CN108584971A - A method of preparing high mode soluble silicate using gasification slag - Google Patents
A method of preparing high mode soluble silicate using gasification slag Download PDFInfo
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- CN108584971A CN108584971A CN201810421417.3A CN201810421417A CN108584971A CN 108584971 A CN108584971 A CN 108584971A CN 201810421417 A CN201810421417 A CN 201810421417A CN 108584971 A CN108584971 A CN 108584971A
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/20—Silicates
- C01B33/32—Alkali metal silicates
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
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Abstract
The present invention provides a kind of methods preparing high mode soluble silicate using gasification slag, and described method includes following steps：(1) gasified slag with Ore Leaching, after separation of solid and liquid, obtain activation gasification slag and liquid phase；(2) lye of activation gasification slag and a concentration of 1 5mol/L of hydroxide ion is subjected to desilication reaction at 85 105 DEG C, is separated by solid-liquid separation later, obtains desiliconization liquid and solid phase；(3) desiliconization liquid is post-processed, obtains high mode soluble silicate.The method is compared with the existing technology, without adding any silicon source, raw material sources are extensive, and reaction condition is mild, and process is simple, easy to operate, obtained silicate product quality is higher, for modulus 1.5 2.5, production cost is low, does not generate secondary solid and liquid pollutant, realize that the minimizing of gasification slag, recycling efficiently utilize, economy and obvious environment benefit.
Description
Technical field
The invention belongs to inorganic chemical industry solid wastes recycling utilize technical field, be related to it is a kind of using gasification slag prepare high mode
The method of soluble silicate.
Background technology
Coal gasifying process is one of the main path for producing synthesis gas product, includes mainly fixed bed gasification technology, fluidisation
Solid coal is converted to gaseous synthesis gas by bed gasification technology and entrained flow bed gasification technology, while byproduct steam, tar are (a
Other gasification technology) and the byproducts such as lime-ash.With increasing substantially for synthesis gas product demand, the inorganic lime-ash of by-product is also with big
Amount discharge and stockpiling, cause serious problem of environmental pollution.
The physical characteristic of lime-ash is generated for coal gasification course, CN106336164A and CN106467376A are individually disclosed
A method of prepared using gasification slag it is non-burning brick, using the slag that gasifies as raw material, add thereto cement, sweetened bean paste stone or gangue and
The substances such as slag adjust composition ratio and are mixed, and unburned brick product is obtained after overmolding-maintenance；In order to improve utilization of ash and slag
Added value, CN104774023A and CN105130487A are individually disclosed a kind of preparing Lightweight ceramic using the gentle slugging of flyash
The method of grain and ceramic for filtration is added and is helped on a small quantity after mixing flyash, gasification slag and sodium/potassium feldspar according to a certain percentage
Agent be molded-dry-processes such as firing, qualified light ceramic and ceramic for filtration product can be obtained.Based on its chemical composition
Feature, CN106800416A disclose it is a kind of using the gasification slag method for preparing low-creep refractory brick, with the slag that gasifies, cordierite,
Fused alumina zirconia, lime stone, flyash and feldspar etc. are raw material, the auxiliary agents such as boron carbide fibre and nanometer tungsten oxide are added, by fine grinding-
The workshop sections such as microwave high-temperature sintering-washing-drying obtain the refractory material that mechanical performance is high, creep properties is low and anti-seismic performance is good.Base
In the high feature of gasification slag phosphorus content, CN102980195A discloses a kind of processing method of coal chemical industry gasification slag, by the slag that gasifies
Clay wash is added after evenly mixing with coal slime, and being passed to fluidized-bed combustion boiler by conveyance conduit burns, and improves wherein
The utilization ratio of carbon.But slag mixed ratio is low and valuable resource is lost in the problems such as serious, Wu Fashi there are still gasification for the above method
Now gasify slag full dose and higher value application.
Soluble silicate is a kind of water-soluble silicate, and aqueous solution is commonly called as waterglass, is a kind of mine binder, tool
Have that cohesive force is strong, intensity is higher and an acid resistance/it is heat-resist the features such as.Its chemical formula is R2O·nSiO2, R in formula2O is alkali gold
Belong to oxide, n is the ratio of silica and alkali metal oxide molal quantity, the referred to as number that rubs of waterglass, is to weigh silicate
The important parameter of quality.Different modulus silicate purposes are different, can be widely applied to conventional cast, hot investment casting, papermaking,
The various fields such as ceramics, clay, ore dressing, kaolin and washing.
Presently mainly it is prepared not by carrying out siliceous raw ore (silica and quartz etc.) and the alkali to mix high temperature sintering
With modulus sodium metasilicate product.CN106829983A, CN107215878A and CN107720766A individually disclose a kind of utilize and contain
Silicon mineral (fluorine-containing white residue, rice hull ash or gangue etc.) is mixed with sodium carbonate, and is sintered difference is obtained by the reaction at high temperature
The sodium metasilicate product of quality.CN106966403A discloses a kind of production method of liquid sodium silicate, by quartz and sodium hydroxide
The high-quality sodium silicate product that modulus is 3.2-3.4 can be prepared in solution reaction for a long time under high temperature, high pressure system.On but
It is low to state silicon source reactivity in production sodium metasilicate product process, and reacts item and asks harsh, reaction process energy consumption and material consumption are higher,
Economy and environmental benefit be not notable.
Invention content
In view of the deficiencies of the prior art, the present invention intends to provide it is a kind of using gasification slag prepare high mode can
Silicon can be realized by the mutual cooperation of acid activation and controllable desiliconization in the method for soluble silicate under mild reaction conditions
Substantially dissolution, improve soluble silicate modulus in liquid phase, without adding any silicon source, can access modulus be 1.5-
2.5 high-quality mensuration dissolubility silicic product salt, while secondary solid and liquid pollutant are not generated, realize gasification slag minimizing
It is efficiently utilized with recycling, economy and obvious environment benefit.
Unless otherwise specified, the liquid-solid ratio refers to the mass ratio of liquid and solid to the present invention.
The high mode soluble silicate refers to that the modulus of soluble silicate is 1.5-2.5.
For this purpose, the present invention uses following technical scheme：
A method of high mode soluble silicate being prepared using gasification slag, described method includes following steps：
(1) gasification slag is leached with acid solution, after separation of solid and liquid, obtains activation gasification slag and liquid phase；
(2) it is anti-that the lye of activation gasification slag and a concentration of 1-5mol/L of hydroxide ion are carried out to desiliconization at 85-105 DEG C
It answers, is separated by solid-liquid separation later, obtain desiliconization liquid and solid phase；
(3) desiliconization liquid is post-processed, obtains high mode soluble silicate.
The present invention coordinates subsequent controllable desiliconization by carrying out leaching activation to gasification slag, and can prepare modulus is
The high-quality mensuration dissolubility silicic product salt of 1.5-2.5, while secondary solid and liquid pollutant are not generated, it realizes gasification slag and subtracts
Quantization and recycling efficiently utilize, economy and obvious environment benefit.Compared with the existing technology, preparation provided by the invention is soluble
The method of silicate is without adding any silicon source, and raw material sources are extensive, and reaction condition is mild, and process is simple, easy to operate.
Preparation method provided by the invention by the concentration and lye and activation that control lye gasify the temperature reacted of slag into
The controllable desiliconization of row, removing activate silicon more than 60% (mass percentage) in gasification slag.Lye described in controllable desiliconization process
A concentration of 1-5mol/L, such as 1.5mol/L, 2.0mol/L, 2.5mol/L, 3.8mol/L, 4.3mol/L or 4.8mol/L；
The lye and temperature react of activation gasification slag are 85-105 DEG C, such as 88 DEG C, 90 DEG C, 95 DEG C, 100 DEG C or 103 DEG C.Do not exist
In above range, then cause desilication efficiency low, the modulus of soluble silicate is relatively low in liquid phase.
Pasc reaction activity is relatively low in gasification slag, can not be decomposed and is removed in solution under the conditions of low temperature diluted alkaline, passed through
Gasification slag is activated with acid, the activity of the silicon in gasification slag can be significantly improved so that soluble silicate in desiliconization liquid
Modulus significantly improve, therefore, gasification slag must be activated before controllable desiliconization, acid activation and controllable desiliconization cooperate,
The desiliconization liquid of high mode can be just obtained, and then obtains high mode soluble silicate.
Separation of solid and liquid in step (1) and step (2) is the operation of this field routine, typical but non-limiting solid-liquid point
It such as centrifuges or filters from mode.
Step (1) acid not only plays the role of activation, additionally it is possible to which the content for reducing impurity in gasification slag improves simultaneously
The reactivity of glass aerosil.
Step (1) it is described acid in hydrochloric acid, sulfuric acid or nitric acid any one or at least two combination, it is typical but non-
Restrictive combination such as hydrochloric acid and sulfuric acid, hydrochloric acid and nitric acid, sulfuric acid and nitric acid etc..
Preferably, the hydrochloric acid is selected from industrial by-product hydrochloric acid and/or technical hydrochloric acid.
Preferably, the hydrogen ion concentration of step (1) acid is in 3-10mol/L, as 3.5mol/L, 4.5mol/L,
4.8mol/L, 5.2mol/L, 5.8mol/L, 6.0mol/L, 7.0mol/L, 8.0mol/L, 9.5mol/L or 9.8mol/L etc..
Preferably, step (1) acid and the liquid-solid ratio of gasification slag are 3:1-8:1, such as 4:1、5:1、6:1 or 7:1 etc..
The temperature of step (1) described leaching is 75-95 DEG C, such as 78 DEG C, 80 DEG C, 85 DEG C, 88 DEG C or 92 DEG C.
Preferably, the time of step (1) described leaching is 60-180min, such as 80min, 100min, 120min or 150min
Deng.
Preferably, step (1) leaching carries out under water bath condition.
Step (1) is：Circulating leaching is carried out to gasification slag using hydrochloric acid, is separated by solid-liquid separation, obtains activation gasification slag and liquid phase.
After carrying out circulating leaching to gasification slag using hydrochloric acid, obtained liquid phase is rich molten aluminum phase, can be further used for preparing polymerization chlorine
Change aluminium.The circulating leaching refers to using previous leaching using hydrochloric acid activation gasification slag, leaching later when leaching for the first time
Go out liquid and leach previous leached mud, until cycle terminates.
Preferably, the number of the cycle is 5 times or more, and such as 5 times, 6 times, 7 times, 8 times, 9 times, 10 times or 15 are inferior, lead to
Aluminium ion concentration in liquid phase can be improved to 50-60g/L after crossing 5 times or more cycles, (quality percentage contains simultaneous oxidation aluminium content
Amount) reach 7.5-9.5% or more.
Preferably, part hydrochloric acid is added in the cyclic process of the circulating leaching, the part refers to that the hydrochloric acid added accounts for
The volume of total leaching agent is more than 0 and is less than 100%.
Preferably, it adds a concentration of of hydrochloric acid and is more than 300g/L, such as 310g/L, 320g/L, 350g/L, 380g/L, 390g/
L, it is best can to reach leaching effect at this time by 420g/L or 450g/L etc..
The liquid phase carries out polymerisation with basic salt, and curing obtains aluminium polychloride.
Preferably, the basic salt in calcium aluminate, calcium oxide or the calcium base solid waste any one or at least two
Combination.Typical but non-limiting combination such as calcium aluminate and calcium oxide, calcium aluminate and calcium base solid waste, calcium aluminate, calcium oxide and calcium
Base solid waste.
Preferably, the calcium base solid waste is selected from Industry Waste phosphorus slag and/or high calcium fluidization bed fly ash.
Preferably, the liquid phase and the liquid-solid ratio of basic salt are 6-15mL/g, as 7mL/g, 8mL/g, 9mL/g, 10mL/g,
11mL/g, 12mL/g or 14mL/g etc..
Preferably, in 2-4 addition liquid phase of the alkaline salinity, such as 3 is inferior.
Preferably, the addition partial alkaline salt into liquid phase, if overlong time is added portionwise, body is added every 0.5-1.5h
Being hydrochloric acid volatilization reduces acidity to reduce the dissolving of basic salt, causes basic salt to waste, product basicity reduces；If in batches
The addition time is too short, and basic salt is unable to fully quickly dissolve, and will also basic salt be caused to waste.
Preferably, the temperature of the polymerisation is 75-95 DEG C, such as 78 DEG C, 80 DEG C, 85 DEG C, 88 DEG C or 92 DEG C.
Preferably, the time of the polymerisation be 60-210min, as 80min, 100min, 120min, 150min,
180min or 200min etc..
Preferably, pH is controlled when the polymerisation as 3-5, such as 4.
Preferably, the temperature of the curing is 45-75 DEG C, such as 50 DEG C, 60 DEG C, 65 DEG C or 72 DEG C.
Preferably, the time of the curing is 18-36h, such as 20h, 22h, 25h, 28h, 30h or 34h.
Step (1) is as a preferred technical solution,：The hydrochloric acid for being 4-10mol/L with hydrogen ion concentration is by liquid-solid ratio
3:1-8:1 circulating leaching gasification slag, recycle 5 times or more, the temperature of circulating leaching is 75-95 DEG C, and the time leached every time is 60-
180min, it is more than 300g/L hydrochloric acid that moiety concentrations are added in cyclic process, and circulating leaching is carried out under water bath condition, lived
Change gasification slag and liquid phase；
Preferably, liquid phase and basic salt are subjected to polymerisation 60-210min, liquid under conditions of temperature is 75-95 DEG C
It is mutually 6-15mL/g with the liquid-solid ratio of basic salt, wherein the addition partial alkaline salt into liquid phase, alkalinity is added every 0.5-1.5h
In 2-4 addition liquid phase of salinity, 18-36h is cured under conditions of 45-75 DEG C later, obtains aluminium polychloride.
Circulating leaching is carried out using hydrochloric acid, and then prepares aluminium polychloride and has the following advantages that：Only it is by circulating leaching
The content of aluminium oxide in liquid phase can be improved, aluminium ion concentration in liquid phase can be improved to 50-60g/L, simultaneous oxidation aluminium content (matter
Measure percentage composition) up to 7.5% or more, without adding any silicon source, operating process is simple, and operating flexibility is big, acidleach post activation gas
Slugging impurity content is low, Fe2O3Content is reduced to 1% or so by 9%, and CaO content is reduced to 1% or so, Na by 6%2O content
Be reduced to 0.5% or so by 3%, and should during non-secondary pollution object generate, prepared for silica-base material and building materialsization be using carrying
For a kind of quality raw materials, economy and environmental benefit joint development are realized；The method that aluminium polychloride is prepared using gasification slag is anti-
Mild condition is answered, preparing industry for aluminium polychloride provides a kind of new technology and new raw material, alleviates the high-quality bauxite money in China
Source is exhausted；Gasification slag is replaced with into other materials, the method that can not use circulating leaching prepares aluminium polychloride.
The aluminium polychloride product alumina content (mass percentage) that the method obtains reaches 7.8% or more, salt
Base degree is 54%-82%, and density reaches 1.15g/cm3More than.
Step (2) described lye is selected from sodium hydroxide solution and/or potassium hydroxide solution.The lye can also be other
Substance, as long as its metal ion can with silicate ion formed soluble-salt.
The liquid-solid ratio of the lye and activation gasification slag is 3:1-6:1, such as 3.5:1、4.0:1、4.5:1、4.8:1、5.2:
1、5.5:1 or 5.8:1 etc..
Preferably, the time of step (2) described desilication reaction be 90-240min, as 110min, 130min, 150min,
180min, 190min, 210min or 230min etc..
Step (2) described solid phase can be used for preparing sorbing material after drying.
Step (3) it is described post-processing include：Desiliconization liquid is concentrated into the 60%-90% of original volume, such as 65%, 70%,
75%, 80%, 85% or 88% etc..
Preferably, the concentration is evaporation and concentration.
Preferably, step (1) and/or step (2) are used to prepare after the steam cooling generated in the evaporating concentration process
Required acid and/or aqueous slkali.
Preferably, the temperature after cooling is 55-85 DEG C, such as 58 DEG C, 60 DEG C, 65 DEG C, 70 DEG C, 78 DEG C or 82 DEG C.
As most preferred technical solution, described method includes following steps：
(1) hydrochloric acid for being 3-10mol/L with hydrogen ion concentration is 3 by liquid-solid ratio:1-8:1 circulating leaching gasification slag, cycle 5
More than secondary, the temperature of circulating leaching is 75-95 DEG C, and the time leached every time is 60-180min, and it is dense to add part in cyclic process
Degree obtains activation gasification slag and liquid phase for more than 300g/L hydrochloric acid, circulating leaching carries out under water bath condition；
(2) liquid phase and basic salt are subjected to polymerisation 60- under conditions of temperature is 75-95 DEG C and pH is 3-5
The liquid-solid ratio of 210min, liquid phase and basic salt is 6-15mL/g, wherein the addition part alkali into liquid phase is added every 0.5-1.5h
Property salt, alkaline salinity 2-4 times is added in liquid phase, cures 18-36h under conditions of 45-75 DEG C later, obtain aluminium polychloride；
(3) lye of a concentration of 1-5mol/L of hydroxide ion and activation are gasified into slag according to liquid-solid ratio 3:1-6:1
85-105 DEG C of progress desilication reaction, the desilication reaction time is 90-240min, is separated by solid-liquid separation later, obtains desiliconization liquid and solid phase；
(4) desiliconization liquid is concentrated by evaporation to the 60%-90% of original volume, obtains high mode soluble silicate；
Wherein, step (2) and step (3) are without sequencing.
The soluble silicate mould that the method for the present invention for preparing high mode soluble silicate using gasification slag obtains
For number in 1.5-2.5, quality is higher, can be widely applied to the fields such as coating, concrete, silica gel and waterproofing agent.
Numberical range of the present invention includes not only enumerated point value, further includes the above-mentioned numerical value not included
Arbitrary point value between range, as space is limited and for concise consideration, range includes described in the present invention no longer exclusive list
Specific point value.
Compared with prior art, beneficial effects of the present invention are：
The method provided by the invention for preparing high mode soluble silicate using gasification slag is taken off by acid activation with controllable
The substantially dissolution of silicon can be realized in the mutual cooperation of silicon under mild reaction conditions, can remove 60% (mass percentage)
Above silicon improves the modulus of soluble silicate in liquid phase, can obtain the high quality silicon hydrochlorate that modulus is 1.5-2.5 and produce
Product, while secondary solid and liquid pollutant are not generated, it realizes gasification slag minimizing and recycling efficiently utilizes, economy and ring
Border remarkable benefit.
The method provided by the invention for preparing high mode soluble silicate using gasification slag compared with the existing technology, is not necessarily to
Any silicon source is added, raw material sources are extensive, and reaction condition is mild, and operating flexibility is big, and process is simple, easy to operate, for Gao Mo
Number soluble silicates provide a kind of new technology and new raw material for the industry of raw material.
It is provided by the invention using gasification slag prepare high mode soluble silicate method can coproducing polymerized aluminium chloride,
Only it is the content that aluminium oxide in liquid phase can be improved by circulating leaching, aluminium ion concentration in liquid phase can be improved to 50-60g/L,
For simultaneous oxidation aluminium content (mass percentage) up to 7.5% or more, reaction condition is mild, without adding any silicon source, operates
Journey is simple, and operating flexibility is big, and acidleach post activation gasification slag impurity content is low, Fe2O3Content is reduced to 1% or so, CaO to contain by 9%
Amount is reduced to 1% or so, Na by 6%2O content is reduced to 0.5% or so by 3%, is prepared for silica-base material and building materialsization utilize
A kind of quality raw materials are provided, preparing industry for aluminium polychloride provides a kind of new technology and new raw material, alleviates China's fine aluminum
Native ore resources are exhausted.
Description of the drawings
Fig. 1 is the process flow chart that high-modulus sodium silicate is prepared using gasification slag that one embodiment of the present invention provides.
Specific implementation mode
Technical solution to further illustrate the present invention below with reference to the accompanying drawings and specific embodiments.
A kind of technique preparing high-modulus sodium silicate using gasification slag, as shown in Figure 1, the technique includes the following steps：
(1) gasification slag is leached with acid solution, after separation of solid and liquid, obtains activation gasification slag and liquid phase；
(2) activation gasification slag is carried out for the sodium hydroxide solution of 1-5mol/L at 85-105 DEG C with hydroxide ion concentration
Desilication reaction is separated by solid-liquid separation later, obtains desiliconization liquid and solid phase；
(3) desiliconization liquid is evaporated processing, obtains high-modulus sodium silicate.
Embodiment 1
A kind of technique being prepared sodium metasilicate using gasification slag, is included the following steps：
Process in leaching：Using gasification slag with industrial by-product hydrochloric acid according to liquid-solid ratio 8:1 carries out hybrid reaction, and wherein hydrochloric acid is dense
Degree is 3mol/L, and reaction temperature is 95 DEG C, reaction time 90min, rotating speed 350r/min；After reaction, by solid-liquid
Isolated activation gasification slag；
Desiliconization process：Above-mentioned activation gasification slag is reacted with diluted sodium hydroxide solution, wherein alkali concentration is 2mol/L, reaction
Temperature is 90 DEG C, reaction time 120min, liquid-solid ratio 5:1, rotating speed 350r/min；After reaction, by solid-liquid point
From obtaining sodium silicate rough product；
It is concentrated by evaporation：By above-mentioned sodium silicate rough product by being concentrated by evaporation to the 80% of original volume, water temperature to be evaporated reduces
When to 65 DEG C, it is delivered to Ore Leaching and diluted alkaline desiliconization workshop section；
It is 1.95 to obtain sodium metasilicate product modulus.
Embodiment 2
A kind of technique being prepared sodium metasilicate using gasification slag, is included the following steps：
Process in leaching：Using gasification slag with nitric acid according to liquid-solid ratio 7:1 carries out hybrid reaction, and wherein concentration of nitric acid is
4mol/L, reaction temperature are 90 DEG C, reaction time 120min, rotating speed 350r/min；After reaction, by being separated by solid-liquid separation
Obtain activation gasification slag；
Desiliconization process：Above-mentioned activation gasification slag is reacted with diluted sodium hydroxide solution, wherein alkali concentration is 3mol/L, reaction
Temperature is 95 DEG C, reaction time 150min, liquid-solid ratio 3:1, rotating speed 350r/min；After reaction, by solid-liquid point
From obtaining sodium silicate rough product；
It is concentrated by evaporation：By above-mentioned sodium silicate rough product by being concentrated by evaporation to the 90% of original volume, water temperature to be evaporated reduces
When to 55 DEG C, it is delivered to Ore Leaching and diluted alkaline desiliconization workshop section；
It is 2.17 to obtain sodium metasilicate product modulus.
Embodiment 3
A kind of technique being prepared sodium metasilicate using gasification slag, is included the following steps：
Process in leaching：Using gasification slag with industrial by-product hydrochloric acid according to liquid-solid ratio 4:1 carries out hybrid reaction, and wherein hydrochloric acid is dense
Degree is 9mol/L, and reaction temperature is 80 DEG C, reaction time 180min, rotating speed 350r/min；After reaction, by solid-liquid
Isolated activation gasification slag；
Desiliconization process：Above-mentioned activation gasification slag is reacted with diluted sodium hydroxide solution, wherein alkali concentration is 2mol/L, reaction
Temperature is 105 DEG C, reaction time 120min, liquid-solid ratio 5:1, rotating speed 350r/min；After reaction, by solid-liquid point
From obtaining sodium silicate rough product；
It is concentrated by evaporation：By above-mentioned sodium silicate rough product by being concentrated by evaporation to the 70% of original volume, water temperature to be evaporated reduces
When to 75 DEG C, it is delivered to Ore Leaching and diluted alkaline desiliconization workshop section；
It is 2.42 to obtain sodium metasilicate product modulus.
Embodiment 4
A kind of technique being prepared sodium metasilicate using gasification slag, is included the following steps：
Process in leaching：Using gasification slag with industrial by-product hydrochloric acid according to liquid-solid ratio 6:1 carries out hybrid reaction, and wherein hydrochloric acid is dense
Degree is 6mol/L, and reaction temperature is 95 DEG C, reaction time 60min, rotating speed 350r/min；After reaction, by solid-liquid
Isolated activation gasification slag；
Desiliconization process：Above-mentioned activation gasification slag is reacted with diluted sodium hydroxide solution, wherein alkali concentration is 4mol/L, reaction
Temperature is 85 DEG C, reaction time 180min, liquid-solid ratio 4:1, rotating speed 350r/min；After reaction, by solid-liquid point
From obtaining sodium silicate rough product；
It is concentrated by evaporation：By above-mentioned sodium silicate rough product by being concentrated by evaporation to the 85% of original volume, water temperature to be evaporated reduces
When to 65 DEG C, it is delivered to Ore Leaching and diluted alkaline desiliconization workshop section；
It is 1.94 to obtain sodium metasilicate product modulus.
Embodiment 5
A kind of technique being prepared sodium metasilicate using gasification slag, is included the following steps：
Process in leaching：Using gasification slag with sulfuric acid according to liquid-solid ratio 3:1 carries out hybrid reaction, and wherein sulfuric acid concentration is
5mol/L, reaction temperature are 75 DEG C, reaction time 180min, rotating speed 350r/min；After reaction, by being separated by solid-liquid separation
Obtain activation gasification slag；
Desiliconization process：Above-mentioned activation gasification slag is reacted with diluted sodium hydroxide solution, wherein alkali concentration is 3mol/L, reaction
Temperature is 85 DEG C, reaction time 90min, liquid-solid ratio 3:1, rotating speed 350r/min；After reaction, by being separated by solid-liquid separation
Obtain sodium silicate rough product；
It is concentrated by evaporation：By above-mentioned sodium silicate rough product by being concentrated by evaporation to the 90% of original volume, water temperature to be evaporated reduces
When to 55 DEG C, it is delivered to Ore Leaching and diluted alkaline desiliconization workshop section；
It is 1.58 to obtain sodium metasilicate product modulus.
Embodiment 6
A kind of technique being prepared sodium metasilicate using gasification slag, is included the following steps：
Process in leaching：Using gasification slag with industrial by-product hydrochloric acid according to liquid-solid ratio 5:1 carries out hybrid reaction, and wherein hydrochloric acid is dense
Degree is 5mol/L, and reaction temperature is 85 DEG C, reaction time 120min, rotating speed 350r/min；After reaction, by solid-liquid
Isolated activation gasification slag；
Desiliconization process：Above-mentioned activation gasification slag is reacted with diluted sodium hydroxide solution, wherein alkali concentration is 3mol/L, reaction
Temperature is 105 DEG C, reaction time 180min, liquid-solid ratio 4:1, rotating speed 350r/min；After reaction, by solid-liquid point
From obtaining sodium silicate rough product；
It is concentrated by evaporation：By above-mentioned sodium silicate rough product by being concentrated by evaporation to the 85% of original volume, water temperature to be evaporated reduces
When to 65 DEG C, it is delivered to Ore Leaching and diluted alkaline desiliconization workshop section；
It is 2.06 to obtain sodium metasilicate product modulus.
Embodiment 7
A kind of technique being prepared sodium metasilicate using gasification slag, is included the following steps：
Process in leaching：Using gasification slag with sulfuric acid according to liquid-solid ratio 4:1 carries out hybrid reaction, and wherein sulfuric acid concentration is
4mol/L, reaction temperature are 95 DEG C, reaction time 180min, rotating speed 350r/min；After reaction, by being separated by solid-liquid separation
Obtain activation gasification slag；
Desiliconization process：Above-mentioned activation gasification slag is reacted with diluted sodium hydroxide solution, wherein alkali concentration is 2mol/L, reaction
Temperature is 95 DEG C, reaction time 120min, liquid-solid ratio 3:1, rotating speed 350r/min；After reaction, by solid-liquid point
From obtaining sodium silicate rough product；
It is concentrated by evaporation：By above-mentioned sodium silicate rough product by being concentrated by evaporation to the 70% of original volume, water temperature to be evaporated reduces
When to 65 DEG C, it is delivered to Ore Leaching and diluted alkaline desiliconization workshop section；
It is 1.83 to obtain sodium metasilicate product modulus.
Embodiment 8
A kind of technique being prepared sodium metasilicate using gasification slag, is included the following steps：
Process in leaching：Using gasification slag with nitric acid according to liquid-solid ratio 7:1 carries out hybrid reaction, and wherein sulfuric acid concentration is
6mol/L, reaction temperature are 90 DEG C, reaction time 150min, rotating speed 350r/min；After reaction, by being separated by solid-liquid separation
Obtain activation gasification slag；
Desiliconization process：Above-mentioned activation gasification slag is reacted with diluted sodium hydroxide solution, wherein alkali concentration is 4mol/L, reaction
Temperature is 90 DEG C, reaction time 180min, liquid-solid ratio 4:1, rotating speed 350r/min；After reaction, by solid-liquid point
From obtaining sodium silicate rough product；
It is concentrated by evaporation：By above-mentioned sodium silicate rough product by being concentrated by evaporation to the 75% of original volume, water temperature to be evaporated reduces
When to 55 DEG C, it is delivered to Ore Leaching and diluted alkaline desiliconization workshop section；
It is 2.31 to obtain sodium metasilicate product modulus.
Embodiment 9
A kind of technique being prepared potassium silicate using gasification slag, is included the following steps：
Process in leaching：Using gasification slag with industrial by-product hydrochloric acid according to liquid-solid ratio 8:1 carries out hybrid reaction, and wherein hydrochloric acid is dense
Degree is 3mol/L, and reaction temperature is 95 DEG C, reaction time 90min, rotating speed 350r/min；After reaction, by solid-liquid
Isolated activation gasification slag；
Desiliconization process：Above-mentioned activation gasification slag is reacted with dilute potassium hydroxide solution, wherein alkali concentration is 1mol/L, reaction
Temperature is 100 DEG C, reaction time 240min, liquid-solid ratio 6:1, rotating speed 350r/min；After reaction, by solid-liquid point
From obtaining potassium silicate crude product；
It is concentrated by evaporation：By above-mentioned potassium silicate crude product by being concentrated by evaporation to the 60% of original volume, water temperature to be evaporated reduces
When to 85 DEG C, it is delivered to Ore Leaching and diluted alkaline desiliconization workshop section；
It is 1.78 to obtain potassium silicate product modulus.
Embodiment 10
A kind of technique being prepared sodium metasilicate using gasification slag, is included the following steps：
Process in leaching：Using gasification slag with sulfuric acid according to liquid-solid ratio 8:1 carries out hybrid reaction, and wherein concentration of hydrochloric acid is
10mol/L, reaction temperature are 95 DEG C, reaction time 90min, rotating speed 350r/min；After reaction, by being separated by solid-liquid separation
Obtain activation gasification slag；
Desiliconization process：Above-mentioned activation gasification slag is reacted with diluted sodium hydroxide solution, wherein alkali concentration is 5mol/L, reaction
Temperature is 90 DEG C, reaction time 180min, liquid-solid ratio 4:1, rotating speed 350r/min；After reaction, by solid-liquid point
From obtaining sodium silicate rough product；
It is concentrated by evaporation：By above-mentioned sodium silicate rough product by being concentrated by evaporation to the 70% of original volume, water temperature to be evaporated reduces
When to 60 DEG C, it is delivered to Ore Leaching and diluted alkaline desiliconization workshop section；
It is 2.15 to obtain sodium metasilicate product modulus.
Embodiment 11
It is a kind of to prepare the technique of sodium metasilicate using gasification slag, in addition to process in leaching is operations described below, remaining and 1 phase of embodiment
Together：
Using gasification slag with industrial by-product hydrochloric acid according to liquid-solid ratio 6:1 carries out hybrid reaction, and wherein concentration of hydrochloric acid is 200g/
L, reaction temperature are 95 DEG C, reaction time 180min, rotating speed 350r/min；After reaction, it is obtained by separation of solid and liquid
Filtrate；
Fresh process by-product hydrochloric acid (mass percentage 30%) is added into above-mentioned filtrate prepares required volume (leaching
When reach liquid-solid ratio 6:1) acidleach process as above, is carried out, process as above is repeated, after recycling 9 times, rich aluminum solutions and work is obtained by filtration
Change gasification slag, wherein alumina content (mass percentage) is up to 8.2% in rich aluminic acid liquid；
Industry Waste phosphorus slag (CaO mass percentages are added into the richness aluminum solutions>30%), divide 4 additions, interval is added
Time is 0.5h, carries out polymerization adjusting and controlling, and control pH is 95 DEG C in 3-5, liquid-solid ratio 6mL/g, polymerization temperature, and polymerization time is
210min, curing temperature is at 65 DEG C, curing time 36h.
Aluminium polychloride product alumina content (mass percentage) 8.4%, basicity 56% are obtained, density is
1.15g/cm3。
It is 2.08 to obtain sodium metasilicate product modulus.
Embodiment 12
It is a kind of to prepare the technique of sodium metasilicate using gasification slag, in addition to process in leaching is operations described below, remaining and 1 phase of embodiment
Together：
Using gasification slag with industrial by-product hydrochloric acid according to liquid-solid ratio 8:1 carries out hybrid reaction, and wherein concentration of hydrochloric acid is 220g/
L, reaction temperature are 85 DEG C, reaction time 120min, rotating speed 350r/min；After reaction, it is obtained by separation of solid and liquid
Filtrate；
Fresh process by-product hydrochloric acid (mass percentage 30%) is added into above-mentioned filtrate prepares required volume (leaching
When reach liquid-solid ratio 8:1) acidleach process as above, is carried out, process as above is repeated, after recycling 7 times, rich aluminum solutions and work is obtained by filtration
Change gasification slag, wherein alumina content (mass percentage) is up to 7.8% in rich aluminic acid liquid；
Industry Waste phosphorus slag (CaO mass percentages are added into the richness aluminum solutions>30%), divide 2 additions, interval is added
Time is 1.5h, carries out polymerization adjusting and controlling, and control pH is 85 DEG C in 3-5, liquid-solid ratio 10mL/g, polymerization temperature, and polymerization time is
180min, curing temperature is at 75 DEG C, curing time 30h.
Aluminium polychloride product alumina content (mass percentage) 8.2%, basicity 61% are obtained, density is
1.17g/cm3。
It is 1.84 to obtain sodium metasilicate product modulus.
Embodiment 13
It is a kind of to prepare the technique of sodium metasilicate using gasification slag, in addition to process in leaching is operations described below, remaining and 1 phase of embodiment
Together：
Using gasification slag with industrial by-product hydrochloric acid according to liquid-solid ratio 3:1 carries out hybrid reaction, and wherein concentration of hydrochloric acid is 220g/
L, reaction temperature are 75 DEG C, reaction time 60min, rotating speed 350r/min；After reaction, it is filtered by separation of solid and liquid
Liquid；
Fresh process by-product hydrochloric acid (mass percentage 30%) is added into above-mentioned filtrate prepares required volume (leaching
When reach liquid-solid ratio 3:1) acidleach process as above, is carried out, process as above is repeated, after recycling 7 times, rich aluminum solutions and work is obtained by filtration
Change gasification slag, wherein alumina content (mass percentage) is up to 7.6% in rich aluminic acid liquid；
Calcium oxide is added into the richness aluminum solutions, is added three times, addition interval time is 1h, carries out polymerization adjusting and controlling, control
PH is in 3-5, liquid-solid ratio 15mL/g, and polymerization temperature is 75 DEG C, polymerization time 60min, and curing temperature is at 45 DEG C, the curing time
18h。
Aluminium polychloride product alumina content (mass percentage) 8.0%, basicity 62% are obtained, density is
1.15g/cm3。
It obtains sodium metasilicate product to rub several being 1.95.
Comparative example 1
Except by the gasification slag in embodiment 1 replace in bauxite, kaolin or aluminous fly-ash any one or extremely
Outside few two kinds of combination, remaining is same as Example 1.
It is 0.46-0.63 to obtain sodium metasilicate product modulus.
Comparative example 2
Degasification slugging is directly carried out with diluted sodium hydroxide solution outside desilication reaction, remaining and embodiment 1 without Ore Leaching
It is identical.
It is 0.32 to obtain sodium metasilicate product modulus.
Comparative example 3
In addition to alkali concentration is 5.5mol/L in desiliconization process, remaining is same as Example 1.
It is 1.25 to obtain sodium metasilicate product modulus.
Comparative example 4
In addition to alkali concentration is 0.5mol/L in desiliconization process, remaining is same as Example 1.
It is 1.42 to obtain sodium metasilicate product modulus.
Comparative example 5
In addition to reaction temperature is 80 DEG C in desiliconization process, remaining is same as Example 1.
It is 1.04 to obtain sodium metasilicate product modulus.
Comparative example 6
In addition to reaction temperature is 110 DEG C in desiliconization process, remaining is same as Example 1.
It is 1.47 to obtain sodium metasilicate product modulus.
Applicant states, the foregoing is merely the specific implementation mode of the present invention, but protection scope of the present invention not office
It is limited to this, person of ordinary skill in the field is it will be clearly understood that any belong to those skilled in the art and taken off in the present invention
In the technical scope of dew, the change or replacement that can be readily occurred in are all fallen within protection scope of the present invention and the open scope.
Claims (10)
1. a kind of method preparing high mode soluble silicate using gasification slag, which is characterized in that the method includes as follows
Step：
(1) it with Ore Leaching gasification slag, is separated by solid-liquid separation, obtains activation gasification slag and liquid phase；
(2) lye of activation gasification slag and a concentration of 1-5mol/L of hydroxide ion is subjected to desilication reaction at 85-105 DEG C,
It is separated by solid-liquid separation later, obtains desiliconization liquid and solid phase；
(3) desiliconization liquid is post-processed, obtains high mode soluble silicate.
2. according to the method described in claim 1, it is characterized in that, step (1) acid is in hydrochloric acid, sulfuric acid or nitric acid
Any one or at least two combination；
Preferably, the hydrochloric acid is selected from industrial by-product hydrochloric acid and/or technical hydrochloric acid；
Preferably, the hydrogen ion concentration of step (1) acid is in 3-10mol/L；
Preferably, step (1) acid and the liquid-solid ratio of gasification slag are 3:1-8:1.
3. method according to claim 1 or 2, which is characterized in that the temperature of step (1) described leaching is 75-95 DEG C；
Preferably, the time of step (1) described leaching is 60-180min；
Preferably, step (1) leaching carries out under water bath condition.
4. according to the method described in one of claim 1-3, which is characterized in that step (1) is：Gasification slag is carried out using hydrochloric acid
Circulating leaching after separation of solid and liquid, obtains activation gasification slag and liquid phase；
Preferably, the number of the cycle is 5 times or more；
Preferably, part hydrochloric acid is added in the cyclic process of the circulating leaching；
Preferably, it adds a concentration of of hydrochloric acid and is more than 300g/L.
5. according to the method described in claim 4, it is characterized in that, the liquid phase carries out polymerisation with basic salt, curing obtains
To aluminium polychloride；
Preferably, the basic salt in calcium aluminate, calcium oxide or calcium base solid waste any one or at least two combination；
Preferably, the calcium base solid waste is selected from Industry Waste phosphorus slag and/or high calcium fluidization bed fly ash；
Preferably, the liquid phase and the liquid-solid ratio of basic salt are 6-15mL/g；
Preferably, in 2-4 addition liquid phase of the alkaline salinity；
Preferably, the addition partial alkaline salt into liquid phase is added every 0.5-1.5h；
Preferably, the temperature of the polymerisation is 75-95 DEG C；
Preferably, the time of the polymerisation is 60-210min；
Preferably, it is 3-5 that pH is controlled when the polymerisation；
Preferably, the temperature of the curing is 45-75 DEG C；
Preferably, the time of the curing is 18-36h.
6. according to the method described in one of claim 1-5, which is characterized in that step (1) is：It is 4- with hydrogen ion concentration
The hydrochloric acid of 10mol/L is 3 by liquid-solid ratio:1-8:1 circulating leaching gasification slag, recycle 5 times or more, the temperature of circulating leaching is 75-
95 DEG C, the time leached every time is 60-180min, and it is more than 300g/L hydrochloric acid, cycle leaching that moiety concentrations are added in cyclic process
Go out and carried out under water bath condition, obtains activation gasification slag and liquid phase；
Preferably, the liquid phase and basic salt are subjected to polymerisation 60-210min, liquid under conditions of temperature is 75-95 DEG C
It is mutually 6-15mL/g with the liquid-solid ratio of basic salt, wherein the addition partial alkaline salt into liquid phase, alkalinity is added every 0.5-1.5h
In 2-4 addition liquid phase of salinity, 18-36h is cured under conditions of 45-75 DEG C later, obtains aluminium polychloride.
7. according to the method described in one of claim 1-6, which is characterized in that it is molten that step (2) described lye is selected from sodium hydroxide
Liquid and/or potassium hydroxide solution.
8. according to the method described in one of claim 1-7, which is characterized in that the lye and the liquid-solid ratio for activating gasification slag are
3:1-6:1；
Preferably, the time of step (2) described desilication reaction is 90-240min.
9. according to the method described in one of claim 1-8, which is characterized in that step (3) it is described post-processing include：By desiliconization liquid
It is concentrated into the 60%-90% of original volume；
Preferably, the concentration is evaporation and concentration；
Preferably, it is used to prepare needed for step (1) and/or step (2) after the steam cooling generated in the evaporating concentration process
Acid and/or aqueous slkali；
Preferably, the temperature after cooling is 55-85 DEG C.
10. according to the method described in one of claim 1-9, which is characterized in that described method includes following steps：
(1) hydrochloric acid for being 3-10mol/L with hydrogen ion concentration is 3 by liquid-solid ratio:1-8:1 circulating leaching gasify slag, cycle 5 times with
On, the temperature of circulating leaching is 75-95 DEG C, and the time leached every time is 60-180min, and adding moiety concentrations in cyclic process is
More than 300g/L hydrochloric acid, circulating leaching carries out under water bath condition, obtains activation gasification slag and liquid phase；
(2) liquid phase and basic salt are subjected to polymerisation 60-210min, liquid under conditions of temperature is 75-95 DEG C and pH is 3-5
It is mutually 6-15mL/g with the liquid-solid ratio of basic salt, wherein the addition partial alkaline salt into liquid phase, alkalinity is added every 0.5-1.5h
In 2-4 addition liquid phase of salinity, 18-36h is cured under conditions of 45-75 DEG C later, obtains aluminium polychloride；
(3) lye of a concentration of 1-5mol/L of hydroxide ion and activation are gasified into slag according to liquid-solid ratio 3:1-6:1 in 85-
105 DEG C of progress desilication reactions, the desilication reaction time is 90-240min, is separated by solid-liquid separation later, obtains desiliconization liquid and solid phase；
(4) desiliconization liquid is concentrated by evaporation to the 60%-90% of original volume, obtains high mode soluble silicate；
Wherein, step (2) and step (3) are without sequencing.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110616320A (en) * | 2019-09-17 | 2019-12-27 | 北京科技大学 | Method for desiliconizing silicon-containing ore or slag |
| CN111060417A (en) * | 2019-11-25 | 2020-04-24 | 中国石油化工股份有限公司 | Quantitative analysis method for gasified slag mineral phase |
| CN112661162A (en) * | 2020-12-16 | 2021-04-16 | 青岛惠城环保科技股份有限公司 | Method for treating petroleum coke hydrogen production ash and mesoporous silicon material |
| CN113045341A (en) * | 2019-12-26 | 2021-06-29 | 国家能源投资集团有限责任公司 | Method for preparing alkali-free silicon fertilizer from silicon-containing acid treatment solution and alkali-free silicon fertilizer |
| CN114985435A (en) * | 2022-08-05 | 2022-09-02 | 中国科学院过程工程研究所 | Method for comprehensively utilizing waste salt and various solid wastes |
| CN115304090A (en) * | 2022-09-19 | 2022-11-08 | 西安科技大学 | Comprehensive utilization method of coal gasification fine slag |
| CN116078348A (en) * | 2021-11-08 | 2023-05-09 | 中国科学院过程工程研究所 | Comprehensive utilization method of gas slag |
| CN116102187A (en) * | 2021-11-09 | 2023-05-12 | 中国科学院过程工程研究所 | Method for detoxifying gasified slag activated acid liquor and comprehensively utilizing gasified slag activated acid liquor as resources |
| CN117339552A (en) * | 2023-11-21 | 2024-01-05 | 陕西科技大学 | Gas-based residue adsorption-flocculation multifunctional water purifying agent and preparation method and application thereof |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101456689A (en) * | 2009-01-08 | 2009-06-17 | 长安大学 | Comprehensive utilization method of coal water slurry gasified waste residue on Texaco gasifier |
| CN101913756A (en) * | 2010-07-21 | 2010-12-15 | 刘阳生 | Glass-state waste residue resource utilization method |
| CN103641177A (en) * | 2013-12-03 | 2014-03-19 | 新奥科技发展有限公司 | Method for extracting mineral substances in high-high-calcium slag |
| CN104495899A (en) * | 2014-11-30 | 2015-04-08 | 湖南科技大学 | Method for synergic resource utilization of acetylene sludge and coal ash |
| CN104773739A (en) * | 2015-01-14 | 2015-07-15 | 南阳东方应用化工研究所 | Fly ash decomposition method |
| US20160039715A1 (en) * | 2010-09-11 | 2016-02-11 | Alter Nrg Corp. | Carbonaceous bricks for use in carbon beds of gasification reactors and methods of making carbonaceous bricks |
| CN106892444A (en) * | 2015-12-21 | 2017-06-27 | 中国科学院过程工程研究所 | A kind of method of utilization waste hydrochloric acid and aluminium ash production polyaluminium chloride water purification agent |
| CN107021765A (en) * | 2017-05-25 | 2017-08-08 | 中国科学院过程工程研究所 | A kind of method that utilization aluminous fly-ash prepares the coproducing polymerized aluminium chloride of mullite |
-
2018
- 2018-05-04 CN CN201810421417.3A patent/CN108584971B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101456689A (en) * | 2009-01-08 | 2009-06-17 | 长安大学 | Comprehensive utilization method of coal water slurry gasified waste residue on Texaco gasifier |
| CN101913756A (en) * | 2010-07-21 | 2010-12-15 | 刘阳生 | Glass-state waste residue resource utilization method |
| US20160039715A1 (en) * | 2010-09-11 | 2016-02-11 | Alter Nrg Corp. | Carbonaceous bricks for use in carbon beds of gasification reactors and methods of making carbonaceous bricks |
| CN103641177A (en) * | 2013-12-03 | 2014-03-19 | 新奥科技发展有限公司 | Method for extracting mineral substances in high-high-calcium slag |
| CN104495899A (en) * | 2014-11-30 | 2015-04-08 | 湖南科技大学 | Method for synergic resource utilization of acetylene sludge and coal ash |
| CN104773739A (en) * | 2015-01-14 | 2015-07-15 | 南阳东方应用化工研究所 | Fly ash decomposition method |
| CN106892444A (en) * | 2015-12-21 | 2017-06-27 | 中国科学院过程工程研究所 | A kind of method of utilization waste hydrochloric acid and aluminium ash production polyaluminium chloride water purification agent |
| CN107021765A (en) * | 2017-05-25 | 2017-08-08 | 中国科学院过程工程研究所 | A kind of method that utilization aluminous fly-ash prepares the coproducing polymerized aluminium chloride of mullite |
Non-Patent Citations (3)
| Title |
|---|
| BIN LIN ET AL: "Preparation of high performance mullite ceramics from high-aluminum fly ash by an effective method", 《JOURNAL OF ALLOYS AND COMPOUNDS》 * |
| JIAN-BO ZHANG ET AL: "Acid activation for pre-desilicated high-alumina fly ash", 《FUEL PROCESSING TECHNOLOGY》 * |
| 商晓甫等: ""煤气化渣利用技术研究现状及应用趋势浅析"", 《中国环境科学学会学术年会论文集》 * |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110616320A (en) * | 2019-09-17 | 2019-12-27 | 北京科技大学 | Method for desiliconizing silicon-containing ore or slag |
| CN110616320B (en) * | 2019-09-17 | 2020-07-31 | 北京科技大学 | Method for desiliconizing silicon-containing ore or slag |
| CN111060417A (en) * | 2019-11-25 | 2020-04-24 | 中国石油化工股份有限公司 | Quantitative analysis method for gasified slag mineral phase |
| CN113045341A (en) * | 2019-12-26 | 2021-06-29 | 国家能源投资集团有限责任公司 | Method for preparing alkali-free silicon fertilizer from silicon-containing acid treatment solution and alkali-free silicon fertilizer |
| CN112661162A (en) * | 2020-12-16 | 2021-04-16 | 青岛惠城环保科技股份有限公司 | Method for treating petroleum coke hydrogen production ash and mesoporous silicon material |
| CN116078348A (en) * | 2021-11-08 | 2023-05-09 | 中国科学院过程工程研究所 | Comprehensive utilization method of gas slag |
| CN116102187A (en) * | 2021-11-09 | 2023-05-12 | 中国科学院过程工程研究所 | Method for detoxifying gasified slag activated acid liquor and comprehensively utilizing gasified slag activated acid liquor as resources |
| CN114985435A (en) * | 2022-08-05 | 2022-09-02 | 中国科学院过程工程研究所 | Method for comprehensively utilizing waste salt and various solid wastes |
| CN115304090A (en) * | 2022-09-19 | 2022-11-08 | 西安科技大学 | Comprehensive utilization method of coal gasification fine slag |
| CN117339552A (en) * | 2023-11-21 | 2024-01-05 | 陕西科技大学 | Gas-based residue adsorption-flocculation multifunctional water purifying agent and preparation method and application thereof |
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