CN102728210A - Device for forced oxidation treatment of magnesium-method fume desulfurization slag slurry - Google Patents
Device for forced oxidation treatment of magnesium-method fume desulfurization slag slurry Download PDFInfo
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- CN102728210A CN102728210A CN2012102401017A CN201210240101A CN102728210A CN 102728210 A CN102728210 A CN 102728210A CN 2012102401017 A CN2012102401017 A CN 2012102401017A CN 201210240101 A CN201210240101 A CN 201210240101A CN 102728210 A CN102728210 A CN 102728210A
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Abstract
The invention relates to a device for forced oxidation treatment of magnesium-method fume desulfurization slag slurry. The device comprises a reactor, an aeration distribution pipe, an aeration pipe, an air blower, a slag slurry rotational flow guide hood and a slag slurry pump, wherein the reactor is of a concentric double-cylinder structure comprising an inner cylinder and an outer cylinder; a slag discharge port is arranged at the bottom of the reactor; a slag slurry inlet and a slurry outlet are arranged at the side wall of the reactor; the aeration distribution pipe is arranged at the bottom of the reactor; the air blower is connected by the aeration pipe; and the slag slurry rotational flow guide hood is arranged above the inner cylinder so as to change the rotational flow function of the slurry liquid. Compared with the prior art, the device has the advantages of reasonable structural design, convenience in operation, capability of being beneficial for long-term and stable operation, and the like.
Description
Technical field
The present invention relates to a kind of device of field of environment protection, particularly magnesium method flue gas desulphurization slag slurry is carried out the device that forced oxidation is handled.
Background technology
China is maximum in the world coal production and use country, and the amount of sulfur dioxide that annual coal burning discharged is huge, serious harm human health and natural environment.Therefore, the Chinese government just progressively carries out strict coal-fired flue-gas discharge standard, carries out the flue gas desulfurization of station boiler, Industrial Boiler and kiln.
Fume desulphurization method is varied, generally is divided into the wet desulphurization technology, semi-dry desulphurization technology and desulfurization by dry method, and the wet desulphurization technology is because of its efficient height extensive use.Wherein the wet process of FGD technology mainly contains limestone-gypsum method, two alkaline process, magnesium oxide method and the desulfurization of ammonium method etc.At present, it is the flue gas desulfur device of main flow that each thermal power plant sets up with the limestone-gypsum method in succession, and acid rain problem is under control to a certain extent.But because the limestone-based process desulfur technology has relatively high expectations to the automatization level of system, and complex process, thereby there is big difficulty when on less Industrial Boiler of scale and kiln, using.Comparatively speaking, the desulfurization of magnesium method have desulphurizing activated height, technological process simple, take up an area of characteristics such as little, investment and energy consumption are little, less scaling, obtaining application more and more widely aspect the Industrial Boiler smoke gas treatment in recent years.
Yet this method existing questions has at present: 1) the direct product of general magnesium method desulfurization is a magnesium sulfite, because the solubility of magnesium sulfite is higher, causes the inferior sulfate radical in the doctor solution to be difficult to the efficient oxidation; 2) many magnesium method desulphurization plants are not generally set up the oxidizing tower still in the desulfurizing tower bottom, need set up the forced oxidation unit in addition; 3) owing to lack the desulfurizing byproduct recovery technology; Many simple and easy magnesium method sulfur removal technologies are directly with waste water that desulfurization produced and contain the magnesium sulfite waste residue and directly abandon; Not only can cause the waste of magnesium resource, inferior sulfate radical discharges not up to standard in waste water or the waste residue but also can cause.Therefore, no matter be reclaiming type or disposal type in the magnesium method sulfur removal technology, magnesium sulfite is carried out the oxidation link that is absolutely necessary.
Retrieval through to the prior art document is found: number of patent application: CN201110193051.7; Publication number: CN102350197A; Put down in writing " based on magnesian flue gas desulfurization and denitrification apparatus and method ", the technical characterictic of this invention is to remove SO in the bottom of desulphurization denitration tower with the magnesia slurry
2, in circulating absorption solution, add metallic catalyst, and blast air, make desulfurization product MgSO
3Be oxidized to MgSO fast
4This method has the advantages that technology is simple, investment is low, but only through blasting air slurries is fully stirred, and the catalyst cost is also high.
Number of patent application: CN200820135962.8, publication number: CN201280436 has put down in writing " a kind of aeration agitation agitated reactor for preparing magnesium sulfate "; The aerator of this device is arranged on agitated reactor body middle part, adopts micro-pore aeration, and agitating device is arranged on the top of aerator; Its favourable aspect is; Micro-pore aeration has increased the oxygen content in the slurries, and agitator avoids magnesium sulfite directly to precipitate, and reacts fully and carries out.But stirring and aeration all need to start during owing to this agitated reactor operation, and energy consumption is higher.
Say with a smile " experimental study that improves magnesium method flue gas desulphurization accessory substance oxidation rate " (environmental project together; 2011; 29 increase: 409-411) through lucite post lab scale and amplification test, carried out experimental study to influencing the factor that the oxidation of magnesium method desulfurization product magnesium sulfite prepares in the magnesium sulfate process.The compound of processing with metal sulfate is a catalyst, at ambient temperature, can effectively improve the oxidation efficiency of this process.But total oxidation efficient still remains to be improved.
Summary of the invention
The object of the invention is exactly for the defective that overcomes above-mentioned prior art existence a kind of reasonable in design to be provided, and is easy and simple to handle, is convenient to the forced oxidation treating apparatus of the magnesium method flue gas desulphurization slag slurry of operation steady in a long-term.
The object of the invention can be realized through following technical scheme: a kind of forced oxidation treating apparatus of magnesium method flue gas desulphurization slag slurry; It is characterized in that; This device comprises reactor, aeration distributor pipe, aeration tube, air blast, slag slurry eddy flow guide housing and slag stock pump, and described reactor is the concentric double-barrel structure of being made up of inner core and urceolus, and reactor bottom is provided with slag-drip opening, sidewall of reactor is provided with slag slurry inlet and slurries outlet; Described aeration distributor pipe is arranged on reactor bottom; Connect air blast through aeration tube, described slag slurry eddy flow guide housing is arranged on the inner core top, plays the cyclonic action that changes slurries.
Described aeration distributor pipe is arranged under the inner core, and aeration tube one end connects the aeration distributor pipe, and the other end passes inner core and connects air blast.
Described aeration distributor pipe is arranged on 50-200mm position, inner core below, is made up of a plurality of arms, opens solarization air cap on each arm, and opening diameter is 2-10mm.
Described aeration distributor pipe has 3-12 arm.
Described urceolus is a cylinder, and its bottom is provided with back taper, and described slag-drip opening is arranged on the band conical lower portion, and the span of described cylinder diameter D is at 300-3000mm; The urceolus height is 1-10D.
Described inner diameter of steel flue is 0.3-0.7 times of urceolus diameter, i.e. 0.3-0.7D.
The diameter of described slag slurry eddy flow guide housing is 1.0-1.2 a times of inner diameter of steel flue, high 20-50cm, and the tangential flow guiding blade is housed.
The flow of described air blast per hour is 5-100 a times of forced oxidation treating apparatus dischargeable capacity, and blast is 20-80kPa.
Described slag slurry inlet is arranged on the one side sidewall of urceolus top; Described slurries outlet is arranged on the opposite side sidewall of urceolus below; Described slag slurry inlet also connects doctor solution; PH value through adding liquid in the doctor solution conditioned reaction device is 5-9, and described doctor solution is acid doctor solution, comprises sodium carbonate or sodium acid carbonate.
The liquid solid content is 3-30% in the described reactor, and the desulfurization slag that described forced oxidation treating apparatus is handled is 100-10000kg/ (m
3D).
Pending slag slurry is squeezed into reactor through the slag stock pump from upside, under the effect of aeration distributor pipe and slag slurry eddy flow guide housing, discharges from opposite side through the slurries after the acid doctor solution oxidation.Urceolus is a cylinder, and the bottom is back taper, is provided with slag-drip opening, can regularly remove the desulfurizing byproduct impurity of sedimentation through the mode of gravitational settling, and the aeration distributor pipe is arranged on the bottom of reactor, is connected with air blast through aeration tube.Slag slurry eddy flow guide housing is positioned at the inner core top, plays the effect of the flow direction that changes slurries.
Compared with prior art, technological merit of the present invention is, uses concentric double-barrel structure; When air blast blasts air-flow bottom it; Because the gas shock effect can make the interior liquid of reactor by the inner core fast rise, and carry a large amount of thin bubbles secretly; At the top liquid again through urceolus to dirty and get back to reactor bottom, form liquid high efficiency circulating in reactor like this.In addition, because the effect of tangential flow guiding blade, liquid also has turning effort in the cyclic process, guarantees abundant mixing and contact between air-flow, liquid and the particulate matter, makes the residual magnesia that exists with bulk form in the slag slurry be able to fully dissolving and pulp.Because dissolved oxygen is very high in the circulating fluid, can make the magnesium sulfite efficient oxidation in the desulfurization slag slurry is magnesium sulfate, and the COD that reduces in the desulfurization slag consumes thing, and gives security for the recovery of magnesium sulfate.After acquiring a certain degree when circulation, the solid constituent in the desulfurization slag slurry then is mainly the magnesium hydroxide of coal ash and a small amount of pulpous state, because the two granular size and density variation are bigger; In this case, if stop aeration, the coal ash that particle and density are all bigger then sinks to the oxidizing tower bottom fast; Magnesium hydroxide then sedimentation is slower, and major part is suspended in the solution, utilizes this species diversity; Then can coal ash be discharged from the slag-drip opening of bottom,, then obtain innoxious desulfurization slag (coal ash) through simple Separation of Solid and Liquid; It directly is sent to the ash field, stacks sale with coal ash.
All apparatus structures are reasonable in design, and are easy and simple to handle, are convenient to operation steady in a long-term.It is high that this reactor has solved traditional aerator energy consumption, and oxidation efficiency is low, and problems such as removal of contamination difficulty are a kind of reactors that is suitable for magnesium method desulfurizing byproduct is oxidized to magnesium sulfate.
Description of drawings
Fig. 1 is the structural representation of apparatus of the present invention.
Among the figure: 1. slag-drip opening, 2. slurries outlet, 3. urceolus, 4. inner core, 5. slag slurry eddy flow guide housing, 6. air blast, 7. slag slurry inlet, 8. guide vane, 9. slag stock pump, 10. aeration distributor pipe.
The specific embodiment
Below in conjunction with accompanying drawing and specific embodiment the present invention is further specified.
As shown in Figure 1; The desuifurized forced oxidation treating apparatus of magnesium method, by 1. slag-drip openings, 2. slurries outlet, 3. urceolus, 4. inner core, 5. slag slurry eddy flow guide housing, 6. air blast, 7. the slag slurry inlet, 8. guide vane, 9. the slag stock pump, 10. aeration distributor pipe etc. is formed.Reactor is the concentric double-barrel structure of being made up of inner core 4 and urceolus 3; Reactor bottom is provided with slag-drip opening 1, sidewall of reactor is provided with slag slurry inlet 7 and slurries outlet 2; Described urceolus 3 is a cylinder; Its bottom is provided with back taper, and described slag-drip opening 1 is arranged on the band conical lower portion, and the span of described cylinder diameter D is at 300-3000mm; The urceolus height is 1-10D.The 0.3-0.7 that described inner core 4 diameters are urceolus diameters doubly, i.e. 0.3-0.7D.Described slag slurry inlet 7 is arranged on the one side sidewall of urceolus 3 tops; Described slurries outlet is established 2 and is put on opposite side sidewall below the urceolus; Described slag slurry inlet 7 also connects doctor solution A; PH value through adding liquid in the doctor solution A conditioned reaction device is 5-9, and described doctor solution is the acid doctor solution of pH＜6.5, comprises sodium carbonate or sodium acid carbonate.
Described aeration distributor pipe 10 is arranged on reactor bottom, is located under the inner core 4, connects air blast 6 through aeration tube; Aeration tube one end connects aeration distributor pipe 10; The other end passes inner core 4 and connects air blast 6, and aeration distributor pipe 10 is arranged on 50-200mm position, inner core 4 below, is made up of 3-12 arm; Open solarization air cap on each arm, opening diameter is 2-10mm.The flow of described air blast 6 per hour is 5-100 a times of forced oxidation treating apparatus dischargeable capacity, and blast is 20-80kPa.Described slag slurry eddy flow guide housing 5 is arranged on inner core 4 tops, plays the cyclonic action that changes slurries.The diameter of described slag slurry eddy flow guide housing is 1.0-1.2 a times of inner diameter of steel flue, high 20-50cm, and the tangential flow guiding blade is housed.
The liquid solid content is 3-30% in the described reactor, and the desulfurization slag that described forced oxidation treating apparatus is handled is 100-10000kg/ (m
3D).
Wherein: slag slurry is squeezed into reactor through slag stock pump 9 from upside, and the slurries after the oxidation are discharged from opposite side.Urceolus is a cylinder, and the bottom is back taper, is provided with slag-drip opening; Can regularly remove the desulfurizing byproduct impurity of sedimentation through the mode of gravitational settling, the aeration distributor pipe is arranged on the bottom of reactor, is connected with air blast through aeration tube; This aerator can drive slurries and stir, and does not need agitator, has saved energy consumption; Slag slurry eddy flow guide housing is positioned at the inner core top, plays the effect of the flow direction that changes slurries.
Present embodiment is realized oxidation through following flow process: the deslagging outlet valve is closed in (1)---and 1, the slurries outlet valve is closed in (2)---and 2, air blast is opened in (3)---and 6; (4) open the slag slurry inlet---7, add the desulfurizing byproduct slurries, oxidation is carried out in (5); (6) ph control---through adding doctor solution, (7) oxidation reaction is accomplished---densitometer control, discharging opening is opened in (8)--and 2; Carry out subsequent regeneration technology, (9) are opened and are removed cinder notch--and 1, removal of contamination.
This technical application compliance test result is specific as follows
Embodiment 1
The structure of forced oxidation tower is shown in accompanying drawing 1, and the urceolus diameter of oxidizing tower is 800mm, and inner diameter of steel flue is 400mm, highly is 2200mm.Through sodium pyrosulfite, magnesium sulfate and magnesia reaction make magnesium sulfite.In oxidation unit, add 700L water, (blow rate required is about 15m to open aerator
3/ h), get the magnesium sulfite slurries of 98kg preparation again and sneak into wherein, the beginning oxidation reaction.Through the inferior sulfate radical concentration that iodimetric titration was measured in the solution at a distance from one hour, reaction back 0h, 1h, 2h, 3h, the inferior sulfate radical concentration of 4h is respectively: 6.24g/l, 8.16g/l, 8.96g/l, 1.42g/l, 0.48g/l, pH is about 8.8.React the first two hour concentration height and be because magnesium sulfite just progressively dissolve, almost dissolving after second hour, inferior sulfate radical concentration decline afterwards very fast; Can explain that this oxidation unit oxidation effectiveness is better; In addition, if the pH value is higher, can directly utilize the lower doctor solution of pH value will be wherein with; The interior solution of oxidizing tower is moved under low pH value situation, help the dissolved oxygen of magnesium sulfite like this.
Adopt instance 1 described device; To the doctor solution that adds in the oxidation unit about 700L; PH is 5.5; Get the desulfurization slag 60kg that certain textile mills actual magnesium method sulfur removal technology produced and mix wherein, drop to below the 0.4g/l from initial 2.0g/l, explain that thus this device is fit to the oxidation processes that the practical sulphur removal slag is starched in the industry through the inferior sulfate radical concentration behind the 6h.
Claims (10)
1. the forced oxidation treating apparatus of magnesium method flue gas desulphurization slag slurry; It is characterized in that; This device comprises reactor, aeration distributor pipe, aeration tube, air blast, slag slurry eddy flow guide housing and slag stock pump, and described reactor is the concentric double-barrel structure of being made up of inner core and urceolus, and reactor bottom is provided with slag-drip opening, sidewall of reactor is provided with slag slurry inlet and slurries outlet; Described aeration distributor pipe is arranged on reactor bottom; Connect air blast through aeration tube, described slag slurry eddy flow guide housing is arranged on the inner core top, plays the cyclonic action that changes slurries.
2. the forced oxidation treating apparatus of a kind of magnesium method flue gas desulphurization slag slurry according to claim 1 is characterized in that described aeration distributor pipe is arranged under the inner core, and aeration tube one end connects the aeration distributor pipe, and the other end passes inner core and connects air blast.
3. the forced oxidation treating apparatus of a kind of magnesium method flue gas desulphurization slag slurry according to claim 1 and 2; It is characterized in that described aeration distributor pipe is arranged on 50-200mm position, inner core below, is made up of a plurality of arms; Open solarization air cap on each arm, opening diameter is 2-10mm.
4. the forced oxidation treating apparatus of a kind of magnesium method flue gas desulphurization slag slurry according to claim 3 is characterized in that described aeration distributor pipe has 3-12 arm.
5. the forced oxidation treating apparatus of a kind of magnesium method flue gas desulphurization slag slurry according to claim 1; It is characterized in that described urceolus is a cylinder, its bottom is provided with back taper; Described slag-drip opening is arranged on the band conical lower portion, and the span of described cylinder diameter D is at 300-3000mm; The urceolus height is 1-10D.
6. the forced oxidation treating apparatus of a kind of magnesium method flue gas desulphurization slag slurry according to claim 5 is characterized in that, described inner diameter of steel flue is 0.3-0.7 times of urceolus diameter, i.e. 0.3-0.7D.
7. the forced oxidation treating apparatus of a kind of magnesium method flue gas desulphurization slag slurry according to claim 6 is characterized in that, the diameter of described slag slurry eddy flow guide housing is 1.0-1.2 a times of inner diameter of steel flue, high 20-50cm, and the tangential flow guiding blade is housed.
8. the forced oxidation treating apparatus of a kind of magnesium method flue gas desulphurization slag slurry according to claim 1 is characterized in that, the flow of described air blast per hour is 5-100 a times of forced oxidation treating apparatus dischargeable capacity, and blast is 20-80kPa.
9. the forced oxidation treating apparatus of a kind of magnesium method flue gas desulphurization slag slurry according to claim 1; It is characterized in that described slag slurry inlet is arranged on the one side sidewall of urceolus top, described slurries outlet is arranged on the opposite side sidewall of urceolus below; Described slag slurry inlet also connects doctor solution; PH value through adding liquid in the doctor solution conditioned reaction device is 5-9, and described doctor solution is acid doctor solution, comprises sodium carbonate or sodium acid carbonate.
10. the forced oxidation treating apparatus of a kind of magnesium method flue gas desulphurization slag slurry according to claim 1 is characterized in that the liquid solid content is 3-30% in the described reactor, and the desulfurization slag that described forced oxidation treating apparatus is handled is 100-10000kg/ (m
3D).
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105084327A (en) * | 2014-05-20 | 2015-11-25 | 上海三卿环保科技有限公司 | Method for preparing high-purity double salt by crystallization of desulfurization and denitrification liquid |
| CN106745155A (en) * | 2016-11-29 | 2017-05-31 | 安徽工业大学 | A kind of flue gas desulfurization byproduct modification processing method |
| CN106757363A (en) * | 2016-11-29 | 2017-05-31 | 安徽工业大学 | A kind of method that utilization sintering flue gas desulfurization accessory substance prepares calcium sulfate crystal whiskers |
| CN107569983A (en) * | 2017-08-08 | 2018-01-12 | 武汉和尔环保科技有限公司 | Smoke-gas wet desulfurization equipment |
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| CN101037271A (en) * | 2007-04-28 | 2007-09-19 | 阮文权 | Biological desulfurizing device for transforming sulfur-containing compound to elemental sulfur |
| CN201280436Y (en) * | 2008-09-27 | 2009-07-29 | 六合天融（北京）环保科技有限公司 | Aeration stirring reaction still for magnesium sulfate preparation |
| CN101804293A (en) * | 2010-04-06 | 2010-08-18 | 天津晓沃环保工程有限公司 | Flue gas desulfurization method of heating boiler and device thereof |
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2012
- 2012-07-11 CN CN201210240101.7A patent/CN102728210B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101037271A (en) * | 2007-04-28 | 2007-09-19 | 阮文权 | Biological desulfurizing device for transforming sulfur-containing compound to elemental sulfur |
| CN201280436Y (en) * | 2008-09-27 | 2009-07-29 | 六合天融（北京）环保科技有限公司 | Aeration stirring reaction still for magnesium sulfate preparation |
| CN101804293A (en) * | 2010-04-06 | 2010-08-18 | 天津晓沃环保工程有限公司 | Flue gas desulfurization method of heating boiler and device thereof |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105084327A (en) * | 2014-05-20 | 2015-11-25 | 上海三卿环保科技有限公司 | Method for preparing high-purity double salt by crystallization of desulfurization and denitrification liquid |
| CN106745155A (en) * | 2016-11-29 | 2017-05-31 | 安徽工业大学 | A kind of flue gas desulfurization byproduct modification processing method |
| CN106757363A (en) * | 2016-11-29 | 2017-05-31 | 安徽工业大学 | A kind of method that utilization sintering flue gas desulfurization accessory substance prepares calcium sulfate crystal whiskers |
| CN106757363B (en) * | 2016-11-29 | 2019-05-07 | 安徽工业大学 | A method of calcium sulfate crystal whiskers are prepared using sintering flue gas desulfurization by-product |
| CN107569983A (en) * | 2017-08-08 | 2018-01-12 | 武汉和尔环保科技有限公司 | Smoke-gas wet desulfurization equipment |
| CN107569983B (en) * | 2017-08-08 | 2020-04-03 | 武汉和尔环保科技有限公司 | Wet flue gas desulfurization equipment |
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