CN101397148B - Purification method of sintered flue gas desulfurization gypsum - Google Patents
Purification method of sintered flue gas desulfurization gypsum Download PDFInfo
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- CN101397148B CN101397148B CN2007100462975A CN200710046297A CN101397148B CN 101397148 B CN101397148 B CN 101397148B CN 2007100462975 A CN2007100462975 A CN 2007100462975A CN 200710046297 A CN200710046297 A CN 200710046297A CN 101397148 B CN101397148 B CN 101397148B
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Abstract
The invention discloses a method for purifying sintering flue gas desulfurized gypsum and is characterized in that the following steps are included: (1) the reverse flotation technology: one or the combination of no less than two of rough flotation, selectiveness flotation and deep flotation; (2) steady flow, the steady flow is carried out on the serious fluid after reverse flotation by adopting a steady flow device; (3) centrifugal dehydration, solid-liquid separation is carried out on the serious fluid after steady flow by adopting a centrifugal dehydration device. The method can overcome the shortcomings that the dehydration performance of the serious fluid of desulfurized gypsum is not good, the color of the by-product gypsum is deep and the content of impurities is high in the prior art, and the desulfurized gypsum with high quality and high whiteness is obtained, meanwhile, the scum containing iron obtained in the by-product can be returned to the sintering process for re-utilization. Moreover, the device of the process is compact and occupies small area, investment is small, and operation is steady.
Description
Technical field
The present invention relates to the purification technique of gypsum, be specifically related to sintered flue gas desulfurization gypsum is carried out the technology of purifying.
Background technology
In the power-plant flue gas wet desulfurizing process, the purifying of gypsum slurries and dehydration are generally finished in the gypsum dehydration system of desulfurization island.Conventional dewatering system is mainly by gypsum rotational flow station, waste-water vortex station, vacuum dehydration filter, gypsum slurries case, gypsum slurries excavationg pump and return duct control valve thereof, water ring vacuum pump, moisture trap, waste water recycling water tank, filter cloth washing water tank and flush water pump, filter cake flush box and flush water pump, and corresponding pipeline, valve, auxiliary device and control system are formed.Whole dewatering process equipment is many, occupation of land is big, complicated operation, and water consumption is big.Gypsum purifying and dehydration are generally: draw the gypsum slurries (concentration 10%～15%) from desulfurizing tower, concentrate through the one-level cyclone, supernatant enters the waste-water vortex station, bottom concentrated slurry (concentration 50%～55%) flow to the vacuum dehydration filter certainly and carries out second dehydration, and meanwhile, rinse-system carries out the flushing of gypsum, reduce the wherein impurity content of chlorion, flying dust etc., with the quality (CN1597069, CN1745881, CN1654400 etc.) of guaranteeing desulfurated plaster.
At U.S. Pat P 5,500,197 and USP 5,215, in 672, taked multi-stage water power cyclone technology and fine grained multi-stage separation technology to carry out the purification of gypsum slurries respectively, its principle, equipment constitute and technical characterstic still belongs to traditional " hydrocyclone+vacuum band-type filter machine " technology.
Because the complexity of mineral component and sintering process, sinter fume duty parameter (exhaust gas volumn, flue-gas temperature, dust concentration, smoke components etc.) fluctuation is very big, not only contains SO in the sinter fume
2, SO
3, NO
x, CO, CO
2, H
2O, O
2, complicated ingredients such as HF, HCl, also adhere to Fe in the flue dust
2O
3, SiO
2, Al
2O
3, the multiple ore deposit composition of joining such as C, and particle mostly is submicron order (dust less than 0.92 μ m often accounts for more than 95.0%).Therefore, the difficulty of governance of sinter fume is quite big, and domestic case history in this field still belongs to blank.
Because the dark (Fe of the particularity of sinter fume, the sintered flue gas desulfurization gypsum slurries color and luster of wet desulfurizing process institute by-product
2O
3Deng the content of material height), composition is more complicated, not only contains unconverted CaSO completely
3, residual CaCO
3, also carry under one's arms by the fines that are difficult to sedimentation, flying dust, organic carbon and the impurity such as soluble-salt formed by the sulfate or the chloride of sodium, potassium, magnesium.Therefore, directly apply mechanically the gypsum dehydration technology of conventional wet desulfurizing process, can bring following problem: 1. the gypsum color is dark, whiteness is low, influences the approach that utilizes of by-product gypsum; 2. the superfine soot dust granule in the slurries can stop up the vacuum belt machine filter cloth again and again, influences the direct motion of Separation of Solid and Liquid operation and the dewatering of gypsum; 3. impurity content is higher in the gypsum, the by-product gypsum grade is low.Therefore,, develop a kind of purifying process of sintered flue gas desulfurization gypsum in conjunction with the characteristics of steel enterprise sintering flue gas, necessary.
Summary of the invention
The purification process that the purpose of this invention is to provide a kind of sintered flue gas desulfurization gypsum, overcome the shortcoming that the gypsum slurries dewatering is not good in the prior art, the by-product gypsum color and luster is dark and impurity content is high, obtain the desulfurated plaster of high-grade, high whiteness, simultaneously, also by-product gained ferruginous dross can be returned sintering circuit utilizes again.
Inventive concept: this technology is used for reference the principle of floating separation, different qualities according to material composition in the sintered flue gas desulfurization gypsum slurries, interpolation by collecting agent, inhibitor, dispersant, pH value conditioning agent etc., in multistage floation tank, finish continuous reverse flotation process, impel that difference appears in each material surface physicochemical properties in the slurries, thereby make a kind of or one group of material selectively be attached to bubble in the slurries, float to liquid level thereupon, skim as scum silica frost, and make in the gypsum slurries the not CaSO of complete oxidation
3Oxidation once more takes place, and finally makes main body composition CaSO
42H
2O is enrichment and purification step by step, obtains the gypsum product that grade and color and luster meet the demands after centrifugal dehydration.
Technical scheme of the present invention is: a kind of purification process of sintered flue gas desulfurization gypsum may further comprise the steps:
A kind of purification process of sintered flue gas desulfurization gypsum is characterized in that may further comprise the steps:
(1) reverse flotation: roughly select earlier, process conditions are: the slurries pH value is 4～6, and collecting agent is a fatty acid, and inhibitor is an ammonium sulfate, and the PH conditioning agent is a sulfuric acid, and dispersant is a waterglass, and carrier is an agstone; Under the brute force of floation tank stirred, the ore particle in the slurries was cleaned mutually, and violent disturbance makes the siliceous carbon-containing impurities of iron content in the slurries and be difficult to the superfine soot dust granule of natural subsidence, at CaCO
3Remove through reverse flotation together under the effect of carrier;
(2) current stabilization, the slurries after adopting constant-current stabilizer to reverse flotation carry out current stabilization;
(3) centrifugal dehydration, the slurries after adopting centrifugal dehumidifier to current stabilization carry out Separation of Solid and Liquid.
Preferably, in the described step (1), carry out any one or two kinds selected or that choose deeply after roughly selecting again, selected process conditions are: the slurries pH value is 8～10, collecting agent is a kind of or several combinations of fatty amines such as lauryl amine and ether amine, inhibitor is starch or waterglass, and the PH conditioning agent is sodium carbonate or calcium hydroxide, does not add dispersant and carrier mass; The process conditions of dark choosing are: the slurries pH value is 5～6, and collecting agent is a petroleum sodium sulfonate, and inhibitor is a waterglass, and the PH conditioning agent is a sulfuric acid.
Preferably, in the described step (1), reverse flotation is the combination of air-dissolving air-float, dispersion air air supporting, electrofloatation and high one or more air-float technologies of effect shallow pool air-floatation.
Preferably, in the described step (1), roughly select that slurry temperature is 40～60 ℃ in the technology, the floation tank time of staying is 5～15min, and collecting agent is a kind of of tall oil, petroleum sodium sulfonate, oleic acid, oxidized paraffin wax soap and lauryl sodium sulfate etc. or several, and addition is 500～1000g/t, the inhibitor addition is 400～1000g/t, pH value conditioning agent addition is 100～500g/t, and the dispersant addition is 200～1000g/t, and the carrier addition is 100～500g/t.
Preferably, in the described step (1), slurry temperature is 30～50 ℃ in the dressing process, the floation tank time of staying is 20～30min, the collecting agent addition is 200～500g/t, and the inhibitor addition is 100～1000g/t, and pH value conditioning agent addition is 100～500g/t.Under the effect of cationic collecting agent, inhibitor and PH conditioning agent etc., the gypsum slurries composition is further selected, and along with the adjustment of pH value and the height disturbance of microbubble, impurity such as most of HCl, HF, heavy metal ion are removed in the slurries.After the scum silica frost that multistage reverse flotation process produces is skimmed, after drying, return sintering circuit and directly utilize.
Preferably, in the described step (1), slurry temperature is 30～50 ℃ in the technology of dark choosing, the floation tank time of staying is 10～30min, the collecting agent addition is 200～500g/t, the inhibitor addition is 100～400g/t, and pH value conditioning agent addition is 100～500g/t, and the forced oxidation air quantity is 2～5 times of conventional flotation design load.According to of the control requirement of later use approach to the gypsum quality, if necessary, then the gypsum slurries after selected being introduced degree of depth floation tank once more, is 5～6 at the slurries pH value, and slurry temperature is 30～50 ℃, the floation tank time of staying is 10～30min, collecting agent is a petroleum sodium sulfonate, and inhibitor is under the process conditions of waterglass, strengthens the forced oxidation air quantity, give full play to the disturbance and the oxidation of come-up micro-bubble, make CaSO residual in the slurries
3Further forced oxidation takes place, and generates CaSO
42H
2O.
Preferably, in the described step (3), with the supernatant that produces after the centrifugal dehydration as a supplement water return floating agent series with addition of the pond.
Preferably, in the described step (3), the slurries behind the current stabilization, when entering the inlet of centrifugal dehumidifier, the fluctuation range of its flow and concentration is no more than 10% of design load.
Preferably, in the described step (3), described centrifugal dehumidifier is a centrifuge.
Preferably, the rotating speed of described centrifuge is 2000r/min～4000r/min, by the frequency converter step-less adjustment, thereby obtains the different gypsum of adhesive water content.The shutdown of centrifuge is cleaned and is taked multifrequency time (2～6 times), the slow-speed of revolution (100r/min～500r/min) wash automatically, in case spline bloats existing obstruction or the fuselage shaking amplitude is excessive.
The present invention compared with prior art has following beneficial effect:
(1) utilizes reverse floatation process, realized that the removal of impurities of fine irony particle separates in the slurries, avoided the magnetic selection method shortcoming bad, improved the whiteness of gypsum the weak magnetic substance separating effect.
(2) a large amount of micro-bubbles in the floation tank can make in the desulphurization reaction the not CaSO of complete reaction
3Be oxidized to CaSO
42H
2O has improved grade of gypsum.
(3) performance SO
2The CaCO that absorption reaction is residual
3As the effect of carrier, the fines material of submicron order is swept along flotation, the fines that partly are difficult to natural subsidence can be with CaCO
3Flotation is removed together.
(4) scum silica frost that obtains of multistage floation tank, wherein main component is the oxide of Fe, Ca, Si, Al etc., can return sintering circuit and utilize again.
(5) supernatant that centrifugal dehydration process produces can return floating agent and utilize again with addition of the pond, has reduced the output of gypsum purifying process waste water.
(6) this process unit compactness, take up an area of little, investment is little, stable.
Description of drawings
The invention will be further described below with reference to drawings and Examples.
Fig. 1 is a sintered flue gas desulfurization gypsum purifying process schematic flow sheet.
The specific embodiment
Embodiment 1:
As shown in Figure 1, be 57000 Nm from a flue gas treating capacity
3In the desulfuration absorbing tower of the sintering flue gas desulfurization commerical test device of/h, draw concentration and be 20% sintered flue gas desulfurization gypsum slurries, carry out the gypsum slurries purification experiment of three grades of reverse flotations.
The service condition that one-level is roughly selected the reverse flotation pond is: the slurries pH value is 4.0, slurry temperature is 40 ℃, the floation tank time of staying is 5min, and collecting agent is that tall oil (500g/t), inhibitor are that ammonium sulfate (400g/t), PH conditioning agent are that sulfuric acid (250g/t), dispersant are that waterglass (200g/t), carrier are agstone (100g/t).
The service condition in the selected reverse flotation of secondary pond is: the slurries pH value is 8.0, and slurry temperature is 30 ℃, and the floation tank time of staying is 20min, and collecting agent is that lauryl amine (220g/t), inhibitor are that waterglass (100g/t), PH conditioning agent are sodium carbonate (100g/t).
The service condition of three grades of degree of depth floation tanks is: slurries pH value 5.0, slurry temperature is 32 ℃, the floation tank time of staying is 10min, collecting agent is that petroleum sodium sulfonate (200g/t), inhibitor are waterglass (120g/t), the PH conditioning agent is sulfuric acid (100g/t), and the forced oxidation air quantity is 2 times of conventional flotation design load.
Gypsum slurries after the flotation, by constant-current stabilizer (fluctuation range of slurry flow and concentration the design permissible value 10% in).
Pump into the centrifugal dehydration system and carry out Separation of Solid and Liquid, obtain gypsum by-product, wherein the rotating speed of centrifuge is 2000r/min.The shutdown of centrifuge is cleaned and taked to clean automatically repeatedly, wash for 2 times rotating speed is 100r/min.
For the purpose of contrast, the original gypsum samples of handling without flotation is slurries solid particle natural subsidence, dry the back obtains.The composition contrast of two kinds of gypsum is as shown in table 1.
The composition of gypsum contrast after original gypsum of table 1 and the flotation
| Analysis project | Original gypsum | Gypsum after the flotation |
| Free moisture content/(%) | 10.6 | 9.3 |
| Purity (CaSO 4·2H 2O)/(％) | 85.3 | 92.4 |
| Acid-base value (pH) | 5.8 | 6.2 |
| CaCO 3(％) | 1.88 | 0.82 |
| CaSO 3·1/2H 2O(％) | 0.25 | 0.085 |
| Whiteness | 45 | 82 |
| Average particle size particle size (more than the 32 μ m)/% | 90 | 99 |
| Al 2O 3/％ | 0.28 | ＜0.1 |
| Fe 2O 3/％ | 0.93 | 0.11 |
| SiO 2/％ | 1.5 | 0.52 |
| Cl -(mg/kg) | 900 | 50 |
| F -(mg/kg) | 320 | 42 |
| Mg(mg/kg) | 300 | 130 |
Embodiment 2:
As shown in Figure 1, be 90000m from a flue gas treating capacity
3In the desulfuration absorbing tower of the sintering flue gas desulfurization commerical test device of/h, draw concentration and be 12% sintered flue gas desulfurization gypsum slurries, carry out the gypsum slurries purification experiment of three grades of reverse flotations.
The service condition that one-level is roughly selected the reverse flotation pond is: the slurries pH value is 5.2, slurry temperature is 55 ℃, the floation tank time of staying is 15min, and collecting agent is that tall oil (1000g/t), inhibitor are that ammonium sulfate (500g/t), PH conditioning agent are that sulfuric acid (200g/t), dispersant are that waterglass (400g/t), carrier are agstone (100g/t).
The service condition in the selected reverse flotation of secondary pond is: the slurries pH value is 9.5, and slurry temperature is 45 ℃, and the floation tank time of staying is 25min, and collecting agent is that lauryl amine (300g/t), inhibitor are that waterglass (400g/t), PH conditioning agent are sodium carbonate (200g/t).
The service condition of three grades of degree of depth floation tanks is: slurries pH value 5.5, slurry temperature is 40 ℃, the floation tank time of staying is 10min, collecting agent is that petroleum sodium sulfonate (200g/t), inhibitor are waterglass (150g/t), the PH conditioning agent is sulfuric acid (300g/t), and the forced oxidation air quantity is 2 times of conventional flotation design load.
Gypsum slurries after the flotation, by constant-current stabilizer (fluctuation range of slurry flow and concentration the design permissible value 10% in).
Pump into the centrifugal dehydration system and carry out Separation of Solid and Liquid, obtain gypsum by-product, wherein the rotating speed of centrifuge is 3000r/min.The shutdown of centrifuge is cleaned and taked to clean automatically repeatedly, wash for 3 times rotating speed is 300r/min.
For the purpose of contrast, the original gypsum samples of handling without flotation is slurries solid particle natural subsidence, dry the back obtains.The composition contrast of two kinds of gypsum is as shown in table 2.
The composition of gypsum contrast after original gypsum of table 2 and the flotation
| Analysis project | Original gypsum | Gypsum after the flotation |
| Free moisture content/(%) | 8.6 | 7.3 |
| Purity (CaSO 4·2H 2O)/(％) | 85.3 | 96.4 |
| Acid-base value (pH) | 5.8 | 6.9 |
| CaCO 3(％) | 1.88 | 0.52 |
| CaSO 3·1/2H 2O(％) | 0.25 | 0.065 |
| Whiteness | 45 | 85 |
| Average particle size particle size (more than the 32 μ m)/% | 90 | 99 |
| Al 2O 3/％ | 0.28 | ＜0.1 |
| Fe 2O 3/％ | 0.93 | 0.12 |
| SiO 2/％ | 1.5 | 0.55 |
| Cl -(mg/kg) | 900 | 50 |
| F -(mg/kg) | 320 | 40 |
| Mg(mg/kg) | 300 | 80 |
Embodiment 3:
From a flue gas treating capacity is 60000m
3In the desulfuration absorbing tower of the sintering flue gas desulfurization commerical test device of/h, draw concentration and be 11% sintered flue gas desulfurization gypsum slurries, carry out the gypsum slurries purification experiment of three grades of reverse flotations.
The service condition that one-level is roughly selected the reverse flotation pond is: the slurries pH value is 6.0, slurry temperature is 60 ℃, the floation tank time of staying is 15min, and collecting agent is that oleic acid (1000g/t), inhibitor are that ammonium sulfate (1000g/t), PH conditioning agent are that sulfuric acid (500g/t), dispersant are that waterglass (900g/t), carrier are agstone (450g/t).
The service condition in the selected reverse flotation of secondary pond is: the slurries pH value is 10.0, and slurry temperature is 40 ℃, and the floation tank time of staying is 30min, and collecting agent is that lauryl amine (500g/t), inhibitor are that starch (350g/t), PH conditioning agent are calcium hydroxide (500g/t).
The service condition of three grades of degree of depth floation tanks is: slurries pH value 6.0, slurry temperature is 40 ℃, the floation tank time of staying is 30min, collecting agent is that petroleum sodium sulfonate (200g/t), inhibitor are waterglass (150g/t), the PH conditioning agent is sulfuric acid (300g/t), and the forced oxidation air quantity is 5 times of conventional flotation design load.
Gypsum slurries after the flotation, by constant-current stabilizer (fluctuation range of slurry flow and concentration the design permissible value 5% in).
Pump into the centrifugal dehydration system and carry out Separation of Solid and Liquid, obtain gypsum by-product, wherein the rotating speed of centrifuge is 4000r/min.The shutdown of centrifuge is cleaned and taked to clean automatically repeatedly, wash for 6 times rotating speed is 500r/min.
For the purpose of contrast, the original gypsum samples of handling without flotation is slurries solid particle natural subsidence, dry the back obtains.The composition contrast of two kinds of gypsum is as shown in table 3.
The composition of gypsum contrast after original gypsum of table 3 and the flotation
| Analysis project | Original gypsum | Gypsum after the flotation |
| Free moisture content/(%) | 8.6 | 3.5 |
| Purity (CaSO 4·2H 2O)/(％) | 85.3 | 93.8 |
| Acid-base value (pH) | 5.8 | 6.4 |
| CaCO 3(％) | 1.88 | 0.55 |
| CaSO 3·1/2H 2O(％) | 0.25 | 0.025 |
| Whiteness | 45 | 89 |
| Average particle size particle size (more than the 32 μ m)/% | 90 | 98 |
| Al 2O 3/％ | 0.28 | ＜0.1 |
| Fe 2O 3/％ | 0.93 | 0.10 |
| SiO 2/％ | 1.5 | 0.35 |
| Cl -(mg/kg) | 900 | 40 |
| F -(mg/kg) | 320 | 20 |
| Mg(mg/kg) | 300 | 60 |
Embodiment 4:
From a smoke treatment amount is 90000m
3In the desulfuration absorbing tower of the sintering flue gas desulfurization commerical test device of/h, draw concentration and be 15% sintered flue gas desulfurization gypsum slurries, carry out the gypsum purification experiment of two-stage reverse flotation.
The service condition that one-level is roughly selected the reverse flotation pond is: the slurries pH value is 5.4, slurry temperature is 58 ℃, the floation tank time of staying is 12min, and collecting agent is that petroleum sodium sulfonate (1000g/t), inhibitor are that ammonium sulfate (400g/t), PH conditioning agent are that sulfuric acid (100g/t), dispersant are that waterglass (500g/t), carrier are agstone (100g/t).
The service condition in the selected reverse flotation of secondary pond is: the slurries pH value is 9.0, and slurry temperature is 50 ℃, and the floation tank time of staying is 20min, and collecting agent is that lauryl amine (300g/t), inhibitor are that starch (250g/t), PH conditioning agent are sodium carbonate (200g/t).
According to actual needs, slurries are without degree of depth flotation.
Gypsum slurries after the flotation, by constant-current stabilizer (fluctuation range of slurry flow and concentration the design permissible value 8% in).
Pump into the centrifugal dehydration system and carry out Separation of Solid and Liquid, obtain gypsum by-product, wherein the rotating speed of centrifuge is 3400r/min.The shutdown of centrifuge is cleaned and taked to clean automatically repeatedly, wash for 2 times rotating speed is 500r/min.
For the purpose of contrast, the original gypsum samples of handling without flotation is slurries solid particle natural subsidence, dry the back obtains.The composition contrast of two kinds of gypsum is as shown in table 4.
The composition of gypsum contrast after original gypsum of table 4 and the flotation
| Analysis project | Original gypsum | Gypsum after the flotation |
| Free moisture content/(%) | 8.6 | 9.5 |
| Purity (CaSO 4·2H 2O)/(％) | 83.6 | 92.0 |
| Acid-base value (pH) | 6.0 | 8.1 |
| CaCO 3(％) | 1.48 | 0.35 |
| CaSO 3·1/2H 2O(％) | 0.35 | 0.04 |
| Whiteness | 40 | 85 |
| Average particle size particle size (more than the 32 μ m)/% | 91 | 99 |
| Al 2O 3/％ | 0.18 | ＜0.1 |
| Fe 2O 3/％ | 0.88 | 0.18 |
| SiO 2/％ | 1.60 | 0.65 |
| Cl -(mg/kg) | 1100 | 85 |
| F -(mg/kg) | 280 | 60 |
| Mg(mg/kg) | 360 | 80 |
Embodiment 5:
From a flue gas treating capacity is 57000Nm
3In the desulfuration absorbing tower of the sintering flue gas desulfurization commerical test device of/h, draw concentration and be 15% sintered flue gas desulfurization gypsum slurries, carry out the gypsum slurries purification experiment of two-stage reverse flotation.
The service condition that one-level is roughly selected the reverse flotation pond is: the slurries pH value is 6.0, slurry temperature is 55 ℃, the floation tank time of staying is 15min, and collecting agent is that oleic acid (800g/t), inhibitor are that ammonium sulfate (750g/t), PH conditioning agent are that sulfuric acid (300g/t), dispersant are that waterglass (700g/t), carrier are agstone (350g/t).
Selected without secondary, directly carry out degree of depth dissolved air floatation, the service condition of degree of depth floation tank is: slurries pH value 5.4, slurry temperature is 45 ℃, the floation tank time of staying is 30min, collecting agent is that petroleum sodium sulfonate (400g/t), inhibitor are waterglass (350g/t), and the PH conditioning agent is sulfuric acid (380g/t), and the forced oxidation air quantity is 3 times of conventional flotation design load.
Gypsum slurries after the flotation, by constant-current stabilizer (fluctuation range of slurry flow and concentration the design permissible value 10% in).
Pump into the centrifugal dehydration system and carry out Separation of Solid and Liquid, obtain gypsum by-product, wherein the rotating speed of centrifuge is 4000r/min.The shutdown of centrifuge is cleaned and taked to clean automatically repeatedly, wash for 6 times rotating speed is 500r/min.
For the purpose of contrast, the original gypsum samples of handling without flotation is slurries solid particle natural subsidence, dry the back obtains.The composition contrast of two kinds of gypsum is as shown in table 5.
The composition of gypsum contrast after original gypsum of table 5 and the flotation
| Analysis project | Original gypsum | Gypsum after the flotation |
| Free moisture content/(%) | 8.6 | 5.2 |
| Purity (CaSO 4·2H 2O)/(％) | 85.3 | 91.4 |
| Acid-base value (pH) | 5.8 | 6.2 |
| CaCO 3(％) | 1.88 | 1.05 |
| CaSO 3·1/2H 2O(％) | 0.25 | 0.045 |
| Whiteness | 45 | 85 |
| Average particle size particle size (more than the 32 μ m)/% | 90 | 97 |
| Al 2O 3/％ | 0.28 | ＜0.1 |
| Fe 2O 3/％ | 0.93 | 0.10 |
| SiO 2/％ | 1.5 | 0.32 |
| Cl -(mg/kg) | 900 | 45 |
| F -(mg/kg) | 320 | 25 |
| Mg(mg/kg) | 300 | 50 |
Claims (10)
1. the purification process of a sintered flue gas desulfurization gypsum is characterized in that may further comprise the steps:
(1) reverse flotation: roughly select earlier, process conditions are: slurry pH value is 4～6, and collecting agent is a fatty acid, and inhibitor is an ammonium sulfate, and the pH conditioning agent is a sulfuric acid, and dispersant is a waterglass, and carrier is an agstone;
(2) current stabilization, the slurries after adopting constant-current stabilizer to reverse flotation carry out current stabilization;
(3) centrifugal dehydration, the slurries after adopting centrifugal dehumidifier to current stabilization carry out Separation of Solid and Liquid.
2. the purification process of sintered flue gas desulfurization gypsum as claimed in claim 1, it is characterized in that, in the described step (1), carry out any one or two kinds selected or that choose deeply after roughly selecting again, selected process conditions are: slurry pH value is 8～10, and collecting agent is one or both combinations of fatty amine and ether amine, and inhibitor is starch or waterglass, the pH conditioning agent is sodium carbonate or calcium hydroxide, does not add dispersant and carrier mass; The process conditions of dark choosing are: slurry pH value is 5～6, and collecting agent is a petroleum sodium sulfonate, and inhibitor is a waterglass, and the pH conditioning agent is a sulfuric acid.
3. the purification process of sintered flue gas desulfurization gypsum as claimed in claim 2 is characterized in that, in the described step (1), reverse flotation is the combination of air-dissolving air-float, dispersion air air supporting, electrofloatation and high one or more air-float technologies of effect shallow pool air-floatation.
4. the purification process of sintered flue gas desulfurization gypsum as claimed in claim 2, it is characterized in that, in the described step (1), roughly select that slurry temperature is 40～60 ℃ in the technology, the floation tank time of staying is 5～15min, collecting agent is an oleic acid, addition is 500～1000g/t, and the inhibitor addition is 400～1000g/t, and pH value conditioning agent addition is 100～500g/t, the dispersant addition is 200～1000g/t, and the carrier addition is 100～500g/t.
5. the purification process of sintered flue gas desulfurization gypsum as claimed in claim 4, it is characterized in that, in the described step (1), slurry temperature is 30～50 ℃ in the dressing process, the floation tank time of staying is 20～30min, the collecting agent addition is 200～500g/t, and the inhibitor addition is 100～1000g/t, and pH value conditioning agent addition is 100～500g/t.
6. the purification process of sintered flue gas desulfurization gypsum as claimed in claim 4, it is characterized in that, in the described step (1), slurry temperature is 30～50 ℃ in the technology of dark choosing, the floation tank time of staying is 10～30min, and the collecting agent addition is 200～500g/t, and the inhibitor addition is 100～400g/t, pH value conditioning agent addition is 100～500g/t, and the forced oxidation air quantity is 2～5 times of conventional flotation design load.
7. the purification process of sintered flue gas desulfurization gypsum as claimed in claim 1 is characterized in that, in the described step (3), with the supernatant that produces after the centrifugal dehydration as a supplement water return floating agent series with addition of the pond.
8. the purification process of sintered flue gas desulfurization gypsum as claimed in claim 1 is characterized in that, in the described step (3), and the slurries behind the current stabilization, when entering the inlet of centrifugal dehumidifier, the fluctuation range of its flow and concentration is no more than 10% of design load.
9. the purification process of sintered flue gas desulfurization gypsum as claimed in claim 1 is characterized in that, in the described step (3), described centrifugal dehumidifier is a centrifuge.
10. the purification process of sintered flue gas desulfurization gypsum as claimed in claim 9, it is characterized in that: the rotating speed of described centrifuge is 2000r/min～4000r/min, by the frequency converter step-less adjustment.
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| CN102319633A (en) * | 2011-10-09 | 2012-01-18 | 中蓝连海设计研究院 | A kind of method for floating of phosphogypsum slag |
| CN102500469A (en) * | 2011-10-20 | 2012-06-20 | 曲靖师范学院 | Phosphogypsum reverse flotation, desilication and impurity removal process |
| CN102616825B (en) * | 2012-04-17 | 2014-04-09 | 河南城建学院 | Purification process of desulfurization gypsum and gypsum raw materials purified through process |
| CN102631811B (en) * | 2012-04-18 | 2014-06-04 | 浙江天蓝环保技术股份有限公司 | Device and method for separating and removing impurities of carbide slag desulfurized gypsum slurry |
| CN103803627B (en) * | 2012-07-18 | 2015-07-08 | 浙江天蓝环保技术股份有限公司 | Separation and impurity removal method of white mud/calcium carbide residue-gypsum process based desulfurization gypsum slurry |
| CN103073044A (en) * | 2012-12-25 | 2013-05-01 | 河南民安新型材料有限公司 | Method for preparing desulfurized gypsum in flue gas desulfurization process simulated in laboratory |
| CN106186029B (en) * | 2016-07-11 | 2018-03-13 | 山东胜伟园林科技有限公司 | A kind of inorganic modified method of desulfurated plaster for alkaline land improving |
| CN106044827B (en) * | 2016-07-12 | 2018-11-27 | 山东胜伟盐碱地科技有限公司 | A kind of impurity-removing method of desulfurization gypsum in coal-fired power plant |
| CN106179771B (en) * | 2016-07-18 | 2019-03-05 | 攀钢集团攀枝花钢铁研究院有限公司 | The recoverying and utilizing method of calcium method tailings in vanadium extraction |
| CN106315652B (en) * | 2016-08-02 | 2017-09-29 | 中国环境科学研究院 | A kind of method of separating-purifying desulfurated plaster and the device for realizing this method |
| CN114247556B (en) * | 2021-12-23 | 2023-06-09 | 四川轻化工大学 | Phase-change purification method for industrial byproduct gypsum and phase-change purified gypsum |
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