discharging the aqueous solution into the sedimentation tank, and the second outlet is used for discharging insoluble matters into the reaction tank.
Specifically, the evaporation crystallizer is respectively provided with a heater, a temperature detector and a temperature sensor, wherein the temperature detector is used for detecting the internal temperature of the evaporation crystallizer, the heater is used for heating the internal part of the evaporation crystallizer, the temperature sensor is used for sensing and controlling the heater to heat or stop heating, and the highest heating temperature of the heater is 100 ℃.
Specifically, the resource utilization treatment system further comprises a condensate water processor, wherein a water inlet of the condensate water processor is communicated with the evaporation crystallizer, and a water outlet of the condensate water processor is respectively communicated with the water washing tank and the sedimentation tank.
In order to extract high-purity potassium salt from biomass combustion ash, the first embodiment comprises the following steps:
S1, carrying out water washing treatment on biomass combustion ash, wherein part of components of the biomass combustion ash are dissolved into water in a water washing process, and a water solution is obtained after chemical reaction;
S2, removing impurities from the aqueous solution obtained in the step S1 by a chemical precipitation method, and removing calcium oxide and magnesium oxide in the aqueous solution to obtain a potassium-sodium solution;
s3, evaporating and concentrating the potassium-sodium solution obtained in the step S2 to obtain a saturated solution containing potassium and sodium;
S4, carrying out solid-liquid separation on the saturated solution containing potassium and sodium obtained in the step S3 to obtain potassium salt crystals, wherein the temperature is continuously increased to 100 ℃ in the evaporation concentration process, the solubility of potassium chloride is obviously increased along with the temperature in the temperature increasing process, the solubility of sodium chloride is not obviously increased along with the temperature, the potassium sodium solution is in a saturated state after the temperature is increased in the evaporation concentration process, the potassium sodium containing solution is cooled, the solubility of potassium chloride is reduced along with the temperature, so that potassium salt crystals are precipitated, and sodium salt crystals are not precipitated in the potassium salt crystals precipitation; therefore, a high-purity potassium salt crystal can be obtained in the solid-liquid separator.
Further illustratively according to the above embodiments, in S1, the main components of the aqueous solution include potassium hydroxide, sodium hydroxide, calcium hydroxide and magnesium hydroxide.
According to the above embodiments, for further detailed description, in S1, the main components of the biomass combustion ash include the following components in percentage by mass: 58% of silicon dioxide, 9% of calcium oxide, 23% of potassium oxide, 6% of ferric oxide, 3% of magnesium oxide and 1% of sodium oxide.
As described in the above examples, in S2, the main components of the potassium-sodium solution include sodium chloride and potassium chloride.
In order to extract high-purity sodium salt from biomass combustion ash, the technical scheme comprises the following steps:
S1, placing biomass combustion ash into a water washing tank for water washing treatment, so that part of components of the biomass combustion ash in the water washing process are dissolved into water and generate chemical reaction to obtain an aqueous solution;
S2, placing the aqueous solution obtained in the step S1 into a sedimentation tank, removing impurities by a chemical sedimentation method, and removing calcium oxide and magnesium oxide in the aqueous solution to obtain a potassium-sodium solution;
S3, putting the potassium-sodium solution obtained in the step S2 into an evaporation crystallizer for evaporation concentration to obtain a saturated solution containing potassium and sodium;
S4, discharging the saturated solution containing potassium and sodium obtained in the step S3 into a solid-liquid separator for solid-liquid separation to obtain a saturated solution containing sodium, wherein the solubility of potassium chloride is increased along with the temperature increase of evaporation concentration and is reduced along with the temperature decrease of the evaporation concentration, so that when the saturated solution containing potassium and sodium is obtained after the evaporation concentration, potassium salt crystal salt is separated out after the temperature reduction, the saturated solution containing potassium and sodium is subjected to solid-liquid separation to obtain potassium salt crystals and the saturated solution containing sodium, wherein the main component of the saturated solution containing sodium is sodium chloride, the concentration of potassium chloride and sodium chloride in the saturated solution containing potassium and sodium continuously changes due to the fact that the potassium salt crystals are continuously separated out in the solid-liquid separator, and the solubility of the potassium chloride crystals after the temperature reduction can be lower than the solubility of the sodium chloride, so that when the solution containing sodium in the evaporation crystallizer is saturated, the sodium salt crystals can be separated out through the solid-liquid separator, and high-purity sodium salt crystals are obtained;
s5, carrying out the S3 on the saturated solution containing sodium in the S4 again to obtain sodium salt crystals.
In S1, the main components of the aqueous solution include potassium hydroxide, sodium hydroxide, calcium hydroxide, and magnesium hydroxide.
In S1, the main components of the biomass combustion ash include the following components in percentage by mass: 59% of silicon dioxide, 9% of calcium oxide, 22% of potassium oxide, 5% of ferric oxide, 4% of magnesium oxide and 1% of sodium oxide
In S2, the main components of the potassium-sodium solution include sodium chloride and potassium chloride.
In order to realize simultaneous extraction of sodium salt and potassium salt in biomass combustion ash, the technical scheme comprises the following steps:
S1, placing biomass combustion ash into a water washing tank for water washing treatment, so that part of components of the biomass combustion ash in the water washing process are dissolved into water and generate chemical reaction to obtain an aqueous solution;
S2, placing the aqueous solution obtained in the step S1 into a sedimentation tank, removing impurities by a chemical sedimentation method, and removing calcium oxide and magnesium oxide in the aqueous solution to obtain a potassium-sodium solution;
S3, putting the potassium-sodium solution obtained in the step S2 into an evaporation crystallizer for evaporation concentration to obtain a saturated solution containing potassium and sodium;
s4, discharging the saturated solution containing potassium and sodium obtained in the step S3 into a solid-liquid separator for solid-liquid separation to obtain potassium salt crystals and the saturated solution containing sodium respectively;
s5, carrying out the S3 on the saturated solution containing sodium in the S4 again to obtain sodium salt crystals.
It should be noted that in the step S2, the main components of the potassium-sodium solution include sodium chloride and potassium chloride.
It should be noted that in the step S3, the main components of the saturated solution containing potassium and sodium are 90% of potassium chloride and 4.5% of sodium chloride by mass percent.
It should be noted that the main component of the saturated solution containing potassium and sodium is consistent with the main component of the potassium and sodium solution, and the concentration of the saturated solution containing potassium and sodium is higher than that of the potassium and sodium solution, and because the saturated solution containing potassium and sodium is concentrated by the evaporation crystallizer, the concentration of the saturated solution containing potassium and sodium is higher than that of the saturated solution containing potassium and sodium, so that the solid-liquid separation of the saturated solution containing potassium and sodium in the subsequent steps is realized to extract high-purity potassium salt crystals and sodium salt crystals.
The content of potassium chloride in the potassium-sodium solution is 20 times of the content of sodium chloride, so that in the evaporation concentration process, potassium chloride firstly reaches a saturated state and is separated out as crystals, at the moment, sodium chloride is not saturated, the solubility of the sodium chloride is not changed greatly at different temperatures, the solubility of the potassium chloride is greatly improved along with the rise of the temperature, and therefore, when the potassium salt solution is at high temperature and is close to saturation, the saturated containing solution containing potassium and sodium is cooled, and the solubility of the potassium chloride is reduced along with the fall of the temperature, so that potassium salt crystals can be separated out; the sodium chloride is not saturated, and the solubility of the sodium chloride is not greatly changed along with the decrease of the temperature, so that sodium salt crystals are not separated out in the evaporation concentration process; therefore, potassium salt crystals with higher purity can be obtained in the solid-liquid separator, the separated liquid flows back to the evaporation crystallizer to be continuously evaporated and concentrated, the concentration of potassium chloride and sodium chloride in saturated solution containing potassium and sodium can be continuously changed due to continuous precipitation of the potassium salt crystals in the solid-liquid separator, and the sodium salt crystals can be separated and precipitated through the solid-liquid separator when the sodium-containing liquid in the evaporation crystallizer is saturated due to lower-temperature potassium chloride solubility lower than sodium chloride solubility after precipitation, so that the potassium salt crystals and the sodium salt crystals are extracted from biomass combustion ash.
The evaporator comprises an evaporation crystallizer, a temperature detector and a temperature sensor, wherein the evaporation crystallizer is respectively provided with a heater, the temperature detector and the temperature sensor, the temperature detector is used for detecting the internal temperature of the evaporation crystallizer, the heater is used for heating the inside of the evaporation crystallizer, the temperature sensor is used for sensing and controlling the heater to heat or stop heating, and the highest heating temperature of the heater is 100 ℃; the inside of the evaporative crystallizer is heated by the heater, so that the temperature in the evaporative crystallizer is increased to 100 ℃, and the temperature data is transmitted by the temperature sensor after the temperature in the evaporative crystallizer is detected by the temperature detector, so that the heater is controlled, and the heater is heated or stopped.
In summary, the evaporation crystallizer and the solid-liquid separator separate potassium chloride from sodium chloride by different physical characteristics of potassium chloride and sodium chloride in the saturated solution containing potassium and sodium, so as to obtain potassium salt crystals and sodium salt crystals.
In order to extract silicon dioxide from biomass combustion ash, the method comprises the following steps: carrying out water washing treatment on biomass combustion ash, dissolving part of biomass combustion ash into water, and generating chemical reaction to obtain an aqueous solution; in the water washing treatment process of biomass combustion ash, the dissolved part is aqueous solution, the undissolved part is insoluble, the insoluble part comprises silicon dioxide and ferric oxide, the undissolved part of the biomass combustion ash is discharged into a reaction tank for iron removal treatment, the insoluble part is added with an acidic cleaning agent to remove the ferric oxide, high-purity silicon dioxide is obtained, and silicate and water are generated after alkaline elements are added into the high-purity silicon dioxide.
The technical scheme can realize that insoluble matters in the water washing method of biomass combustion ash are used for extracting silicon dioxide, and the effect of completely utilizing biomass combustion ash resources is achieved through the industrial application of the silicon dioxide as silicate.
Further limiting the above description, removing impurities from the obtained aqueous solution by chemical precipitation, and removing calcium oxide and magnesium oxide in the aqueous solution to obtain potassium-sodium solution.
Further limiting the above description, evaporating and concentrating the potassium-sodium solution to obtain saturated solution containing potassium and sodium.
According to the above, it is limited that, the potassium salt crystal and the saturated solution containing sodium are obtained by solid-liquid separation of the saturated solution containing potassium and sodium respectively; concentrating the saturated solution containing sodium again by an evaporation crystallizer, and separating out sodium salt crystals by a solid-liquid separator.
In summary, the main components of the biomass ash are 55-60% of silicon dioxide SiO 2, 4-9% of calcium oxide, 15-23% of potassium oxide, 1-6% of ferric oxide, 3-4% of magnesium oxide and 1% of sodium oxide; the insoluble substances after water washing are mainly silicon dioxide, and can be used as dehumidifying drying agent, dehydrating agent, dampproof agent, air humidity regulator and the like after purification.
Extracting silicon dioxide from insoluble matters generated in the process of washing biomass combustion ash, wherein the extracted silicon dioxide is subjected to pickling agent de-ironing treatment, and the silicon dioxide is not reacted with water and is insoluble in water; the water can be reacted with hot strong alkali solution or melted alkali to generate silicate and water, wherein the obtained water can be discharged into a water washing tank again to carry out water washing treatment on biomass combustion ash.
In order to realize that the vapor generated by evaporating and concentrating the biomass combustion ash in the evaporating crystallizer is recycled, the fifth embodiment effectively saves the cost and improves the circularity, and the technical scheme comprises the following steps: a biomass combustion fly ash-based resource utilization processing system for implementing the above-described resource utilization processing method, the resource utilization processing system comprising: a water washing tank, a reaction tank, a sedimentation tank, an evaporation crystallizer and a solid-liquid separator;
The washing tank is used for carrying out washing treatment on biomass combustion ash to enable partial components of the biomass combustion ash to generate chemical reaction with water, wherein a water solution is formed by a dissolved part of the biomass combustion ash, undissolved parts of the biomass combustion ash are discharged into the reaction tank to be subjected to iron removal treatment, the water solution is discharged into the sedimentation tank, the sedimentation tank is used for carrying out chemical sedimentation on the water solution to remove calcium oxide and magnesium oxide and obtain potassium sodium solution, the potassium sodium solution is discharged into the evaporation crystallizer, the evaporation crystallizer is used for carrying out evaporation concentration on the potassium sodium solution to obtain saturated solution containing potassium sodium, a liquid outlet of the evaporation crystallizer is communicated with the solid-liquid separator, the solid-liquid separator is used for carrying out solid-liquid separation on the saturated solution containing potassium sodium to obtain potassium salt crystals and saturated solution containing sodium after separation, and the saturated solution containing sodium is discharged into the evaporation crystallizer again to obtain sodium salt crystals after evaporation concentration.
According to the above, the resource utilization treatment system further comprises a condensate water processor, the water inlet of the condensate water processor is communicated with the evaporation crystallizer, the water outlet of the condensate water processor is respectively communicated with the water washing tank and the sedimentation tank, the water vapor generated in the evaporation crystallization process of the evaporation crystallizer is recovered through the condensate water processor, and the water vapor is cooled and then is discharged into the water washing tank and the sedimentation tank, so that the effect of saving water sources is achieved, and the cost is reduced.
The aspects of the present application have been described in detail hereinabove with reference to the accompanying drawings. In the foregoing embodiments, the descriptions of the embodiments are focused on, and for those portions of one embodiment that are not described in detail, reference may be made to the related descriptions of other embodiments. Those skilled in the art will also appreciate that the acts and modules referred to in the specification are not necessarily required for the present application. In addition, it can be understood that the steps in the method of the embodiment of the present application may be sequentially adjusted, combined and pruned according to actual needs, and the modules in the device of the embodiment of the present application may be combined, divided and pruned according to actual needs.
The foregoing description of embodiments of the application has been presented for purposes of illustration and description, and is not intended to be exhaustive or limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the various embodiments described. The terminology used herein was chosen in order to best explain the principles of the embodiments, the practical application, or the improvement of technology in the marketplace, or to enable others of ordinary skill in the art to understand the embodiments disclosed herein.
Claims (10)
1. The resource utilization treatment method based on the biomass combustion fly ash is characterized by comprising the following steps of:
S1, carrying out water washing treatment on biomass combustion ash, dissolving part of the biomass combustion ash into water, and carrying out chemical reaction to obtain a dissolved part which is an aqueous solution; the undissolved part is an insoluble substance, the insoluble substance comprises silicon dioxide and ferric oxide, the insoluble substance is added with an acidic cleaning agent to remove the ferric oxide to obtain high-purity silicon dioxide, and the high-purity silicon dioxide is added with an alkaline element to generate silicate and water;
S2, removing impurities from the aqueous solution obtained in the step S1 by a chemical precipitation method, and removing calcium oxide and magnesium oxide in the aqueous solution to obtain a potassium-sodium solution;
s3, evaporating and concentrating the potassium-sodium solution obtained in the step S2 to obtain a saturated solution containing potassium and sodium;
s4, carrying out solid-liquid separation on the saturated solution containing potassium and sodium obtained in the step S3 to obtain potassium salt crystals and a saturated solution containing sodium respectively;
s5, carrying out the S3 on the saturated solution containing sodium in the S4 again to obtain sodium salt crystals.
2. The method for resource utilization treatment based on biomass combustion fly ash according to claim 1, wherein in S1, the main components of the aqueous solution include potassium hydroxide, sodium hydroxide, calcium hydroxide and magnesium hydroxide.
3. The resource utilization treatment method based on biomass combustion fly ash according to claim 1, wherein in the step S1, the main components of the biomass combustion fly ash comprise the following components in percentage by mass: 55% -60% of silicon dioxide, 4% -9% of calcium oxide, 15% -23% of potassium oxide, 1% -6% of ferric oxide, 3% -4% of magnesium oxide and 1% of sodium oxide.
4. The method for resource utilization treatment based on biomass combustion fly ash according to claim 1, wherein in S2, the main components of the potassium-sodium solution include sodium chloride and potassium chloride.
5. The resource utilization treatment method based on biomass combustion fly ash according to claim 1, wherein in the step S3, the main components of the saturated solution containing potassium and sodium are 90% of potassium chloride and 4.5% of sodium chloride by mass percent.
6. The resource utilization treatment method based on biomass combustion fly ash according to claim 1, wherein the main component of the saturated solution containing potassium and sodium is consistent with the main component of the potassium and sodium solution, and the concentration of the saturated solution containing potassium and sodium is higher than the concentration of the potassium and sodium solution.
7. A biomass combustion fly ash based resource utilization processing system for performing the resource utilization processing method according to any one of claims 1 to 6, characterized in that the resource utilization processing system comprises:
a water washing tank, a reaction tank, a sedimentation tank, an evaporation crystallizer and a solid-liquid separator;
The washing tank is used for carrying out washing treatment on biomass combustion ash to enable partial components of the biomass combustion ash to generate chemical reaction with water, wherein a water solution is formed by a dissolved part of the biomass combustion ash, undissolved parts of the biomass combustion ash are discharged into the reaction tank to be subjected to iron removal treatment, the water solution is discharged into the sedimentation tank, the sedimentation tank is used for carrying out chemical sedimentation on the water solution to remove calcium oxide and magnesium oxide and obtain potassium sodium solution, the potassium sodium solution is discharged into the evaporation crystallizer, the evaporation crystallizer is used for carrying out evaporation concentration on the potassium sodium solution to obtain saturated solution containing potassium sodium, a liquid outlet of the evaporation crystallizer is communicated with the solid-liquid separator, the solid-liquid separator is used for carrying out solid-liquid separation on the saturated solution containing potassium sodium to obtain potassium salt crystals and saturated solution containing sodium after separation, and the saturated solution containing sodium is discharged into the evaporation crystallizer again to obtain sodium salt crystals after evaporation concentration.
8. The biomass combustion fly ash-based resource utilization treatment system according to claim 7, wherein a first outlet and a second outlet are respectively arranged outside the water washing tank, the first outlet is used for discharging the aqueous solution into the sedimentation tank, and the second outlet is used for discharging insoluble matters into the reaction tank.
9. The resource utilization treatment system based on biomass combustion fly ash according to claim 7, wherein a heater, a temperature detector and a temperature sensor are respectively arranged in the evaporation crystallizer, the temperature detector is used for detecting the internal temperature of the evaporation crystallizer, the heater is used for heating the inside of the evaporation crystallizer, the temperature sensor is used for sensing and controlling the heater to heat or stop heating, and the highest heating temperature of the heater is 100 ℃.
10. The resource utilization treatment system based on biomass combustion fly ash of claim 7, further comprising a condensate water processor, wherein a water inlet of the condensate water processor is communicated with the evaporation crystallizer, and a water outlet of the condensate water processor is respectively communicated with the water washing tank and the sedimentation tank.
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