CN216837159U - System for utilize desulfurization ash to make baking soda - Google Patents
System for utilize desulfurization ash to make baking soda Download PDFInfo
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- CN216837159U CN216837159U CN202220743391.6U CN202220743391U CN216837159U CN 216837159 U CN216837159 U CN 216837159U CN 202220743391 U CN202220743391 U CN 202220743391U CN 216837159 U CN216837159 U CN 216837159U
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Abstract
A system for preparing baking soda by utilizing desulfurized ash belongs to the technical field of baking soda preparation and waste comprehensive utilization. One technical scheme comprises a preheater, a dissolving unit, a multi-media filter, a three-platen frame filter press, an organic matter removing unit, an aeration impurity removing unit, a fluorine removing unit, a salt separating unit, an evaporator, two centrifuges, three spray drying towers and a conversion unit; the other technical scheme is added with a leaching unit compared with the technical scheme. The utility model transfers a large amount of sodium bicarbonate out of the system, and then converts the sodium sulfate in the system into the baking soda, thereby reducing the usage amount of the conversion agent for converting the sodium sulfate into the baking soda; and a salt separating device is added to separate the sodium sulfate from other miscellaneous salts in the system, so that the purity of the final sodium bicarbonate product is ensured, and the desulfurized fly ash is fully recycled.
Description
Technical Field
The utility model belongs to the technical field of baking soda preparation and waste comprehensive utilization, a system for utilize desulfurization ash system baking soda is related to.
Background
The flue gas desulfurization ash is a first-level dangerous solid waste generated in the coke oven flue gas desulfurization process by taking sodium carbonate and sodium bicarbonate as desulfurizing agents, wherein the main components are sodium carbonate, sodium bicarbonate, sodium sulfate and the like, and the flue gas desulfurization ash contains impurity ions in a certain proportion. The desulfurized fly ash is easy to dissolve in water, and can infiltrate into soil through dripping of rainwater during stacking or landfill treatment, thereby causing serious pollution to the soil and underground water.
CN209940485U provides a baking soda desulfurization ash resource utilization device, and the device includes dissolving unit, filter unit, aeration reaction unit, whirl unit, crystallization unit and drying unit, and the solution that baking soda desulfurization ash dissolved and filtered gets enters aeration reaction unit, and the middle reaction gets the thick liquid, and the thick liquid gets baking soda crystal through whirl unit separation, gets the baking soda product through drying unit drying, but the device does not include the salt separation unit, and miscellaneous salt such as sodium chloride, sodium fluoride, sodium nitrate all exist in final product, and the baking soda product purity that obtains can not guarantee.
CN211871388U proposes a device for recycling desulfurized ash from coking flue gas by dry method, which, on the basis of the dissolution and filtration of desulfurized ash, proposes to add sulfuric acid into the dissolved solution in a sodium sulfate reaction kettle to react with sodium carbonate to generate sodium sulfate, but the desulfurized ash usually contains 5% to 10% of sodium carbonate, and the reaction consumes a large amount of sulfuric acid, which is a high treatment cost in view of economic efficiency.
A system for preparing baking soda by utilizing desulfurized ash is urgently needed, the product purity of the baking soda can be ensured, and the treatment cost is lower.
Disclosure of Invention
The utility model aims at providing a system for preparing baking soda by utilizing desulfurized ash, aiming at the defects of the prior art, the impurity removal device in the process of recovering baking soda by desulfurized ash is optimized and perfected, firstly, a large amount of sodium bicarbonate in the system is transferred out, then, sodium sulfate in the system is converted into baking soda, and the use amount of a conversion reagent for converting sodium sulfate into baking soda is reduced; and a salt separating device is added to separate the sodium sulfate from other miscellaneous salts in the system, so that the purity of the final sodium bicarbonate product is ensured, and the desulfurized fly ash is fully recycled. The purpose of the utility model is realized through the following technical scheme.
A system for preparing baking soda by utilizing desulfurized ash, wherein one technical scheme comprises a preheater, a dissolving unit, a multi-media filter, a three-platen frame filter press, an organic matter removing unit, an aeration impurity removing unit, a fluorine removing unit, a salt separating unit, an evaporator, two centrifuges, three spray drying towers and a conversion unit;
the cold fluid inlet of the preheater is an inlet of water used by the dissolving unit, the cold fluid outlet of the preheater is connected with a liquid inlet of the dissolving unit, the hot fluid inlet of the preheater is connected with the steam outlet of the evaporator, and the hot fluid outlet of the preheater is a condensed water outlet;
the dissolving unit is provided with a desulfurized ash inlet, a discharge hole of the dissolving unit is connected with a feed hole of the multi-medium filter, a discharge hole of the multi-medium filter is connected with a feed hole of the organic matter removing unit, and a discharge hole of the organic matter removing unit is connected with a feed hole of the aeration impurity removing unit;
the bottom of each of the aeration impurity removal unit and the spray drying tower is provided with an air inlet and is connected with an air source;
the slurry outlet at the top of the aeration impurity removal unit is connected with the feed inlet of a first plate-and-frame filter press, the liquid outlet of the first plate-and-frame filter press is connected with the inlet of a fluorine removal unit, and the discharge outlet of the first plate-and-frame filter press is connected with the feed inlet of a first spray drying tower;
the defluorination unit is provided with a defluorination agent inlet, a discharge hole of the defluorination unit is connected with a feed hole of the second plate-and-frame filter press, and a liquid outlet of the second plate-and-frame filter press is connected with a feed hole of the salt separation unit;
the salt separation unit is characterized in that a liquid discharge port of the salt separation unit is connected with a feed port of the evaporator, a crystal discharge port of the salt separation unit is connected with a feed port of a first centrifugal machine, a discharge port of the first centrifugal machine is connected with a feed port of a first spray drying tower, and a discharge port of the first spray drying tower is connected with a feed port of the conversion unit;
the solid discharge port of the evaporator is connected with the feed port of a second centrifuge, the discharge port of the second centrifuge is connected with the feed port of a second spray drying tower, and the discharge port of the second spray drying tower is a mixed salt outlet;
the conversion unit is provided with an ammonium bicarbonate inlet, a discharge hole of the conversion unit is connected with a feed inlet of a third plate-and-frame filter press, and a discharge hole of the third plate-and-frame filter press is connected with a feed inlet of a third spray drying tower; the liquid outlet of the third plate frame filter press is an ammonium sulfate outlet, and the discharge port of the third spray drying tower is a sodium bicarbonate product outlet.
The working process of the system is as follows: the water for dissolving the desulfurization ash is preheated by the preheater and enters the dissolving unit, and the water and the desulfurization ash are mixed and dissolved in a certain proportion in the dissolving unit and then enter the multi-media filter. After being filtered by the multi-medium filter, the filtrate enters an organic matter removing unit. And after passing through the organic matter removing unit, the wastewater enters an aeration impurity removing unit, and air or oxygen and carbon dioxide are introduced into the aeration impurity removing unit. After the reaction is completed, the slurry enters a first plate-and-frame filter press, and a filter cake obtained after filter pressing enters a first spray drying tower to be dried to obtain crude baking soda (a mixture of sodium sulfate and sodium bicarbonate); and (4) feeding the filter liquor after filter pressing into a fluorine removal unit. And adding a fluorine removal agent in proportion into the fluorine removal unit, fully reacting, then discharging water to enter a second plate-and-frame filter press, and feeding filter liquor obtained after filter pressing to a salt separation unit. The crystals of the salt separation unit enter a first centrifuge for spin-drying, and then enter a first spray drying tower for drying after spin-drying, so as to obtain a mixture of sodium sulfate and sodium bicarbonate; and the liquid of the salt separating unit enters a second evaporator for continuous evaporation and crystallization, and a small amount of mixed salt is obtained after centrifugal dehydration by a second centrifugal machine and drying by a second spray drying tower. And the mixture of sodium sulfate and sodium bicarbonate obtained by the first spray drying tower enters a conversion unit, the sodium sulfate and ammonium bicarbonate are mixed in the conversion unit to generate double decomposition reaction, the concentration of the sodium bicarbonate is supersaturated to separate out a large amount of crystals, the crystals enter a third plate-and-frame filter press, the filtrate is an ammonium sulfate solution, and the filter cake enters a third spray drying tower to be dried to obtain the product baking soda.
Further, the organic matter removing unit is an adsorption unit or an oxidation unit, wherein the adsorption material in the adsorption unit is selected from one of carbon-based adsorption materials (such as walnut shells, fruit shells, sawdust, anthracite, fly ash and activated carbon) or inorganic adsorption materials (such as diatomite, kaolin, bentonite, expanded shale, alumina and natural zeolite) or fiber adsorption materials (such as fiber balls and sponges) or adsorption resins; the oxidation unit is selected from one or more of a medicament oxidation device, a wet oxidation device, a Fenton oxidation device, an ozone catalytic oxidation device, a photocatalytic oxidation device and an electrochemical oxidation device.
Further, the fluorine removal unit is selected from one or a combination of a plurality of calcium method fluorine removal devices, aluminum salt fluorine removal devices and resin adsorption fluorine removal devices.
Further, the salt separation unit is selected from one or a combination of several of an evaporative crystallization device, a freezing crystallization device and a nanofiltration device.
The system has the following beneficial technical effects: (1) the heat source of the preheater comes from the steam waste heat in the evaporator, the heat is fully utilized, and the condensed water can be used as the water supplement of the desulfurized fly ash dissolved water. (2) The system is provided with an organic matter removing unit, an aeration impurity removing unit and a fluorine removing unit, F-Too high a concentration would lead to a considerable increase in the material costs of the evaporative crystallizer, and the removal and conversion of impurities would be beneficial for the purity increase of the baking soda. (3) The multi-stage spray drying tower can realize the separation of the sodium bicarbonate and the miscellaneous salts, and ensures the purity of the sodium bicarbonate product.
The utility model provides another technical proposal, which comprises a preheater, a dissolving unit, a leaching unit, a multi-medium filter, a three-platen frame filter press, an organic matter removing unit, an aeration impurity removing unit, a fluorine removing unit, a salt separating unit, an evaporator, two centrifuges, three spray drying towers and a conversion unit;
the cold fluid inlet of the preheater is an inlet of water used by the dissolving unit, the cold fluid outlet of the preheater is connected with a liquid inlet of the dissolving unit, the hot fluid inlet of the preheater is connected with the steam outlet of the evaporator, and the hot fluid outlet of the preheater is a condensed water outlet;
the dissolving unit is provided with a sodium sulfate inlet, and a discharge hole of the dissolving unit is connected with a feed inlet at the top of the leaching unit;
the top of the leaching unit is provided with a desulfurized fly ash inlet, a liquid discharge port of the leaching unit is connected with a feed inlet of the multi-media filter, and a solid discharge port of the leaching unit is connected with a feed inlet of the conversion unit; the discharge hole of the multi-medium filter is connected with the feed inlet of the organic matter removing unit, and the discharge hole of the organic matter removing unit is connected with the feed inlet of the aeration impurity removing unit;
the bottom of each of the aeration impurity removal unit and the spray drying tower is provided with an air inlet and is connected with an air source;
the slurry outlet at the top of the aeration and impurity removal unit is connected with the feed inlet of a first plate-and-frame filter press, the liquid outlet of the first plate-and-frame filter press is connected with the inlet of a fluorine removal unit, and the discharge outlet of the first plate-and-frame filter press is connected with the feed inlet of a first spray drying tower;
the defluorination unit is provided with a defluorination agent inlet, a discharge hole of the defluorination unit is connected with a feed hole of the second plate-and-frame filter press, and a liquid outlet of the second plate-and-frame filter press is connected with a feed hole of the salt separation unit;
the liquid discharge port of the salt separation unit is connected with the feed port of the evaporator, the crystal discharge port of the salt separation unit is connected with the feed port of a first centrifuge, the discharge port of the first centrifuge is connected with the feed port of a first spray drying tower, and the discharge port of the first spray drying tower is connected with the feed port of the conversion unit;
the solid discharge hole of the evaporator is connected with the feed inlet of a second centrifugal machine, the discharge hole of the second centrifugal machine is connected with the feed inlet of a second spray drying tower, and the discharge hole of the second spray drying tower is a mixed salt outlet;
the conversion unit is provided with an ammonium bicarbonate inlet, a discharge hole of the conversion unit is connected with a feed inlet of a third plate-and-frame filter press, and a discharge hole of the third plate-and-frame filter press is connected with a feed inlet of a third spray drying tower; the liquid outlet of the third plate frame filter press is an ammonium sulfate outlet, and the discharge port of the third spray drying tower is a sodium bicarbonate product outlet.
The working process of the system is as follows: the water for preparing the saturated sodium sulfate solution is preheated by the preheater and enters the dissolving unit, the water and the anhydrous sodium sulfate are mixed according to a certain proportion in the dissolving unit to prepare the saturated sodium sulfate solution, the saturated sodium sulfate solution enters the top of the leaching unit to leach the desulfurized fly ash, sodium sulfate solids generated after leaching enter the converting unit, and the leached liquid enters the multi-media filter. Filtering by a multi-medium filter, feeding the filtrate into an organic matter removing unit, feeding the filtrate into an aeration impurity removing unit after passing through the organic matter removing unit, introducing air or oxygen and carbon dioxide into the aeration impurity removing unit, feeding the slurry into a first plate-and-frame filter press after complete reaction, and feeding the filter cake obtained by filter pressing into a first spray drying tower for drying to obtain crude baking soda (a mixture of sodium sulfate and sodium bicarbonate); and (4) feeding the filter liquor after filter pressing into a fluorine removal unit. And adding a fluorine removal agent in proportion into the fluorine removal unit, fully reacting, then discharging water to enter a second plate-and-frame filter press, and feeding filter liquor obtained after filter pressing to a salt separation unit. The crystals of the salt separation unit enter a first centrifuge for spin-drying, and then enter a first spray drying tower for drying after spin-drying, so as to obtain a mixture of sodium sulfate and sodium bicarbonate; and the liquid of the salt separating unit enters a second evaporator for continuous evaporation and crystallization, and a small amount of mixed salt is obtained after centrifugal dehydration by a second centrifugal machine and drying by a second spray drying tower. And (3) enabling the sodium sulfate solid in the leaching unit, the mixture of sodium sulfate and sodium bicarbonate obtained by the first spray drying tower to enter a conversion unit, mixing the sodium sulfate and ammonium bicarbonate in the conversion unit to perform double decomposition reaction, separating out a large amount of crystals due to supersaturation of the sodium bicarbonate concentration, enabling the crystals to enter a third plate-and-frame filter press, enabling the filtrate to be an ammonium sulfate solution, and enabling the filter cake to enter a third spray drying tower to be dried to obtain the product sodium bicarbonate.
Further, the organic matter removing unit is an adsorption unit or an oxidation unit, wherein the adsorption material in the adsorption unit is selected from one of carbon-based adsorption materials (such as walnut shells, fruit shells, sawdust, anthracite, fly ash and activated carbon) or inorganic adsorption materials (such as diatomite, kaolin, bentonite, expanded shale, alumina and natural zeolite) or fiber adsorption materials (such as fiber balls and sponges) or adsorption resins; the oxidation unit is selected from one or more of a medicament oxidation device, a wet oxidation device, a Fenton oxidation device, an ozone catalytic oxidation device, a photocatalytic oxidation device and an electrochemical oxidation device.
Further, the fluorine removal unit is selected from one or a combination of a plurality of calcium method fluorine removal devices, aluminum salt fluorine removal devices and resin adsorption fluorine removal devices.
Further, the salt separation unit is selected from one or a combination of several of an evaporative crystallization device, a freezing crystallization device and a nanofiltration device.
The system has the following beneficial technical effects: (1) the heat source of the preheater is from the steam waste heat in the evaporator, the heat is fully utilized, and the condensed water can be used as the water supplement of the sodium sulfate dissolved water. (2) The system is provided with an organic matter removing unit, an aeration impurity removing unit and a fluorine removing unit, F-Too high a concentration would lead to a considerable increase in the material costs of the evaporative crystallizer, and the removal and conversion of impurities would be beneficial for the purity increase of the baking soda. (3) The multi-stage spray drying tower can realize the separation of the sodium bicarbonate and the miscellaneous salts, and ensures the purity of the sodium bicarbonate product. (4) The solid sodium sulfate obtained after the saturated sodium sulfate solution is leached by the leaching unit has high purity, and can be directly used for preparing baking soda after being dried.
Drawings
FIG. 1 is a schematic structural view of example 1.
FIG. 2 is a schematic structural view of example 2.
In the figure: 1-preheater, 2-dissolving unit, 3-multi-media filter, 4-organic matter removing unit, 5-aeration impurity removing unit, 6-first plate-and-frame filter press, 7-fluorine removing unit, 8-second plate-and-frame filter press, 9-salt separating unit, 10-evaporator, 11-first centrifuge, 12-second centrifuge, 13-first spray drying tower, 14-second spray drying tower, 15-converting unit, 16-third plate-and-frame filter press, 17-third spray drying tower and 18-leaching unit.
Detailed Description
The technical solution of the present invention is clearly and completely described below with reference to the drawings. It is to be understood that the described embodiments are merely exemplary of some, and not necessarily all, embodiments of the invention. Based on the embodiments of the present invention, all other embodiments obtained by a person of ordinary skill in the art without creative work belong to the protection scope of the present invention.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are used merely for convenience of description and for simplicity of description, and do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore, should not be construed as limiting the present invention. 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 quantity or location.
In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood according to specific situations by those skilled in the art.
Example 1
As shown in fig. 1, the desulfurization ash baking soda treatment plant system comprises: the device comprises a preheater 1, a dissolving unit 2, a multi-media filter 3, an organic matter removing unit 4, an aeration impurity removing unit 5, a first plate-and-frame filter press 6, a fluorine removing unit 7, a second plate-and-frame filter press 8, a salt separating unit 9, an evaporator 10, a first centrifuge 11, a second centrifuge 12, a first spray drying tower 13, a second spray drying tower 14, a conversion unit 15, a third plate-and-frame filter press 16 and a third spray drying tower 17.
Dissolve the water that the desulfurization ash was used and get into through 1 cold fluid inlet of preheater, 1 cold fluid outlet of preheater links to each other with the inlet of dissolving unit 2, and 1 hot-fluid inlet of preheater links to each other with 10 steam outlet of evaporimeter, and 1 hot-fluid outlet of preheater is the comdenstion water export.
The dissolving unit 2 is provided with a desulfurized fly ash inlet, the discharge hole of the dissolving unit 2 is connected with the feed inlet of the multi-media filter 3, the discharge hole of the multi-media filter 3 is connected with the feed inlet of the organic matter removing unit 4, and the discharge hole of the organic matter removing unit 4 is connected with the feed inlet of the aeration impurity removing unit 5.
The bottoms of the aeration impurity removal unit 5 and the spray drying towers 13, 14 and 17 are provided with air inlets and are connected with an air source.
The outlet of the slurry at the top of the aeration impurity removal unit 5 is connected with the feed inlet of a first plate and frame filter press 6, the liquid outlet of the first plate and frame filter press 6 is connected with the inlet of a fluorine removal unit 7, and the discharge port of the first plate and frame filter press 6 is connected with the feed inlet of a first spray drying tower 13.
The defluorination unit 7 is provided with a defluorination agent inlet, a discharge hole of the defluorination unit 7 is connected with a feed inlet of the second plate and frame filter press 8, and a liquid outlet of the second plate and frame filter press 8 is connected with a feed inlet of the salt separation unit 9.
The liquid discharge port of the salt separation unit 9 is connected with the feed port of the evaporator 10, the crystal discharge port of the salt separation unit 9 is connected with the feed port of the first centrifuge 11, the discharge port of the first centrifuge 11 is connected with the feed port of the first spray drying tower 13, and the discharge port of the first spray drying tower 13 is connected with the feed port of the conversion unit 15.
The solid discharge hole of the evaporator 10 is connected with the feed hole of a second centrifuge 12, the discharge hole of the second centrifuge 12 is connected with the feed hole of a second spray drying tower 14, and the discharge hole of the second spray drying tower 14 is a miscellaneous salt outlet.
The conversion unit 15 is provided with an ammonium bicarbonate inlet, a discharge hole of the conversion unit 15 is connected with a feed inlet of a third plate-and-frame filter press 16, and a discharge hole of the third plate-and-frame filter press 16 is connected with a feed inlet of a third spray drying tower 17; the liquid outlet of the third plate frame filter press 16 is an ammonium sulfate outlet, and the discharge port of the third spray drying tower 17 is a baking soda product outlet.
The working process of the system is as follows: the water for dissolving the desulfurization ash is preheated by the preheater 1 and enters the dissolving unit 2, the water and the desulfurization ash are mixed according to a certain proportion in the dissolving unit 2 and then enter the multi-media filter 3, the water and the desulfurization ash are filtered by the multi-media filter 3, the filtrate enters the organic matter removing unit 4, and the filtrate enters the aeration impurity removing unit 5 after passing through the organic matter removing unit 4. Introducing oxygen and carbon dioxide into the aeration impurity removal unit 5, feeding the slurry into a first plate-and-frame filter press 6 after the reaction is completed, and feeding the filter cake obtained by filter pressing into a first spray drying tower 13 for drying to obtain crude baking soda; the filtrate after filter pressing enters a defluorination unit 7. Adding a fluorine removal agent in proportion, fully reacting, then leading the effluent to enter a second plate-and-frame filter press 8, leading the filter-pressed filtrate to enter a salt separation unit 9, concentrating the filtrate to a certain degree, then leading the precipitated crystals to enter a first centrifuge 11 for spin-drying, and then leading the crystals to enter a first spray drying tower 13 for drying to obtain a mixture of sodium sulfate and sodium bicarbonate; the mother liquor of the salt separating unit 9 enters an evaporator 10 to continue evaporation and crystallization, and is centrifugally dewatered by a second centrifuge 12 and dried by a second spray drying tower 14 to obtain a small amount of miscellaneous salt. The mixture of sodium sulfate and sodium bicarbonate obtained from the first spray drying tower 13 enters the conversion unit 15, the sodium sulfate and ammonium bicarbonate are mixed in the conversion unit 15, the sodium bicarbonate is supersaturated, so that a large amount of crystals are separated out, and the sodium bicarbonate is subjected to pressure filtration by a third plate-and-frame filter press 16 and is dried by a third spray drying tower 17 to obtain the product sodium bicarbonate.
Example 2
As shown in fig. 2, the desulfurization ash baking soda plant system comprises: the device comprises a preheater 1, a dissolving unit 2, a leaching unit 18, a multi-media filter 3, an organic matter removing unit 4, an aeration impurity removing unit 5, a first plate-and-frame filter press 6, a fluorine removing unit 7, a second plate-and-frame filter press 8, a salt separating unit 9, an evaporator 10, a first centrifuge 11, a second centrifuge 12, a first spray drying tower 13, a second spray drying tower 14, a converting unit 15, a third plate-and-frame filter press 16 and a third spray drying tower 17.
Water for preparing a saturated sodium sulfate solution enters through a cold fluid inlet of the preheater 1, a cold fluid outlet of the preheater 1 is connected with a liquid inlet of the dissolving unit, a hot fluid inlet of the preheater 1 is connected with a steam outlet of the evaporator 10, and a hot fluid outlet of the preheater 1 is a condensed water outlet.
The dissolving unit 2 is provided with a sodium sulfate inlet, and a discharge hole of the dissolving unit 2 is connected with a feed inlet at the top of the leaching unit 18.
The top of the leaching unit 18 is provided with a desulfurized fly ash inlet, a liquid discharge port of the leaching unit 18 is connected with a feed port of the multi-media filter 3, and a solid discharge port of the leaching unit 18 is connected with a feed port of the conversion unit 15; the discharge hole of the multi-medium filter 3 is connected with the feed inlet of the organic matter removing unit 4, and the discharge hole of the organic matter removing unit 4 is connected with the feed inlet of the aeration impurity removing unit 5.
The bottoms of the aeration impurity removal unit 5 and the spray drying towers 13, 14 and 17 are provided with air inlets and are connected with an air source.
The outlet of the slurry at the top of the aeration impurity removal unit 5 is connected with the feed inlet of a first plate and frame filter press 6, the liquid outlet of the first plate and frame filter press 6 is connected with the inlet of a fluorine removal unit 7, and the discharge port of the first plate and frame filter press 6 is connected with the feed inlet of a first spray drying tower 13.
The defluorination unit 7 is provided with a defluorination agent inlet, a discharge hole of the defluorination unit 7 is connected with a feed inlet of the second plate and frame filter press 8, and a liquid outlet of the second plate and frame filter press 8 is connected with a feed inlet of the salt separation unit 9.
The liquid discharge port of the salt separation unit 9 is connected with the feed port of the evaporator 10, the crystal discharge port of the salt separation unit 9 is connected with the feed port of the first centrifuge 11, the discharge port of the first centrifuge 11 is connected with the feed port of the first spray drying tower 13, and the discharge port of the first spray drying tower 13 is connected with the feed port of the conversion unit 15.
The solid discharge hole of the evaporator 10 is connected with the feed hole of a second centrifuge 12, the discharge hole of the second centrifuge 12 is connected with the feed hole of a second spray drying tower 14, and the discharge hole of the second spray drying tower 14 is a miscellaneous salt outlet.
The conversion unit 15 is provided with an ammonium bicarbonate inlet, a discharge hole of the conversion unit 15 is connected with a feed inlet of a third plate-and-frame filter press 16, and a discharge hole of the third plate-and-frame filter press 16 is connected with a feed inlet of a third spray drying tower 17; the liquid outlet of the third plate frame filter press 16 is an ammonium sulfate outlet, and the discharge port of the third spray drying tower 17 is a baking soda product outlet.
The working process of the system is as follows: the water for preparing the saturated sodium sulfate solution is preheated by the preheater 1 and enters the dissolving unit 2, the water and the anhydrous sodium sulfate in the dissolving unit 2 are mixed according to a certain proportion to prepare the saturated sodium sulfate solution, and the saturated sodium sulfate solution enters the top of the leaching unit 18 to leach the desulfurized fly ash. And the sodium sulfate solid obtained after leaching enters a conversion unit 15, the leached liquid enters a multi-media filter 3, the liquid is filtered by the multi-media filter 3, the filtrate enters an organic matter removing unit 4, and the filtrate enters an aeration impurity removing unit 5 after being adsorbed by activated carbon. Introducing oxygen and carbon dioxide into the aeration impurity removal unit 5, feeding the slurry into a first plate-and-frame filter press 6 after the reaction is completed, and feeding the filter cake obtained by filter pressing into a first spray drying tower 13 for drying to obtain crude baking soda; and (3) feeding the filter-pressed filtrate into a fluorine removal unit 7, adding a fluorine removal agent in proportion, fully reacting, and feeding the effluent into a second plate-and-frame filter press 8. The filter-pressed filtrate enters a salt separating unit 9, crystals precipitated after the filtrate is concentrated to a certain degree enter a first centrifuge 11 for spin-drying, and the crystals enter a first spray drying tower 13 for drying after spin-drying, so that a mixture of sodium sulfate and sodium bicarbonate is obtained; the mother liquor of the salt separating unit 9 enters an evaporator 10 to continue evaporation and crystallization, and a small amount of miscellaneous salt is obtained through centrifugal dehydration by a second centrifuge 12 and a second spray drying tower 14. The mixture of sodium sulfate and sodium bicarbonate obtained from the first spray drying tower 13 enters the conversion unit 15, the sodium sulfate and ammonium bicarbonate are mixed in the conversion unit 15, the sodium bicarbonate is supersaturated, so that a large amount of crystals are separated out, and the sodium bicarbonate is subjected to pressure filtration by a third plate-and-frame filter press 16 and is dried by a third spray drying tower 17 to obtain the product sodium bicarbonate.
Although embodiments of the present invention have been shown and described, it is to be understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that changes, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art without departing from the principles and spirit of the present invention. The protection scope of the present invention is defined by the claims and their equivalents.
Claims (7)
1. A system for preparing baking soda by utilizing desulfurized ash is characterized by comprising a preheater, a dissolving unit, a multi-medium filter, a three-platen frame filter press, an organic matter removing unit, an aeration impurity removing unit, a fluorine removing unit, a salt separating unit, an evaporator, two centrifuges, three spray drying towers and a conversion unit;
the cold fluid inlet of the preheater is an inlet of water used by the dissolving unit, the cold fluid outlet of the preheater is connected with a liquid inlet of the dissolving unit, the hot fluid inlet of the preheater is connected with the steam outlet of the evaporator, and the hot fluid outlet of the preheater is a condensed water outlet;
the dissolving unit is provided with a desulfurized ash inlet, a discharge hole of the dissolving unit is connected with a feed hole of the multi-medium filter, a discharge hole of the multi-medium filter is connected with a feed hole of the organic matter removing unit, and a discharge hole of the organic matter removing unit is connected with a feed hole of the aeration impurity removing unit;
the bottom of each of the aeration impurity removal unit and the spray drying tower is provided with an air inlet and is connected with an air source;
the slurry outlet at the top of the aeration impurity removal unit is connected with the feed inlet of a first plate-and-frame filter press, the liquid outlet of the first plate-and-frame filter press is connected with the inlet of a fluorine removal unit, and the discharge outlet of the first plate-and-frame filter press is connected with the feed inlet of a first spray drying tower;
the defluorination unit is provided with a defluorination agent inlet, a discharge hole of the defluorination unit is connected with a feed hole of the second plate-and-frame filter press, and a liquid outlet of the second plate-and-frame filter press is connected with a feed hole of the salt separation unit;
the salt separation unit is characterized in that a liquid discharge port of the salt separation unit is connected with a feed port of the evaporator, a crystal discharge port of the salt separation unit is connected with a feed port of a first centrifugal machine, a discharge port of the first centrifugal machine is connected with a feed port of a first spray drying tower, and a discharge port of the first spray drying tower is connected with a feed port of the conversion unit;
the solid discharge hole of the evaporator is connected with the feed inlet of a second centrifugal machine, the discharge hole of the second centrifugal machine is connected with the feed inlet of a second spray drying tower, and the discharge hole of the second spray drying tower is a mixed salt outlet;
the conversion unit is provided with an ammonium bicarbonate inlet, a discharge hole of the conversion unit is connected with a feed inlet of a third plate-and-frame filter press, and a discharge hole of the third plate-and-frame filter press is connected with a feed inlet of a third spray drying tower; the liquid outlet of the third plate frame filter press is an ammonium sulfate outlet, and the discharge port of the third spray drying tower is a sodium bicarbonate product outlet.
2. A system for preparing baking soda by utilizing desulfurized ash is characterized by comprising a preheater, a dissolving unit, a leaching unit, a multi-medium filter, a three-platen frame filter press, an organic matter removing unit, an aeration impurity removing unit, a fluorine removing unit, a salt separating unit, an evaporator, two centrifuges, three spray drying towers and a conversion unit;
the cold fluid inlet of the preheater is an inlet of water used by the dissolving unit, the cold fluid outlet of the preheater is connected with a liquid inlet of the dissolving unit, the hot fluid inlet of the preheater is connected with the steam outlet of the evaporator, and the hot fluid outlet of the preheater is a condensed water outlet;
the dissolving unit is provided with a sodium sulfate inlet, and a discharge hole of the dissolving unit is connected with a feed inlet at the top of the leaching unit;
the top of the leaching unit is provided with a desulfurized fly ash inlet, a liquid discharge port of the leaching unit is connected with a feed inlet of the multi-media filter, and a solid discharge port of the leaching unit is connected with a feed inlet of the conversion unit; the discharge hole of the multi-medium filter is connected with the feed inlet of the organic matter removing unit, and the discharge hole of the organic matter removing unit is connected with the feed inlet of the aeration impurity removing unit;
the bottom of each of the aeration impurity removal unit and the spray drying tower is provided with an air inlet and is connected with an air source;
the slurry outlet at the top of the aeration impurity removal unit is connected with the feed inlet of a first plate-and-frame filter press, the liquid outlet of the first plate-and-frame filter press is connected with the inlet of a fluorine removal unit, and the discharge outlet of the first plate-and-frame filter press is connected with the feed inlet of a first spray drying tower;
the defluorination unit is provided with a defluorination agent inlet, a discharge hole of the defluorination unit is connected with a feed hole of the second plate-and-frame filter press, and a liquid outlet of the second plate-and-frame filter press is connected with a feed hole of the salt separation unit;
the salt separation unit is characterized in that a liquid discharge port of the salt separation unit is connected with a feed port of the evaporator, a crystal discharge port of the salt separation unit is connected with a feed port of a first centrifugal machine, a discharge port of the first centrifugal machine is connected with a feed port of a first spray drying tower, and a discharge port of the first spray drying tower is connected with a feed port of the conversion unit;
the solid discharge hole of the evaporator is connected with the feed inlet of a second centrifugal machine, the discharge hole of the second centrifugal machine is connected with the feed inlet of a second spray drying tower, and the discharge hole of the second spray drying tower is a mixed salt outlet;
the conversion unit is provided with an ammonium bicarbonate inlet, a discharge hole of the conversion unit is connected with a feed inlet of a third plate-and-frame filter press, and a discharge hole of the third plate-and-frame filter press is connected with a feed inlet of a third spray drying tower; the liquid outlet of the third plate frame filter press is an ammonium sulfate outlet, and the discharge port of the third spray drying tower is a sodium bicarbonate product outlet.
3. The system of claim 1 or 2, wherein the organic removal unit is an adsorption unit or an oxidation unit.
4. The system according to claim 3, wherein the organic substance removing unit is an adsorption unit, and the adsorption material in the adsorption unit is selected from one of carbon-based adsorption material, inorganic adsorption material, fiber adsorption material and adsorption resin.
5. The system of claim 3, wherein the organic matter removing unit is an oxidation unit selected from one or more of a chemical oxidation device, a wet oxidation device, a Fenton oxidation device, an ozone catalytic oxidation device, a photocatalytic oxidation device and an electrochemical oxidation device.
6. The system of claim 1 or 2, wherein the fluorine removal unit is selected from one or more of a calcium method fluorine removal device, an aluminum salt fluorine removal device and a resin adsorption fluorine removal device.
7. The system of claim 1 or 2, wherein the salt separation unit is selected from one or more of an evaporative crystallization device, a freeze crystallization device and a nanofiltration device.
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| CN202220743391.6U CN216837159U (en) | 2022-04-01 | 2022-04-01 | System for utilize desulfurization ash to make baking soda |
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| CN202220743391.6U CN216837159U (en) | 2022-04-01 | 2022-04-01 | System for utilize desulfurization ash to make baking soda |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117228694A (en) * | 2023-11-13 | 2023-12-15 | 北京康仑循环科技有限公司 | Method for preparing baking soda by using desulfurized fly ash |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117228694A (en) * | 2023-11-13 | 2023-12-15 | 北京康仑循环科技有限公司 | Method for preparing baking soda by using desulfurized fly ash |
| CN117228694B (en) * | 2023-11-13 | 2024-01-26 | 北京康仑循环科技有限公司 | Method for preparing baking soda by using desulfurized fly ash |
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