CN109850922B - Method and device for recycling baking soda desulfurization ash - Google Patents
Method and device for recycling baking soda desulfurization ash Download PDFInfo
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Abstract
The invention discloses a baking soda desulfurization ash recycling method and a device, wherein the method comprises the following steps: dissolving baking soda desulfurization ash and filtering to obtain a dissolving solution; reacting the dissolved solution with quicklime or lime milk under the condition of introducing gas containing carbon dioxide and oxygen to obtain slurry; solid-liquid separation is carried out on the slurry to obtain a calcium sulfate byproduct and a supernatant; and drying the baking soda crystals obtained by crystallizing the supernatant to obtain a baking soda product. The device comprises a dissolving unit, a filtering unit, an aeration reaction unit, a cyclone unit, a crystallization unit and a drying unit which are sequentially connected through pipelines, wherein a dissolving solution obtained by dissolving and filtering baking soda desulfurization ash enters the aeration reaction unit to react to obtain slurry, a supernatant obtained by separating the slurry through the cyclone unit is crystallized by the crystallization unit to obtain baking soda crystals, and then the baking soda crystals are dried by the drying unit to obtain baking soda products. The invention can solve the disposal problem of baking soda desulfurization ash in the prior art and reduce the running cost of baking soda desulfurization.
Description
Technical Field
The invention relates to the technical field of recycling of solid wastes, in particular to a method and a device for recycling baking soda desulfurization ash.
Background
Sodium bicarbonate (sodium bicarbonate) flue gas desulfurization technology is increasingly used in flue gas desulfurization projects in the non-electric industry due to the advantages of initial investment saving, small equipment occupation area, reduced system temperature, no wastewater generation and the like. However, for the desulfurization ash generated by the baking soda desulfurization process, an effective comprehensive utilization way is still lacking at present, and the stacking of the baking soda desulfurization ash needs to occupy a large amount of land and causes a plurality of environmental problems.
With the increasing strictness of environmental protection standards, not only is the pollutant emission concentration in the flue gas strictly controlled, but also the problems of solid waste generation and disposal are more and more emphasized. Therefore, it is important to develop an effective baking soda desulfurization ash recycling method.
On the other hand, compared with other desulfurization technologies, the unit price of the baking soda is higher than that of other desulfurizing agents, so that the operation cost of the baking soda desulfurization process is higher, the popularization of the baking soda desulfurization technology is limited, and the economic burden of enterprises is increased. If the baking soda desulfurization ash can be simply treated, the baking soda desulfurization ash can be regenerated into baking soda products which can be used for desulfurization, the running cost of enterprises can be obviously reduced, and the competitiveness of desulfurization technology is improved.
Disclosure of Invention
The invention aims to solve the disposal problem of baking soda desulfurization ash and reduce the operation cost of baking soda desulfurization in the prior art, and provides a recycling utilization method and device for converting baking soda desulfurization ash into a desulfurizing agent through simple treatment.
In one aspect, the invention provides a baking soda desulfurization ash recycling method, which comprises the following steps:
A. dissolving baking soda desulfurization ash and filtering to obtain a dissolving solution;
B. reacting the dissolved solution with quicklime or lime milk under the condition of introducing gas containing carbon dioxide and oxygen to obtain slurry;
C. solid-liquid separation is carried out on the slurry to obtain supernatant and byproduct calcium sulfate or gypsum;
D. and drying the baking soda crystals obtained by crystallizing the supernatant to obtain a baking soda product, wherein the purity of the baking soda product is higher than 99%.
According to one embodiment of the baking soda desulfurization ash recycling method, in the step A, process water or crystal lean liquid obtained by separating the supernatant liquid after crystallization is adopted to dissolve the baking soda desulfurization ash, wherein 100-150 kg of the baking soda desulfurization ash is added into each ton of process water, and 40-50 kg of the baking soda desulfurization ash is added into each ton of crystal lean liquid; the dissolution temperature is 30 to 60 ℃, preferably 35 to 40 ℃.
According to one embodiment of the baking soda desulfurization ash recycling method, in the step A, a quartz sand filter material or an anthracite filter material is adopted for filtering, wherein the filtering speed is 8-10 m/h, preferably 9m/h; the thickness of the filter material layer is 0.8-1.5 m, preferably 1.0-1.2 m; d, d 10 0.9 to 1.2.
According to one embodiment of the baking soda desulfurization ash recycling method of the present invention, in the step B, the addition mass ratio of the quicklime or lime milk to the baking soda desulfurization ash is controlled to be 0.35:1 to 0.45:1, preferably 0.4:1 to 0.42:1, a step of; the gas containing carbon dioxide and oxygen is purified flue gas or hot air, the temperature of the gas containing carbon dioxide and oxygen is 50-60 ℃, the reaction time is 0.5-1 h, and the discharge temperature of the slurry is controlled to be not more than 60 ℃.
According to one embodiment of the baking soda desulfurization ash recycling method, in the step D, baking soda crystal seeds are added during primary crystallization, the crystallization temperature is 20-30 ℃, a cooling crystallization medium is cooling water or cooling brine, the crystallization time is not less than 3 hours, the crystal growing time is not less than 6 hours, and the crystal granularity of baking soda crystals is controlled to be larger than 0.5mm.
According to one embodiment of the baking soda desulfurization ash recycling method, in the step D, the drying medium is purified flue gas or hot air, the temperature of the drying medium is 70-80 ℃, the drying time is not more than 20 minutes, the discharge temperature of baking soda products is not more than 60 ℃, and the drying medium subjected to heat exchange and temperature reduction is used as gas containing carbon dioxide and oxygen to be introduced into the dissolution liquid for reaction.
The invention further provides a baking soda desulfurization ash recycling device, which comprises a dissolving unit, a filtering unit, an aeration reaction unit, a cyclone unit, a crystallization unit and a drying unit which are sequentially connected through pipelines, wherein a dissolving liquid obtained by dissolving and filtering baking soda desulfurization ash enters the aeration reaction unit to react with quicklime or lime milk and introduced gas containing carbon dioxide and oxygen to obtain slurry, supernatant obtained by separating the slurry by the cyclone unit is crystallized by the crystallization unit to obtain baking soda crystals, and the baking soda crystals are dried by the drying unit to obtain baking soda products.
According to one embodiment of the baking soda desulfurization ash recycling device, a first stirring unit is arranged in the dissolving unit, and the dissolving unit is also connected with the crystallization unit through a crystallization lean solution return pipe; the filter unit is internally provided with a filter material layer with the thickness of 0.8-1.5 m, and the filter material of the filter material layer is quartz sand filter material or anthracite filter material.
According to one embodiment of the baking soda desulfurization ash recycling device, the aeration reaction unit is provided with a second stirring unit and an aeration pipe, and the aeration pipe is connected with the drying unit through a drying medium return pipe and a fan; the rotational flow unit is a suspension separator with 2-3 stages connected in series.
According to one embodiment of the baking soda desulfurization ash recycling device, the crystallization unit is an indirect heat exchange cooling crystallizer, a crystal growing area is arranged in the crystallization unit, and the cooling medium is cooling water or frozen brine; the drying unit is a normal pressure or micro-positive pressure dryer, and the drying medium is purified flue gas or hot air.
Compared with the prior art, the invention can fully utilize the carbon dioxide in the flue gas to convert the baking soda desulfurization ash into the desulfurizing agent baking soda, effectively solve the problem of treatment of the desulfurization ash and has no wastewater discharge problem. In addition, sulfate radical in baking soda desulfurized ash can be utilized to convert low-added-value quicklime into high-added-value calcium sulfate byproducts or gypsum, so that the full and reasonable utilization of solid waste resources is realized.
Drawings
Fig. 1 shows a schematic structure of a baking soda desulfurization ash recycling apparatus according to an exemplary embodiment of the present invention.
Reference numerals illustrate:
1-dissolving unit, 11-first stirring unit, 2-filtering unit, 21-filter layer, 3-aeration reaction unit, 31-second stirring unit, 32-aeration pipe (containing aeration nozzle), 4-cyclone unit, 41-calcium sulfate byproduct or gypsum, 42-supernatant, 5-crystallization unit, 51-baking soda crystal, 52-crystallization lean solution, 53-crystallization lean solution return pipe, 6-drying unit, 61-drying medium return pipe, and 7-fan.
Detailed Description
All of the features disclosed in this specification, or all of the steps in a method or process disclosed, may be combined in any combination, except for mutually exclusive features and/or steps.
Any feature disclosed in this specification may be replaced by alternative features serving the same or equivalent purpose, unless expressly stated otherwise. That is, each feature is one example only of a generic series of equivalent or similar features, unless expressly stated otherwise.
The baking soda desulfurization ash recycling method of the invention is specifically described and illustrated below. Wherein, the baking soda disclosed by the invention is named as sodium bicarbonate.
According to an exemplary embodiment of the present invention, the baking soda desulfurization ash recycling method includes the following steps.
Step A:
first, baking soda desulfurization ash is dissolved and filtered to obtain a solution.
The main byproducts of baking soda desulfurization are sodium sulfate, sodium sulfite and sodium carbonate, which is decomposed by unreacted sodium bicarbonate under heat, i.e., baking soda desulfurization ash mainly comprises sodium sulfate, sodium sulfite and sodium carbonate.
The step specifically comprises the steps of dissolving baking soda desulfurization ash to form a dissolving solution, and filtering to remove insoluble matters and suspended matters in the dissolving solution so as to carry out subsequent reactions.
Specifically, the baking soda desulfurization ash can be dissolved by adopting process water, wherein 100-150 kg of baking soda desulfurization ash is added into each ton of process water, and the dissolution temperature is controlled to be 30-60 ℃, preferably 35-40 ℃.
During filtration, quartz sand filter materials or anthracite filter materials can be adopted for filtration, and insoluble substances and suspended substances in the solution are trapped by the filter materials. Wherein, the filtration speed is controlled to be 8-10 m/h, preferably 9m/h; the thickness of the filter material layer is 0.8-1.5 m, preferably 1.0-1.2 m; d, d 10 0.9 to 1.2.
And (B) step (B):
and C, reacting the filtered solution obtained in the step A with quicklime or lime milk under the condition of introducing gas containing carbon dioxide and oxygen to obtain slurry.
The baking soda desulfurization ash solution can react with quicklime or lime milk through aeration to generate sodium bicarbonate and calcium sulfate byproducts or gypsum, and the reaction formula is as follows:
3CaO+Na 2 CO 3 +2Na 2 SO 3 +Na 2 SO 4 +O 2 +7CO 2 +4H 2 O→8NaHCO 3 +3CaSO 4
CaSO 4 +2H 2 O→CaSO 4 .2H 2 O
in the step, the adding mass ratio of the quicklime or lime milk to the desulfurized fly ash is controlled to be 0.35:1 to 0.45:1, preferably 0.4:1 to 0.42:1. the gas containing carbon dioxide and oxygen is preferably purified flue gas or hot air, wherein the temperature of the gas containing carbon dioxide and oxygen is controlled to be 50-60 ℃, the aeration reaction time is 0.5-1 h, and the discharge temperature of the slurry is controlled to be not more than 60 ℃.
Thus, sodium carbonate, sodium sulfate and sodium sulfite in baking soda desulfurization ash are converted into sodium bicarbonate (baking soda) and byproduct calcium sulfate or gypsum through a series of chemical reactions, and a suspension slurry is formed under stirring.
Step C:
and B, carrying out solid-liquid separation on the slurry obtained in the step B to obtain supernatant and byproduct calcium sulfate or gypsum.
Since calcium sulfate or gypsum is a solid precipitate, it will sink during the solid-liquid separation process and be discharged for continued use as a by-product. The supernatant of sodium bicarbonate dissolved in water can be separated for subsequent treatment to obtain sodium bicarbonate product.
Step D:
and C, crystallizing the supernatant obtained in the step C to obtain sodium bicarbonate crystals, and drying the sodium bicarbonate crystals to obtain sodium bicarbonate products, wherein the purity of the sodium bicarbonate products is higher than 99%, so that the sodium bicarbonate products can be continuously used for desulfurizing sodium bicarbonate, and the desulfurizing cost is reduced.
Since the solubility of baking soda decreases with decreasing temperature, baking soda is crystallized from the supernatant liquid during the cooling process to form baking soda crystals. In the crystallization step, sodium bicarbonate seed crystals are preferably added during the primary crystallization, and the crystallization temperature is controlled to be 20-30 ℃. The cooling crystallization medium can be cooling water or cooling brine, the crystallization time is not less than 3 hours, the crystal growing time is not less than 6 hours, and finally the crystal granularity of the baking soda crystal is controlled to be more than 0.5mm.
The crystallized lean solution obtained by separation after crystallization can be returned to the step A for dissolving baking soda desulfurization ash, so that the generation of wastewater can be reduced. At this time, 40-50 kg of baking soda desulfurization ash is added into each ton of crystallization lean solution to prepare a dissolution solution.
In the drying step, the drying medium is purified flue gas or hot air, and more preferably purified flue gas, because carbon dioxide contained in the flue gas can effectively inhibit decomposition of baking soda. Therefore, the drying medium subjected to heat exchange and temperature reduction can be used as gas containing carbon dioxide and oxygen to be pressurized and then introduced into the dissolving liquid for reaction in the step C.
Preferably, the temperature of the drying medium is 70-80 ℃, the drying time is not more than 20 minutes, and the discharge temperature of the baking soda product is controlled not more than 60 ℃.
The device of the invention will be described in detail with reference to the accompanying drawings.
Fig. 1 shows a schematic structure of a baking soda desulfurization ash recycling apparatus according to an exemplary embodiment of the present invention.
As shown in fig. 1, the baking soda desulfurization ash recycling apparatus according to an exemplary embodiment of the present invention includes a dissolving unit 1, a filtering unit 2, an aeration reaction unit 3, a cyclone unit 4, a crystallization unit 5, and a drying unit 6, which are sequentially connected through pipes.
Dissolving baking soda desulfurization ash, filtering to obtain a solution, introducing the solution into an aeration reaction unit 3, reacting with quicklime or lime milk and introduced gas containing carbon dioxide and oxygen to obtain slurry, separating the slurry by a cyclone unit 4 to obtain supernatant, crystallizing by a crystallization unit 50 to obtain baking soda crystals, and drying the baking soda crystals by a drying unit 6 to obtain a baking soda product.
According to the present invention, the first stirring unit 11 is provided in the dissolving unit 1, and the first stirring unit 11 is advantageous in accelerating the dissolution of the dissolved ash and maintaining the insoluble matters of the baking soda desulfurization ash in a suspended state. And, the dissolution unit 1 is also connected to the crystallization unit 5 through the crystallization lean liquid return pipe 53, so that the crystallization lean liquid obtained after crystallization can be returned for dissolution of baking soda desulfurization ash. Therefore, when the process water or the crystallized lean solution after crystallization is used for dissolution, the process water or the crystallized lean solution and the baking soda desulfurization ash are mixed according to a certain proportion (the process water is adopted for primary dissolution), and then the dissolution is carried out in the dissolution unit 1, and the dissolution unit 1 is preferably provided with a matching instrument such as a liquid level meter, a thermometer and the like.
Filtration sheetThe element 2 is provided with a filter material layer 21 with the thickness of 0.8-1.5 m, and the filter material of the filter material layer 21 is quartz sand filter material or anthracite filter material. Specifically, the solution prepared by the dissolving unit 1 is delivered to the filtering unit by gravity flow or a pump, and insoluble substances and suspended substances in the solution are trapped when passing through the filtering material layer 21, so that the turbidity of the filtrate at the outlet of the filtering unit 2 is less than 5NTU. Wherein the filter material layer 21 is preferably uniform-graded quartz sand filter material, and d is preferably 10 The value is 0.9-1.2; suitable filtration rates are 8 to 10m/h, preferably 9m/h; the thickness of the filter material layer is 0.8-1.5 m, and the thickness of the filter material layer is 1.0-1.2 m.
The aeration reaction unit 3 is provided therein with a second stirring unit 31 and an aeration pipe 32, the aeration pipe 32 is provided with an aeration nozzle and is used for introducing a gas containing carbon dioxide and oxygen into the aeration reaction unit 3 to perform an aeration reaction, and the second stirring unit 31 is advantageous in promoting the progress of the reaction and forming a suspension slurry. The aeration pipe 32 is connected with the drying unit 6 through the drying medium return pipe 61 and the fan 7, so that the drying medium can be used as the reaction gas of the aeration reaction to participate in the reaction after heat exchange and temperature reduction from the drying unit 6, and the gas utilization rate is improved. Preferably, the aeration reaction unit 3 is provided with a thermometer, a PH meter and other matched instruments.
Specifically, the dissolved solution at the outlet of the filtering unit 2 is fed to the aeration reaction unit 3 by gravity flow or a water pump, quicklime powder or lime milk is added into the aeration reaction unit 3, and is fully mixed with the dissolved solution under the action of the second stirring unit 31 and subjected to chemical reaction under the aeration condition, and sodium carbonate, sodium sulfite and sodium sulfate in the dissolved solution are converted into calcium sulfate or gypsum and sodium bicarbonate (baking soda). That is, through a series of chemical reactions, the dissolution solution and quicklime powder or lime milk are converted into a mixed slurry of sodium bicarbonate (baking soda) solution and calcium sulfate or gypsum in the aeration reaction unit 3, and the total chemical equation occurring in the aeration reaction unit 3 is:
3CaO+Na 2 CO 3 +2Na 2 SO 3 +Na 2 SO 4 +O 2 +7CO 2 +4H 2 O→8NaHCO 3 +3CaSO 4 ↓
the addition amount of the quicklime powder or the lime milk can be accurately calculated according to the desulfurization components and the chemical reaction coefficients. The aeration is used for providing carbon dioxide and oxygen required by chemical reaction, and the gas used can be purified flue gas or hot air doped with a certain proportion of carbon dioxide, or any mixed gas containing a certain amount of carbon dioxide and oxygen.
The cyclone unit 4 can be a suspension separator with 2-3 stages connected in series or other devices capable of playing a role in solid-liquid separation. The suspension slurry generated by the aeration reaction unit 3 enters the cyclone unit 4 for solid-liquid separation, the obtained solid phase substance is the byproduct calcium sulfate or gypsum, and the baking soda solution in liquid phase enters the crystallization unit 5 for subsequent treatment.
The crystallization unit 5 is an indirect heat exchange cooling crystallizer, a crystal growing area is arranged in the crystallization unit, and the cooling medium is cooling water or chilled brine. Specifically, the supernatant (baking soda solution) entering the crystallization unit 5 is cooled down, and as the solubility of baking soda decreases with a decrease in temperature, baking soda is crystallized out of the solution in the crystallization unit 5. The baking soda solution is cooled by indirect heat exchange, the proper crystallization temperature is 20-30 ℃, and the cooling medium can be cooling water or chilled brine existing in factories. Preferably, sodium bicarbonate seed crystals are added to the crystallization unit 5 at the time of initial operation.
The drying unit 6 is a normal pressure or micro-positive pressure dryer, the drying medium is purified flue gas or hot air, preferably purified flue gas is adopted, and carbon dioxide contained in the flue gas can effectively inhibit decomposition of baking soda. The precipitated crystals are dried by flue gas in a drying unit 6, and the purity of the sodium bicarbonate crystals after drying is higher than 99%.
Taking a certain coking plant flue gas desulfurization project as an example, the design flue gas volume is 400000Nm 3 /h, the original SO in the flue gas 2 The concentration was 400mg/Nm 3 Flue gas SO after desulfurization 2 The discharge concentration was 35mg/Nm 3 The usage amount of the desulfurizer is 350kg/h. The baking soda is 1800 yuan/ton per unit price, and the limestone powder is 450 yuan/ton per unit price, so that the desulfurization can be saved every year after the invention is adoptedThe running cost of the agent is about 462 ten thousand yuan. In addition, the invention solves the disposal problem of the desulfurization ash, and the byproduct calcium sulfate or gypsum can obtain considerable benefit, wherein the benefit is about 80 ten thousand yuan per year according to the calculation of the unit price of the calcium sulfate of 350 yuan per ton, and the economic benefit is huge.
The invention is not limited to the specific embodiments described above. The invention extends to any novel one, or any novel combination, of the features disclosed in this specification, as well as to any novel one, or any novel combination, of the steps of the method or process disclosed.
Claims (11)
1. The method for recycling baking soda desulfurization ash is characterized by comprising the following steps of:
A. dissolving baking soda desulfurization ash and filtering to obtain a dissolving solution;
B. reacting the dissolved solution with quicklime or lime milk under the condition of introducing gas containing carbon dioxide and oxygen to obtain slurry;
C. solid-liquid separation is carried out on the slurry to obtain supernatant and byproduct calcium sulfate or gypsum;
D. and drying the baking soda crystals obtained by crystallizing the supernatant to obtain a baking soda product, wherein the purity of the baking soda product is higher than 99%.
2. The recycling method of baking soda desulfurization ash according to claim 1, wherein in the step a, the baking soda desulfurization ash is dissolved by using process water or a crystallization lean solution obtained by separating the supernatant after crystallization, wherein 100-150 kg of baking soda desulfurization ash is added into each ton of process water, and 40-50 kg of baking soda desulfurization ash is added into each ton of crystallization lean solution; the dissolution temperature is 30-60 ℃.
3. The method for recycling baking soda desulfurization ash according to claim 1, wherein the dissolution temperature is 35-40 ℃.
4. The method for recycling baking soda desulfurization ash according to claim 1, wherein in the step A, a quartz sand filter material or an anthracite filter material is adopted for filtering, and the filtering speed is 8-10 m/h; the thickness of the filter material layer is 0.8-1.5 m; d10 is 0.9 to 1.2.
5. The method for recycling baking soda desulfurization ash according to claim 1, wherein in the step A, a quartz sand filter material or an anthracite filter material is adopted for filtering, and the filtering speed is 9m/h; the thickness of the filter material layer is 1.0-1.2 m; d10 is 0.9 to 1.2.
6. The method for recycling baking soda desulfurization ash according to claim 1, characterized in that in the step B, the addition mass ratio of the quicklime or lime milk to the baking soda desulfurization ash is controlled to be 0.35:1 to 0.45:1, a step of; the gas containing carbon dioxide and oxygen is purified flue gas or hot air, the temperature of the gas containing carbon dioxide and oxygen is 50-60 ℃, the reaction time is 0.5-1 h, and the discharge temperature of the slurry is controlled to be not more than 60 ℃.
7. The method for recycling baking soda desulfurization ash according to claim 1, wherein in the step B, the addition mass ratio of the quicklime or lime milk to the baking soda desulfurization ash is controlled to be 0.4:1 to 0.42:1.
8. the recycling method of baking soda desulfurization ash according to claim 1, wherein in the step D, baking soda seed crystal is added during primary crystallization, the crystallization temperature is 20-30 ℃, the cooling crystallization medium is cooling water or cooling brine, the crystallization time is not less than 3 hours, the crystal growth time is not less than 6 hours, and the crystal granularity of baking soda crystals is controlled to be more than 0.5mm.
9. The method for recycling baking soda desulfurization ash according to claim 1 or 6, wherein in the step D, the drying medium is purified flue gas or hot air, the temperature of the drying medium is 70-80 ℃, the drying time is not more than 20 minutes, the discharge temperature of baking soda products is not more than 60 ℃, and the drying medium subjected to heat exchange and temperature reduction is used as gas containing carbon dioxide and oxygen to be introduced into the dissolution liquid for reaction.
10. The device is characterized by comprising a dissolving unit, a filtering unit, an aeration reaction unit, a cyclone unit, a crystallization unit and a drying unit which are sequentially connected through pipelines, wherein a dissolving liquid obtained by dissolving and filtering the baking soda desulfurization ash enters the aeration reaction unit to react with quicklime or lime milk and introduced gas containing carbon dioxide and oxygen to obtain slurry, supernatant obtained by separating the slurry through the cyclone unit is crystallized through the crystallization unit to obtain baking soda crystals, the baking soda crystals are dried through the drying unit to obtain baking soda products, and a first stirring unit is arranged in the dissolving unit and is connected with the crystallization unit through a crystallization lean solution return pipe; the filter unit is internally provided with a filter material layer with the thickness of 0.8-1.5 m, the filter material of the filter material layer is quartz sand filter material or anthracite filter material, the aeration reaction unit is internally provided with a second stirring unit and an aeration pipe, and the aeration pipe is connected with the drying unit through a drying medium return pipe and a fan; the rotational flow unit is a suspension separator with 2-3 stages connected in series.
11. The baking soda desulfurization ash recycling device according to claim 10, wherein the crystallization unit is an indirect heat exchange cooling crystallizer and is internally provided with a crystal growing area, and the cooling medium is cooling water or chilled brine; the drying unit is a normal pressure or micro-positive pressure dryer, and the drying medium is purified flue gas or hot air.
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| CN110451532A (en) * | 2019-08-28 | 2019-11-15 | 淮阴工学院 | A kind of sodium method Desulphurization recycling processing method |
| CN112047363A (en) * | 2020-10-05 | 2020-12-08 | 湖南海联三一小苏打有限公司 | Sodium bicarbonate desulfurized fly ash resource utilization method |
| CN114920277A (en) * | 2022-05-07 | 2022-08-19 | 昆明理工大学 | Method and device for preparing alpha-semi-hydrated gypsum by dry desulphurization slag elution crystallization |
| CN114772626A (en) * | 2022-06-02 | 2022-07-22 | 武汉华德环保工程技术有限公司 | Method for co-producing sodium sulfate and calcium carbonate from sodium bicarbonate desulfurized fly ash |
| CN115403059B (en) * | 2022-09-02 | 2023-07-07 | 东方电气集团东方锅炉股份有限公司 | Method and system for recycling baking soda dry desulfurization ash |
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