CN105329923B - Crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate - Google Patents
Crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate Download PDFInfo
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- CN105329923B CN105329923B CN201510787380.2A CN201510787380A CN105329923B CN 105329923 B CN105329923 B CN 105329923B CN 201510787380 A CN201510787380 A CN 201510787380A CN 105329923 B CN105329923 B CN 105329923B
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
- C01F5/40—Magnesium sulfates
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Abstract
The invention provides a crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate. We unceasingly test and actually apply the process, a cold crystallizing process performed through circulating cooling water of a compressed air cooling tower is ereached and developed according to the physical characteristic that magnesium sulfate can be separated out by crystallization at the temperature of 25 DEG C or lower, magnesium sulfate is crystallized at normal temperature by lowering the temperature of desulfurizing liquid to be 25 DEGC or lower, a good effect is achieved in actual application, and the defects that according to a three-effect evaporation and crystallization process, pipes can be blocked easily, energy consumption is large, and safety is not sufficient are overcome.
Description
Technical field
The present invention relates to a kind of processing technology of industrially desulfurized byproduct is and in particular to a kind of magnesium method flue gas desulphurization byproduct
Magnesium sulfate crystallization processes.
Background technology
Require with national environmental protection increasingly strict, will put forward higher requirement to steel industry pollution emission reduction, special
It is not that steel industry air contaminant treatment task during " 12 " is heavy and arduous, it is suitable that sulfur dioxide reduces discharging situation
Severe.
Flue gas desulfurization at present is most to adopt wet-type calcium desulfuration mode, and calcium method advantage is technology maturation, but shortcoming is also many:
By-product utilization value is low, demister easily blocks up, equipment is perishable and serious wear, liquid-gas ratio are big, cycling use of water amount is big, power consumption
High.
According to sintering flue gas fluctuation and smoke pollution composition feature, and international community's environmental pollution administers the change requiring
Change, in conjunction with China " 12 " during requirement to environmental protection, and international environmental protection development trend, according to domestic burning
So producing in knot flue gas desulfurization generation skill2, dioxin, particulate matter, nox, so3, the integrated treatment of the multiple pollutant such as hf, hcl,
We have selected wet-type magnesium method flue gas desulfurization technique.
Temperature after removal of impurities for the magnesium sulfate waste liquid after desulfurization is about 30 DEG C, and the content of magnesium sulfate is about 12%, waste liquid warp
Enter triple effect evaporator after the preheating of two-stage preheater to be evaporated concentrating, be concentrated into saturated solution, dtb is delivered to by discharging pump
Crystallizer；Saturated solution of magnesium sulfate decrease temperature crystalline in crystallizer forms epsom salt crystal, and crystallization solution is centrifuged
Afterwards, mother liquor Returning evaporimeter continues to be concentrated by evaporation, and the crystallization isolated is entered fluidized bed and is dried, and last epsom salt produces
Product are packed.Raw steam enters the shell side heat exchange condensation of an effect heating chamber after heat pump decompression, and condensed water enters triple effect evaporation
Device waste heat recycles；One effect separation chamber produce indirect steam part by heat pump aspirate, compression after return one effect heating chamber shell
Journey, remaining indirect steam enters 2nd effect evaporator heat exchange condensation, and condensed water enters triple effect evaporator and recycles；Are produced from two effect separation chambers
Raw indirect steam enters triple effect evaporator heat exchange condensation, and condensed water enters condensate water pot recycling；The two of end effect generation
Secondary steam enters indirect condenser and carries out condensation recovery.
The evaporation flow process of triple effect heat pump:
Relatively low, a part of high pressure of consumption, the height of the raw steam of the temperature of indirect steam produced by 1st effective evaporator, pressure ratio
Warm steam passes through heat pump and improves the pressure of part indirect steam, and its temperature also will accordingly improve, secondary after pressure by improving
Steam replaces raw steam as the thermal source of 1st effective evaporator, and remaining indirect steam is as the thermal source of lower 1st effective evaporator；Three
Effect vapo(u)rization system adds heat pump to save the consumption of steam to a great extent.
The temperature that magnesium sulfate waste liquid enters vapo(u)rization system is 30 DEG C, passes through exhaust steam using the indirect steam of triple effect evaporator pre-
Waste liquid is preheating to 50-60 DEG C by hot device, recycles the condensed water of 1st effective evaporator that waste liquid is preheated to 70-90 DEG C, improves useless
Liquid enters the temperature of 1st effective evaporator, reduces the area of 1st effective evaporator and indirect condenser, used heat is utilized.
Liquid between each effect evaporimeter be by effect between pressure differential conveyed, can decrease between each effect section of tubing and
The investment of conveying equipment and power consumption.
Evaporimeter all using forced circulation type evaporimeter, by the use of forced circulation pump as liquid between heating chamber and separation chamber
Form the motive force of circulation, control liquid in the rate of circulating flow in heating tube between 1.2-3.0m/s, it is to avoid liquid is in evaporimeter
Interior hot-spot or concentration is excessive causes fouling, scabs.
Due to containing certain impurity in magnesium sulfate waste liquid, in evaporation process, create a part of problem, for example: steam
Send out that device heat exchanger tube fouling, the system continuous cycle of operation be short, high energy consumption.When cooling water pressure is inadequate, easily cause vacuum degree deficiency；Steam
When vapour is unstable, it is also easy to produce foam.Equipment once breaks down, and maintenance cost is big, and because equipment component has air pressure,
Belong to pressure vessel, the potential safety hazard existing is big.
The byproduct magnesium sulfate producing in wet-type magnesium method desulfurization technique is mainly with crystallization mode output.We combine actual fortune
There are many problems with middle this crystallization processes of discovery, for overcoming the many shortcomings in triple effect evaporation crystallization processes, we newly research and develop
Go out a kind of water-cooled crystallization processes, overcome the shortcoming in triple effect evaporation crystallization processes, and saved operating cost.
Content of the invention
For solve the easy plugging of triple effect evaporation crystallization processes, energy consumption is big, security is not enough the shortcomings of, the present invention provide a kind of magnesium
Method flue gas desulfurization byproduct magnesium sulfate crystallization processes.
The present invention passes through continuous experiment practice through us, can the crystallization when temperature is less than 25 DEG C according to magnesium sulfate
The physical characteristic separating out.Develop a set of by pressure-air cooling tower recirculated cooling water cold crystallization technique, using magnesium sulfate
Solubility curve, to make magnesium sulfate crystallize by reducing desulfurization liquid temp at normal temperatures to less than 25 DEG C, and in actual motion
Achieve good effect.
The core of the present invention is: about 50 DEG C of magnesium sulfate slurry temperature out from desulfurizing tower 1, excavationg pump is input to plate
Frame filter press 2 filters, and filtrate water is delivered to retort 3 through filtrate water pump by the filtered fluid after filtration, passes through to add in retort 3
Plus a small amount of reactant 10, by Adlerika concentrate, after concentrate, the Adlerika close to saturation flows into crystallizing tank 5 and forms sulfuric acid
Magnesium magma.It is respectively provided with ring stainless steel condenser pipe 11 and agitator, condenser pipe uses in retort 3, crystallizing tank 5 and discharge tank 6
Recirculated cooling water in cooling tower 9, recirculated cooling water, after the rising of ring stainless steel condenser pipe temperature, is recycled to cooling again
Tower 9.Using compressed air refrigeration, recirculated water is lowered the temperature in cooling tower 9, cooling Posterior circle water passes through condenser pipe again to desulfurization
Liquid is cooled down, and by continuous circulating cooling, after making desulfurization liquid temp be down to 25 DEG C, is delivered to discharge tank 6.Fluid temperature reduces
To after 20 DEG C about, with discharging pump, magnesium sulfate magma is squeezed into centrifuge 7 and be dehydrated.Crystal after dehydration for the magnesium sulfate is from centrifuge
After 7 discharging opening blankings, packed with closer 8, the mother liquor that centrifuge 7 separates reenters mother liquor tank 4.Mother liquor pump will
Mother liquor returns in retort 3 and recycles.
Reactant 10 alleged by the present invention refers to the concentrated sulfuric acid and magnesia.
Two kinds of process operation Cost comparisons (being calculated with 126m3/h exhaust gas volumn)
Marginal data:
Fig. 1 is magnesium method flue gas desulphurization byproduct magnesium sulfate crystallization processes flow chart
In figure: 1- desulfurizing tower；2- plate and frame filter press；3- retort；4- mother liquor tank；5- crystallizing tank；6- discharge tank；7- is centrifuged
Machine；8- magnesium sulfate closer；9- circulating cooling tower；10- reactant；11- stainless steel condensate pipe.
Specific embodiment:
First, assembled by process chart, then run.I.e. magnesium sulfate slurries out from desulfurizing tower 1,
It is input to plate and frame filter press 2 by excavationg pump to filter, filtrate water is delivered to retort through filtrate water pump by the filtered fluid after filtration
3, pass through to add a small amount of reactant 10, by Adlerika concentrate, close to the Adlerika of saturation after concentrate in retort 3
Flow into crystallizing tank 5 and form magnesium sulfate magma.It is respectively provided with ring stainless steel condenser pipe 11 in retort 3, crystallizing tank 5 and discharge tank 6
And agitator.Condenser pipe uses the recirculated cooling water in cooling tower 9, and recirculated cooling water passes through in ring stainless steel condenser pipe temperature
After rising, again it is recycled to cooling tower 9.Using compressed air refrigeration, recirculated water is lowered the temperature in cooling tower 9, Posterior circle water of lowering the temperature
By condenser pipe, doctor solution is cooled down again, by continuous circulating cooling, after making desulfurization liquid temp be down to 25 DEG C, be delivered to out
Batch can 6.Same setting ring stainless steel condenser pipe and agitator in discharge tank 6, after fluid temperature is reduced to 20 DEG C about, with going out
Magnesium sulfate magma is squeezed into centrifuge 7 and is dehydrated by material pump.Crystal after dehydration for the magnesium sulfate, after centrifuge 7 discharging opening blanking, is used
Closer 8 is packed, and the mother liquor that centrifuge 7 separates reenters mother liquor tank 4.Mother liquor is returned to retort by mother liquor pump
Recycle in 3.
Claims (1)
1. magnesium method flue gas desulphurization byproduct magnesium sulfate crystallization processes it is characterised in that: from desulfurizing tower (1) out magnesium sulfate slurry
Liquid is input to plate and frame filter press (2) through excavationg pump and filters, and filtrate water is delivered to reaction through filtrate water pump by the filtered fluid after filtration
Tank (3), passes through to add a small amount of reactant (10), by Adlerika concentrate, close to the sulphur of saturation after concentrate in retort (3)
Sour magnesium solution flows into crystallizing tank (5) and forms magnesium sulfate magma, is respectively provided with ring in retort (3), crystallizing tank (5) and discharge tank (6)
Shape stainless steel condenser pipe (11) and agitator, condenser pipe uses recirculated cooling water, and recirculated cooling water is condensed by ring stainless steel
After pipe temperature rises, it is recycled to cooling tower (9), cooling tower is lowered the temperature to recirculated water using compressed air refrigeration in (9), cooling
Posterior circle water is cooled down to doctor solution by condenser pipe again, by continuous circulating cooling, after making desulfurization liquid temp be down to 25 DEG C,
It is delivered to discharge tank (6), same setting ring stainless steel condenser pipe and agitator in discharge tank (6), fluid temperature is reduced to 20
DEG C about after, with discharging pump by magnesium sulfate magma squeeze into centrifuge (7) dehydration, magnesium sulfate through dehydration after crystal from centrifuge
(7) after discharging opening blanking, packed with closer (8), the mother liquor that centrifuge (7) separates reenters mother liquor tank (4),
Mother liquor pump returns to mother liquor in retort (3) and recycles.
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| CN201510787380.2A CN105329923B (en) | 2015-11-17 | 2015-11-17 | Crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate |
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| CN201510787380.2A CN105329923B (en) | 2015-11-17 | 2015-11-17 | Crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate |
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| CN105329923B true CN105329923B (en) | 2017-01-25 |
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| CN108706613A (en) * | 2018-08-06 | 2018-10-26 | 山东大学 | A kind of system and method preparing magnesium sulfate using steam source cycle |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101423234A (en) * | 2008-11-27 | 2009-05-06 | 六合天融（北京）环保科技有限公司 | Process for preparing heptahydrate magnesium sulfate and liquid sulphur dioxide |
| CN102205201A (en) * | 2011-06-10 | 2011-10-05 | 赵玉斌 | Recovering process for desulphurized ammonium sulfate/magnesium sulfate |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN1056779C (en) * | 1996-08-08 | 2000-09-27 | 刘家栋 | Continuously self-cooling crystalizing technology |
| CN101549210B (en) * | 2008-04-03 | 2011-04-13 | 上海瑞惠机械设备制造有限公司 | Fume wet-type magnesia desulfated waste-liquid recovery method |
| CN101407325B (en) * | 2008-11-11 | 2010-06-16 | 大连市中山区鑫阳矿业化工研究所 | Method for separating boric acid and magnesium sulphate in boric acid production mother liquor by using magnesium sulphate |
| CN103382035B (en) * | 2013-08-01 | 2015-03-04 | 河北诺达化工设备有限公司 | Magnesium sulfate heptahydrate producing process with fully-continuous method |
| CN104058429A (en) * | 2014-07-04 | 2014-09-24 | 中节能六合天融环保科技有限公司 | Method for magnesium sulfate continuous crystallization |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101423234A (en) * | 2008-11-27 | 2009-05-06 | 六合天融（北京）环保科技有限公司 | Process for preparing heptahydrate magnesium sulfate and liquid sulphur dioxide |
| CN102205201A (en) * | 2011-06-10 | 2011-10-05 | 赵玉斌 | Recovering process for desulphurized ammonium sulfate/magnesium sulfate |
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