CN101941783B - Method for washing carbon for removing sodium from silicon-removed alkaline residues of coal ash or basic red mud after process of extracting Al2O3 - Google Patents
Method for washing carbon for removing sodium from silicon-removed alkaline residues of coal ash or basic red mud after process of extracting Al2O3 Download PDFInfo
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Abstract
The invention discloses a method for washing carbon for removing sodium from silicon-removed alkaline residues of coal ash or basic red mud after a process of extracting Al2O3. The method is characterized by comprising the following step of: in a stirring and washing process, introducing desulfurated flue gas into a stirring and washing solution, wherein the washing temperature of the stirring and washing solution after introducing the desulfurated flue gas is 30-80 DEG C, the liquid/solid ratio L/S of the stirring and washing solution is 3-10, the introducing quantity of the flue gas is 0.5-2L/min, and the stirring and washing time is 1-3h. The method is simple and easy to apply, and the used stirring and washing solution can be used as a carbon source for cultivating spirulinas and a pH regulating agent; the silicon-removed alkaline residues after sodium removal can be used as a substrate for producing aluminum oxide by a lime sintering method; and the red mud after sodium removal is used as a substrate for producing silicate cement. The invention not only achieves the effects of waste gas emission reduction, waste liquid recycling and waste reduction, but also truly realizes a circulating economic model of the sustainable comprehensive recycling of three wastes (waste flue gas, sodium removal liquid and the red mud), and has obvious economic and social benefits.
Description
Technical field
The present invention removes the method for sodium in the alkaline residue for carbon divides washing; Relate to flyash and produce desiliconization ash alkaline residue behind the WHITE CARBON BLACK and take off sodium technology, and the alkaline red mud after the bauxite into alumina technology washs and takes off sodium with the alkaline red mud washing that this alkaline residue is produced behind the alumina technology with soda-lime or lime sinter process.The laterite washing that is used to produce the flyash desiliconization alkaline residue of aluminum oxide or produce the silicate cement mud base takes off sodium technology.
Background technology
Flyash is the solid waste that the coal-burning power plant discharges.At present, total volume of cargo in storage of China's flyash has surpassed 1,000,000,000 tons, but also increases with annual 1000 ten thousand tons speed.A large amount of soils are are not only occupied in the discharging of a large amount of flyash, and serious environment pollution, have constituted the dual destruction to ecological and environment.Al in the flyash that Jin Beidianchang dumps
20
3Content generally about 41%, Si0
2Content be about 48%, the content of calcium, iron, titanium, magnesium and other impurity is all lower, has the comprehensive development and utilization of becoming more meticulous again and is worth.
Now, the scientific and technical personnel of China's aluminium industry have attached great importance to the development research of the economic utilization technology of low alumina silica ratio bauxite resource.Though aluminous fly-ash is rich in Al
2O
3, but owing to contain SiO
2Amount is big, and alumina silica ratio is low, still can not be regarded as low alumina silica ratio bauxite resource.But if with the SiO in the flyash
2Extract a part or major part, be the bauxite resource utilization of extracting in the flyash and created condition.Put forward the level of the alumina silica ratio of the flyash behind the silicon near low alumina-silicon ratio alumyte, undoubtedly, this will become an approach that remedies China's bauxite resource shortage.The silicon that extracts in the flyash is prepared into the new technology of WHITE CARBON BLACK, becomes to extract Al
2O
3The prerequisite operation, but both low thick WHITE CARBON BLACK of output cost of this technology also can be produced the WHITE CARBON BLACK of high-grade different purposes, and the market adaptability is stronger.
Under normal pressure, utilize caustic alkali to be prone to and the amorphous silica reaction, ability rapidly obtain silicic acid; The aluminum oxide inertia of burning according to high temperature is big, and the characteristic that indissoluble goes out can realize preferably that silicon separates with aluminium.Meanwhile, a large amount of alkali has been incorporated into as producing Al
2O
3In the desiliconization alkaline residue of raw material; Thereby influence the production of follow-up aluminum oxide; Alkali has only the appropriateness of the high-alkali desiliconization slag of flyash is taken off sodium just might obtain being used to produce silicate cement after lime sinter process is carried aluminium low sodium red mud than the key factor that is lime sinter process stripping aluminium.
Flyash alkalescence red mud is the residue that produces in the soda-lime sintering process extracting aluminum oxide production process by the high-alkali desiliconization ash of flyash, and red mud is alkalescence, and red mud per ton attaches 3～4 m
3Alkali lye.Red mud waste by total utilization of PCA produces can take the wet method open pile to be stored in the environment; But take a large amount of land resourcess; Consume the place maintenance cost, and red mud high-alkali, high salinity adheres to liquid through seepage, can cause soil, water body and body of groundwater to pollute.Red mud the most effectively, big comprehensive utilization is the raw material as silicate cement, so require the sodium amount that contains of red mud must be less than 2%, otherwise faces the limited problem of utilization of red mud equally.The alkalescence of red mud has also restricted its recycling in other respects.Therefore, realize that cost-effectively red mud dealkalization is the red mud comprehensive utilization of resources, particularly be widely used in the silicate cement mud base and produce the preceding problem demanding prompt solution of cement.
At present, the dealkalize technology that both at home and abroad sintering process or Bayer process red mud the is adopted lime method of making a living more.Be the dealkalize agent with unslaked lime promptly, under hydrothermal condition with red mud in alkaline matter generation calcium sodium replacement(metathesis)reaction.The sodium salt that alkaline matter in the red mud is converted into different shape gets into solution, and unslaked lime then is converted into the insoluble calcium salt and gets into red mud.Unslaked lime method dealkalize technology exist service temperature high, generate the calcium salt pollutent, along with lime valency expansion process cost is rising always, less economical, be difficult to industrialization promotion and continue application.
Summary of the invention
The objective of the invention is to, a kind of flyash desiliconization alkaline residue is provided or extracts Al
2O
3The carbon of the alkaline red mud after the technology divides the washing method for removing Na, and this method can make the total content of dealkalize rear oxidation sodium be reduced to below 2%.Thereby make its become a kind of can be by a large amount of production aluminum oxide that utilize again or the raw material of silicate cement.
In order to realize above-mentioned task, the present invention takes following technical solution:
A kind of flyash desiliconization alkaline residue or extraction Al
2O
3The carbon of the alkaline red mud after the technology divides the washing method for removing Na, and this method comprises conventional washing and the agitator treating of leaving standstill, and it is characterized in that; In the agitator treating process; Stack gas in stirring washing lotion after the feeding desulfurization, the flue tolerance of the desulfurization of feeding is 0.5L/min～2L/min, stirs liquid-solid ratio L/S=3～10 of washing lotion; Wash temperature is 30～80 ℃, and the agitator treating time is 1～3h.
Stack gas after the described feeding desulfurization is divided to feed for three times to stir and is carried out circulation cleaning in the washing lotion.Specifically comprise the following steps:
Step 1 is that 1～1.5 normal temperature industry softening water of radix leaves standstill washing to flyash desiliconization alkaline residue or alkaline red mud butt on the adhesive tape filter, and wash-out adheres to alkali;
Step 2; With the desiliconization alkaline residue or the alkaline red mud that leave standstill after the washing; Send into the agitator treating reactor drum with liquid-solid ratio L/S=3～10 and carry out first time washing and take off sodium, in the agitator treating, the stack gas that feeds for the first time after the desulfurization is 0.5L/min～2L/min; Wash temperature is 30～80 ℃, and washing time is 0.3～1h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, liquids recovery;
Step 3, solid filter cake change the agitator treating reactor drum over to carries out second time washing and takes off sodium, and liquid-solid ratio keeps L/S=3～10, and in the agitator treating, the stack gas that feeds for the second time after the desulfurization is 0.5L/min～2L/min, and washing time is 0.3～1h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, and liquids recovery recycles;
Step 4, solid filter cake continue to change over to the agitator treating reactor drum washs for the third time and takes off sodium, and liquid-solid ratio keeps L/S=3～10; The stack gas air flow that feeds for the third time after the desulfurization is 0.5～2L/min, and washing time is 0.4～1h, after agitator treating finishes; Centrifugal; Solid-liquid separation gets solid filter cake and liquid, and liquids recovery recycles;
Step 5 is carried out pressure-filteration drying with solid filter cake, obtains the base-material of aluminum oxide or silicate cement.
Flyash desiliconization alkaline residue of the present invention or extraction Al
2O
3The carbon of the alkaline red mud after the technology divides the washing method for removing Na, and simple, washings can be recycled, and can reduce the water consumption of taking off the sodium washings greatly, the conserve water resource.Not only reach " reducing discharge of waste gases ", " waste liquid recycling " and " refuse decrement ", and really realize the three wastes (CO
2, take off sodium liquid and red mud) sustainable comprehensively the utilization again and recycling economy, show remarkable economic efficiency and social benefit.
Description of drawings
Fig. 1 is a schema of the present invention;
The present invention is described in further detail below in conjunction with embodiment that accompanying drawing and inventor provide.
Embodiment
The present invention is directed to the shortcoming of service temperature height in the unslaked lime method dealkalize technology, generation calcium salt pollutent, the CO that utilizes Industrial processes to produce
2Waste gas carries out red mud dealkalization, realizes two refuse (CO
2And red mud) sustainable comprehensively utilization again.
In the experimentation, the applicant studies temperature of reaction, time, the liquid-solid CO when that has investigated carborization in great detail
2Factors such as air flow are compared with traditional unslaked lime dealkalize technology the influence of red mud dealkalization usefulness, and method of the present invention has that service temperature is low, the dealkalize rate is high, gained alkali purity is high, does not have advantages such as new generation of waste materials and discharging.Make finally after the dealkalize that the total content of sodium oxide has been reduced to below 2% in the red mud.Thereby make its might become a kind of can be by the raw materials of a large amount of silicate industries of utilizing again.
Meanwhile take off to highly energy-consuming that sodium liquid multiple-effect evaporation concentrates, reuse technology; The present invention is used for biological culture with the sodium liquid that takes off of lower concentration; Carbon source and pH regulator agent as SPIRULINA CULTIVATION; To nutraceutical requirement, what lower concentration was adopted in the supply of the most important carbon source of growth of spirulina platensis, the present invention in spirulina medium takes off the contained sodium hydrogencarbonate (NaHCO of sodium liquid according to growth of spirulina platensis
3) as carbon source, its consumption is 4～16.8 grams per liters.Except as the carbon supplied, the sodium hydrogencarbonate that takes off in the sodium liquid of lower concentration also has the critical function of regulating nutrient solution pH, its CO
2, HCO
3 -, CO
3 2-In the frond process of growth, be absorbed and used.Because culturing process need not the commodity purchased sodium hydrogencarbonate, has reduced the aquaculture cost of tenaculat Habenaria.The real three wastes (the CO that realizes
2, take off sodium liquid and red mud) sustainable comprehensively the utilization again and recycling economy.
Flyash desiliconization alkaline residue of the present invention or extraction Al
2O
3The carbon of the alkaline red mud after the technology divides the washing method for removing Na; This method comprises conventional washing and the agitator treating of leaving standstill; In the agitator treating process; Stack gas in stirring washing lotion after the feeding desulfurization, the flue tolerance of the desulfurization of feeding is 0.5L/min～2L/min, stirs liquid-solid ratio L/S=3～10 of washing lotion; CO
2Air flow is 0.5～2L/min; The agitator treating time is 1～3h.
The present invention feeds the stack gas after the desulfurization in stirring washing lotion, its principle of taking off the sodium washing is:
The reaction that relates in the carborization dealkalize process mainly contains:
CO
2(g)→?CO
2(l) （1）
CO
2(l)?+?H
2O(l)→?H
2CO
3?→?HCO
3 -?+?H
+ （2）
Na
2O·Al
2O
3(s)?→?Na
2O·Al
2O
3(l)?→?2Na
+ （3）
Na
2SiO
3(s)?→?Na
2SiO
3(l)?→?2Na
+ （4）
Na
2CO
3(s)?→?Na
2CO
3(l)?→?2Na
+ （5）
Na
+?+?HCO
3 -?→?NaHCO
3 （6）
Formula (6) is that carborization carries out the final step that alkali removes or reclaims from flyash desiliconization alkaline residue or alkaline red muds such as aluminum-containing raw material such as flyash, bauxite, so in carbonization process, should generate HCO as much as possible
3 -And Na
+Its Chinese style (1) is CO
2Dissolution process, formula (2) is HCO
3 -Main source, formula (3), (4), (5) are Na
+Main generation step.Sial sodium salt elder generation and gas-to-liquid contact, bubble breaks strong gas-liquid phase physical-chemical reaction takes place then, and carbonic acid gas sial sodium salt combines, and sodium and oxygen silicon key has taken place again then, oxygen aluminium key dissociates, and the sodium salt disengaging solid phase of solubility enters in the middle of the liquid phase.Formula (6) is the ion rapid reaction, and its chemical reaction resistance can be ignored, and therefore, the key of whole alkali recovery process is at CO
2With the dissolving and the diffusion mass transfer of sodium salt in the flyash alkalescence red mud, i.e. CO
2The dissolving resistance to mass transfer of diffusional resistance and sodium salt through liquid film.And the controlled step of process depends on the size of two kinds of resistances, if the former is greater than the latter, then the controlled step of process is CO
2Diffusion mass transfer through liquid film; If the latter is greater than the former, then the controlled step of process is the dissolving mass transfer process of sodium salt.
In the early stage of carburizing reagent, the content of sodium salt is far above CO in the reactive agent
2Content, promptly the liquid-solid interface area is much larger than liquid-gas interface area, CO
2The liquid film diffusional resistance greater than the dissolving resistance of sodium salt.So carburizing reagent takes place in the liquid film at liquid-gas interface place.Seek out the conversion recovery of speed of reaction, increase alkali faster, increase CO
2Massfraction and take suitable stirring to reduce CO
2Resistance through liquid film is very necessary.In the mid-term of carburizing reagent, the Na in the liquid phase main body
+And CO
2Content all bigger, it is maximum that speed of reaction at this moment reaches.Along with CO
2Continuous feeding, its impellent through liquid film is also cumulative big, the reaction interface of carburizing reagent also is deep in the liquid phase main body by liquid film, the expansion of reaction interface has also promoted the quickening of carburizing reagent speed.In this process, because carburizing reagent is thermopositive reaction, system temperature can increase.In experimentation, the intensification meeting fast reaction speed in the certain limit, put forward the highly basic recovery, adopt to have to stir to be very important.
In the latter stage of carburizing reagent, because Na
+Content with the carrying out and constantly reduce of carburizing reagent, and CO
2Content but do not change, therefore, the liquid-solid interface area of reaction is less than the liquid-gas interface area.At this moment, the main resistance of reaction is by CO
2The dissolving resistance change the dissolving resistance of sodium salt gradually into.At CO
2The relatively large situation of diffusion impellent under, the liquid film of liquid-solid interface is transferred at the interface of carburizing reagent by the liquid phase main body.Because the content of the sodium salt in this liquid film is also less, so the speed of carburizing reagent constantly slows down.
On the adhesive tape filter; Adopt a step normal temperature to leave standstill washing, can a large amount of alkali cleanings of adhering to be taken off, then in the agitator treating process; The logical dioxide gas that adds in agitator treating liquid; Divide three washings, the washings that takes off after sodium washs can be recycled, and is about to last exhausted and takes off the sodium washings conduct washings first time next time for the second time; Centrifugal liquid-solid separation, liquid collecting is used for alkali and reclaims.
Solid filter cake changes the agitator treating reactor drum over to, can the washings for the third time that take off the sodium washing last time be become the washings second time next time, recycles; Solid filter cake continues to change over to the washing reaction device and takes off sodium for the third time, takes off sodium for the third time, takes off the industrial softening water preparation of sodium washings with Workshop Production.After wash-out finishes; Solid-liquid separation, washings are collected the washings that sodium is taken off in the washing second time that is used for next time, recycle; The solid filter cake that finally obtains is aluminum oxide or the base-material of silicate cement after the dealkalize, and wherein the total content of sodium oxide has been reduced to below 2%.Thereby make its become a kind of can be by the acceptable materials of a large amount of silicate industries of utilizing again.
Below be the embodiment that the contriver provides.
Embodiment 1:
Referring to Fig. 1; Present embodiment dissolves the residue that the silicon that extracts in the flyash is prepared into behind the WHITE CARBON BLACK to alkali and takes off sodium, comprises and leaves standstill washing and agitator treating, in agitator treating liquid, divides logical stack gas after adding desulfurization three times; Its air flow is 1.5L/min; Liquid-solid ratio L/S=8,40 ℃ of control wash temperatures, the agitator treating time is 1h.
Follow these steps to take off sodium successively:
(1) on the adhesive tape filter, carrying silicon alkaline residue butt with flyash is that the 1.2 normal temperature industry softening water of radix leaves standstill washing, and wash-out adheres to alkali.
(2) will leave standstill alkaline red mud after the washing sends into the agitator treating reactor drum with liquid-solid ratio L/S=8 and carries out agitator treating; In the agitator treating; Divide the stack gas that feeds three intermittences after the desulfurization; Stack gas after the desulfurization use phase reactor evenly break up and be scattered in solid-liquid mutually in, bubble breaks the triphasic physical-chemical reaction of strong gas, liquid, solid takes place then.
Feed the stack gas after the desulfurization first time, the air flow of the stack gas after the adjusting desulfurization is 1.5L/min, and wash temperature is 40 ℃, and washing time is 0.4h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, liquids recovery;
Solid filter cake changes the agitator treating reactor drum over to carry out second time washing and takes off sodium, and liquid-solid ratio remains unchanged, and in the agitator treating, the stack gas air flow that feeds for the second time after the desulfurization remains unchanged, and wash temperature is constant, and washing time is 0.4h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, and liquid collecting recycles after surveying sodium.
Solid filter cake continues to change over to the agitator treating reactor drum and washs for the third time and take off sodium, and liquid-solid ratio remains unchanged, and the stack gas air flow that feeds for the third time after the desulfurization remains unchanged; Wash temperature is constant, and washing time is 0.2h, after agitator treating finishes; Centrifugal, solid-liquid separation gets solid filter cake and liquid; Liquid collecting recycles after surveying sodium.
(3) solid filter cake carries out pressure-filteration drying, is the base-material that lime sinter process is produced aluminum oxide, and wherein the total content of sodium oxide has been reduced to below 2%.
Take off for the first time the sodium washings after alkali reclaims, can be used for the carbon source and the pH regulator agent of SPIRULINA CULTIVATION, its consumption is 4～16.8 grams per liters, meets its concentration range fully.
For the second time, for the third time washings can be used for taking off next time the sodium washing the first time washings and the second not good liquor cycles of washing use.
Embodiment 2:
Referring to Fig. 1, present embodiment extracts Al to flyash
2O
3Alkaline red mud takes off sodium after the technology, comprises leaving standstill washing and agitator treating, in agitator treating liquid, divides the stack gas of leading to after adding desulfurization for three times; 60 ℃ of control agitator treating temperature; Liquid-solid ratio L/S=3, the air flow of the stack gas after the desulfurization are 1L/min, and the agitator treating time is 2h.
Follow these steps to take off sodium successively:
(1) the 1 normal temperature industry softening water that on the adhesive tape filter, is radix with the alkaline red mud butt of flyash leaves standstill washing, and wash-out adheres to alkali.
(2) will leave standstill alkaline red mud after the washing sends into the agitator treating reactor drum with liquid-solid ratio L/S=5 and carries out agitator treating; In the agitator treating; Divide the stack gas that feeds three intermittences after the desulfurization; Stack gas after the desulfurization use phase reactor evenly break up and be scattered in solid-liquid mutually in, bubble breaks the triphasic physical-chemical reaction of strong gas, liquid, solid takes place then.
Feed the stack gas after the desulfurization first time, the stack gas air flow after the adjusting desulfurization is 1L/min, and wash temperature is 60 ℃, and washing time is 1h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, liquids recovery;
Solid filter cake changes the agitator treating reactor drum over to carry out second time washing and takes off sodium, and liquid-solid ratio remains unchanged, and in the agitator treating, the air flow that feeds the stack gas after the desulfurization for the second time remains unchanged, and wash temperature is constant, and washing time is 0.5h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, and liquid collecting recycles after surveying sodium.
Solid filter cake continues to change over to the agitator treating reactor drum and washs for the third time and take off sodium, and liquid-solid ratio remains unchanged, and the stack gas air flow that feeds for the third time after the desulfurization remains unchanged; Wash temperature is constant, and washing time is 0.5h, after agitator treating finishes; Centrifugal, solid-liquid separation gets solid filter cake and liquid; Liquid collecting recycles after surveying sodium.
(3) solid filter cake carries out pressure-filteration drying, is the base-material of producing silicate cement, and wherein the total content of sodium oxide has been reduced to below 2%.
Take off for the first time the sodium washings after alkali reclaims, can be used for the carbon source and the pH regulator agent of SPIRULINA CULTIVATION, its consumption is 4～16.8 grams per liters, meets its concentration range fully.
For the second time, for the third time washings can be used for taking off next time the sodium washing the first time washings and the second not good liquor cycles of washing use.
Embodiment 3:
Referring to Fig. 1, present embodiment extracts Al to flyash
2O
3Alkaline red mud takes off sodium after the technology, comprises leaving standstill washing and agitator treating, in agitator treating liquid, divides the stack gas of leading to after adding desulfurization for three times, and air flow is 0.5L/min, liquid-solid ratio L/S=3, and 50 ℃ of wash temperatures, the agitator treating time is 3h.
Follow these steps to take off sodium successively:
(1) the 1.5 normal temperature industry softening water that on the adhesive tape filter, is radix with the alkaline red mud butt of flyash leaves standstill washing, and wash-out adheres to alkali.
(2) will leave standstill alkaline red mud after the washing sends into the agitator treating reactor drum with liquid-solid ratio L/S=3 and carries out agitator treating; In the agitator treating; Divide the stack gas that feeds three intermittences after the desulfurization; Stack gas after the desulfurization use phase reactor evenly break up and be scattered in solid-liquid mutually in, bubble breaks the triphasic physical-chemical reaction of strong gas, liquid, solid takes place then.
Feed the stack gas after the desulfurization first time, and air flow is 0.5L/min, and wash temperature is 50 ℃, and washing time is 1h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, liquids recovery;
Solid filter cake changes the agitator treating reactor drum over to carry out second time washing and takes off sodium, and liquid-solid ratio remains unchanged, and in the agitator treating, the air flow that feeds the stack gas after the desulfurization for the second time remains unchanged, and wash temperature is constant, and washing time is 1h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, and liquid collecting recycles after surveying sodium.
Solid filter cake continues to change over to the agitator treating reactor drum and washs for the third time and take off sodium, and liquid-solid ratio remains unchanged, and the air flow that feeds the stack gas after the desulfurization for the third time remains unchanged; Wash temperature is constant, and washing time is 1h, after agitator treating finishes; Centrifugal, solid-liquid separation gets solid filter cake and liquid; Liquid collecting recycles after surveying sodium.
(3) solid filter cake carries out pressure-filteration drying, is the base-material of producing silicate cement, and wherein the total content of sodium oxide has been reduced to below 2%.
Take off for the first time the sodium washings after alkali reclaims, can be used for the carbon source and the pH regulator agent of SPIRULINA CULTIVATION, its consumption is 4～16.8 grams per liters, meets its concentration range fully.
For the second time, for the third time washings can be used for taking off next time the sodium washing the first time washings and the second not good liquor cycles of washing use.
Embodiment 4:
Referring to Fig. 1, present embodiment extracts Al to flyash
2O
3Alkaline red mud takes off sodium after the technology, comprises leaving standstill washing and agitator treating, in agitator treating liquid, divides the stack gas of leading to after adding desulfurization for three times, air flow position 1.5L/min, and liquid-solid ratio L/S=5,80 ℃ of control wash temperatures, the agitator treating time is 2h.
Follow these steps to take off sodium successively:
(1) the 1 normal temperature industry softening water that on the adhesive tape filter, is radix with the alkaline red mud butt of flyash leaves standstill washing, and wash-out adheres to alkali.
(2) will leave standstill alkaline red mud after the washing sends into the agitator treating reactor drum with liquid-solid ratio L/S=5 and carries out agitator treating; In the agitator treating; Can divide the stack gas after feed desulfurization three intermittences; Stack gas after the desulfurization use phase reactor evenly break up and be scattered in solid-liquid mutually in, bubble breaks the triphasic physical-chemical reaction of strong gas, liquid, solid takes place then.
Feed the stack gas after the desulfurization first time, the stack gas air flow after the adjusting desulfurization is 1.5L/min, and wash temperature is 80 ℃, and washing time is 0.5h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, liquids recovery;
Solid filter cake changes the agitator treating reactor drum over to carry out second time washing and takes off sodium, and in the agitator treating, the air flow that feeds the stack gas after the desulfurization for the second time remains unchanged, and liquid-solid ratio remains unchanged, and wash temperature is constant, and washing time is 0.5h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, and liquid collecting recycles after surveying sodium.
Solid filter cake continues to change over to the agitator treating reactor drum and washs for the third time and take off sodium, and liquid-solid ratio remains unchanged, and the air flow that feeds the stack gas after the desulfurization for the third time remains unchanged; Wash temperature is constant, and washing time is 1h, after agitator treating finishes; Centrifugal, solid-liquid separation gets solid filter cake and liquid; Liquid collecting recycles after surveying sodium.
(3) solid filter cake carries out pressure-filteration drying, is the base-material of producing silicate cement, and wherein the total content of sodium oxide has been reduced to below 2%.
Take off for the first time the sodium washings after alkali reclaims, can be used for the carbon source and the pH regulator agent of SPIRULINA CULTIVATION, its consumption is 4～16.8 grams per liters, meets its concentration range fully.
For the second time, for the third time washings can be used for taking off next time the sodium washing the first time washings and the second not good liquor cycles of washing use.
Embodiment 5:
Referring to Fig. 1, present embodiment extracts Al to bauxite
2O
3Alkaline red mud takes off sodium after the technology, comprises leaving standstill washing and agitator treating, in agitator treating liquid, divides the stack gas of leading to after adding desulfurization for three times, 30 ℃ of control wash temperatures, liquid-solid ratio L/S=10, CO
2Air flow 2L/min, the agitator treating time is 1h.
Follow these steps to take off sodium successively:
(1) the 1.5 normal temperature industry softening water that on the adhesive tape filter, is radix with the alkaline red mud butt of bauxite leaves standstill washing, and wash-out adheres to alkali.
(2) will leave standstill bauxite alkalescence red mud after the washing sends into the agitator treating reactor drum with liquid-solid ratio L/S=10 and carries out agitator treating; In the agitator treating; Divide the stack gas that feeds three intermittences after the desulfurization; Stack gas after the desulfurization use phase reactor evenly break up and be scattered in solid-liquid mutually in, bubble breaks the triphasic physical-chemical reaction of strong gas, liquid, solid takes place then.
Feed the stack gas after the desulfurization first time, and wash temperature is 30 ℃, and the stack gas air flow after the adjusting desulfurization is 2L/min, and washing time is 0.3h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, liquids recovery;
Solid filter cake changes the agitator treating reactor drum over to carry out second time washing and takes off sodium, and liquid-solid ratio remains unchanged, and in the agitator treating, the air flow that feeds the stack gas after the desulfurization for the second time remains unchanged, and wash temperature is constant, and washing time is 0.3h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, and liquid collecting recycles after surveying sodium.
Solid filter cake continues to change over to the agitator treating reactor drum and washs for the third time and take off sodium, and liquid-solid ratio remains unchanged, and the air flow that feeds the stack gas after the desulfurization for the third time remains unchanged; Wash temperature is constant, and washing time is 0.4h, after agitator treating finishes; Centrifugal, solid-liquid separation gets solid filter cake and liquid; Liquid collecting recycles after surveying sodium.
Solid filter cake carries out pressure-filteration drying, is the base-material of producing silicate cement, and wherein the total content of sodium oxide has been reduced to below 2%.
Take off for the first time the sodium washings after alkali reclaims, can be used for the carbon source and the pH regulator agent of SPIRULINA CULTIVATION, its consumption is 4～16.8 grams per liters, meets its concentration range fully.
For the second time, for the third time washings can be used for taking off next time the sodium washing the first time washings and the second not good liquor cycles of washing use.
Need to prove; Above contriver has provided some preferred embodiments; The invention is not restricted to the foregoing description, for example: flyash is produced red mud that red mud, soda-lime agglomerating red mud and the bauxite Bayer process of desiliconization alkaline residue behind the WHITE CARBON BLACK, lime sintering produce and also can be applicable to present method and carry out carbon and divide washing to take off sodium.Through detecting its sodium content and instance 2 indifferences, the total content of sodium has been reduced to below 2%.Therefore, in the scope that the present invention provides, all can with sodium content be removed to accords with production aluminum oxide or silicate cement the raw material alkali content require level.
Claims (2)
1. a flyash desiliconization alkaline residue or extract Al
2O
3The carbon of the alkaline red mud after the technology divides the washing method for removing Na, and this method comprises conventional washing and the agitator treating of leaving standstill, and it is characterized in that; In the agitator treating process; In stirring washing lotion, divide the stack gas after feeding desulfurization three times, the stack gas after the desulfurization use phase reactor evenly break up and be scattered in solid-liquid mutually in, bubble breaks the triphasic physical-chemical reaction of strong gas, liquid, solid takes place then; The flue tolerance of the desulfurization that feeds is 0.5L/min～2L/min; Stir liquid-solid ratio L/S=3～10 of washing lotion, wash temperature is 30～80 ℃, and the agitator treating time is 1～3h; Specifically comprise the following steps:
Step 1, the normal temperature industry softening water to flyash desiliconization alkaline residue or alkaline red mud butt radix 1～1.5 on adhesive tape filter or other continuous filter units leaves standstill washing, and wash-out adheres to alkali;
Step 2; With the desiliconization alkaline residue or the alkaline red mud that leave standstill after the washing; Send into the agitator treating reactor drum with liquid-solid ratio L/S=3～10 and carry out first time washing and take off sodium, in the agitator treating, the stack gas that feeds for the first time after the desulfurization is 0.5L/min～2L/min; Wash temperature is 30 ℃～80 ℃, and washing time is 0.3～1h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, liquids recovery;
Step 3, solid filter cake change the agitator treating reactor drum over to carries out second time washing and takes off sodium, and liquid-solid ratio keeps L/S=3～10, and in the agitator treating, the stack gas that feeds for the second time after the desulfurization is 0.5L/min～2L/min, and washing time is 0.3～1h; Centrifugal, liquid-solid separation gets solid filter cake and liquid, and liquids recovery recycles;
Step 4, solid filter cake continue to change over to the agitator treating reactor drum washs for the third time and takes off sodium, and liquid-solid ratio keeps L/S=3～10; The stack gas air flow that feeds for the third time after the desulfurization is 0.5～2L/min, and washing time is 0.4～1h, after agitator treating finishes; Centrifugal; Solid-liquid separation gets solid filter cake and liquid, and liquids recovery recycles;
Step 5 is carried out pressure-filteration drying with solid filter cake, obtains producing the base-material of aluminum oxide or silicate cement, and wherein the total content of sodium oxide has been reduced to below 2%.
2. flyash desiliconization alkaline residue as claimed in claim 1 or extraction Al
2O
3The carbon of the alkaline red mud after the technology divides the washing method for removing Na, it is characterized in that take off carbon source and pH regulator agent that the sodium washings is used for SPIRULINA CULTIVATION the described first time, its consumption is 4～16.8 grams per liters, meets its concentration range fully.
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| CN2010102814078A CN101941783B (en) | 2010-09-15 | 2010-09-15 | Method for washing carbon for removing sodium from silicon-removed alkaline residues of coal ash or basic red mud after process of extracting Al2O3 |
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| CN2010102814078A CN101941783B (en) | 2010-09-15 | 2010-09-15 | Method for washing carbon for removing sodium from silicon-removed alkaline residues of coal ash or basic red mud after process of extracting Al2O3 |
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| CN103143251B (en) * | 2013-01-08 | 2015-03-18 | 大唐国际发电股份有限公司高铝煤炭资源开发利用研发中心 | Purification method for industrial emission gas |
| CN104762120B (en) * | 2015-03-04 | 2017-03-01 | 新疆宜化化工有限公司 | A kind of high sodium coal method for removing sodium and equipment |
| CN105238488B (en) * | 2015-09-30 | 2018-08-21 | 华中科技大学 | A kind of dealkalization method of coal |
| CN105251607B (en) * | 2015-11-10 | 2017-09-26 | 河南理工大学 | A kind of red mud cross-flow dealkalization device |
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| CN1218831A (en) * | 1998-07-02 | 1999-06-09 | 中国科学院武汉植物研究所 | Regulating and controlling method for carbon source and PH value in cultivating spirulina |
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| CN1218831A (en) * | 1998-07-02 | 1999-06-09 | 中国科学院武汉植物研究所 | Regulating and controlling method for carbon source and PH value in cultivating spirulina |
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| Title |
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| 韦斌等."一种赤泥脱碱新工艺的初步研究".《中国科技论文在线》.2008,1-5. |
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