CN101549210A - Fume wet-type magnesia desulfated waste-liquid recovery method - Google Patents
Fume wet-type magnesia desulfated waste-liquid recovery method Download PDFInfo
- Publication number
- CN101549210A CN101549210A CNA2008100356716A CN200810035671A CN101549210A CN 101549210 A CN101549210 A CN 101549210A CN A2008100356716 A CNA2008100356716 A CN A2008100356716A CN 200810035671 A CN200810035671 A CN 200810035671A CN 101549210 A CN101549210 A CN 101549210A
- Authority
- CN
- China
- Prior art keywords
- magnesium sulfate
- adlerika
- desulfated
- waste
- liquid recovery
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
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- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims abstract description 40
- 238000011084 recovery Methods 0.000 title claims abstract description 30
- 239000000395 magnesium oxide Substances 0.000 title claims abstract description 27
- 239000007788 liquid Substances 0.000 title claims abstract description 24
- 239000003517 fume Substances 0.000 title claims abstract description 19
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims abstract description 70
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims abstract description 35
- 235000019341 magnesium sulphate Nutrition 0.000 claims abstract description 35
- 238000001704 evaporation Methods 0.000 claims abstract description 8
- 230000008020 evaporation Effects 0.000 claims abstract description 7
- 238000010438 heat treatment Methods 0.000 claims abstract description 5
- 239000013078 crystal Substances 0.000 claims abstract description 4
- 238000002425 crystallisation Methods 0.000 claims description 29
- 230000008025 crystallization Effects 0.000 claims description 20
- 230000000694 effects Effects 0.000 claims description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 12
- 239000003546 flue gas Substances 0.000 claims description 12
- 238000005245 sintering Methods 0.000 claims description 8
- 238000004064 recycling Methods 0.000 claims description 5
- 238000007701 flash-distillation Methods 0.000 claims description 4
- 238000007605 air drying Methods 0.000 claims description 3
- 238000005086 pumping Methods 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims description 3
- WRUGWIBCXHJTDG-UHFFFAOYSA-L magnesium sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Mg+2].[O-]S([O-])(=O)=O WRUGWIBCXHJTDG-UHFFFAOYSA-L 0.000 abstract description 3
- 229940061634 magnesium sulfate heptahydrate Drugs 0.000 abstract description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 abstract 3
- 229910052749 magnesium Inorganic materials 0.000 abstract 3
- 239000011777 magnesium Substances 0.000 abstract 3
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 10
- 238000006477 desulfuration reaction Methods 0.000 description 7
- 230000023556 desulfurization Effects 0.000 description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 235000011114 ammonium hydroxide Nutrition 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- HIVLDXAAFGCOFU-UHFFFAOYSA-N ammonium hydrosulfide Chemical compound [NH4+].[SH-] HIVLDXAAFGCOFU-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Treating Waste Gases (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
Abstract
The invention relates to the field of the fume wet-type magnesia desulfated waste-liquid recovery of boilers and sinter machines, and the like, in particular to a fume wet-type magnesia desulfated waste-liquid recovery method which adopts flash-evaporating concentration for processing a magnesium sulfate solution, the steps are as follows: the first-effect concentrating step of the magnesium solution, using positive-pressure operation and using fresh vapor as a heat resource, and concentrating the magnesium sulfate solution to 20 percent to 25 percent; the second-effect step of the magnesium sulfate solution, heating the solution by using secondary vapor generated in the first-effect evaporation until the concentration of the magnesium sulfate solution reaches 30 percent to 35 percent; the triple-effect concentrating step of the magnesium solution, heating by triple vapor generated in the second-effect concentrating step by adopting an atmosphere condenser and an evacuator so that the triple-effect concentrating step is operated in a vacuum state, and concentrating the magnesium sulfate solution to the set concentration to form a super-saturation solution in the thrice-effect concentrating step of the magnesium solution; the crystallizing step of magnesium sulfate: conveying the super-saturation solution to a crystallizer to enable the magnesium sulfate to form the crystal of magnesium sulfate heptahydrate to be continuously separated out; and the recovery step of the magnesium sulfate heptahydrate. The invention can generate hydrous magnesium sulfate and achieve high recovery rate.
Description
Technical field
The present invention relates to flue gas desulfurization, relate in particular to fields such as boiler, the recovery of sintering device flue gas wet-type magnesia desulfurization waste liquor.
Background technology
The sintering device flue gas that coal electricity industry flue gas, steel industry adopt has following characteristics:
Content of sulfur dioxide is low and unstable.
Smoke treatment mainly contains following two kinds of means at present:
(1) ammonia-process desulfurization technique
Utilize liquefied ammonia or ammoniacal liquor as absorbent, remove the sulfur dioxide in the sintering device flue gas, to reduce the discharge capacity of sulfur dioxide and dust, its byproduct is the sulphur ammonium fertilizer.
This method is and electronic beam method, the supporting use of impulse electric corona method, and these two kinds of methods are not only invested height, and because of equipment component does not pass a test, large-scale unit is used difficulty.
(2) atomizing flue gas cleaner
This sulfur dioxide flue gas is administered the technology desulfurization degree and (is being reached as high as 95%) more than 75%.The big multipaths of this method is longer, invests higherly, and absorptivity is not very desirable, because sulfur dioxide and lime reaction can generate one deck coating on the surface, the absorbent utilization rate is not high simultaneously; The secondary pollution in addition that has.
For this reason, people consider to adopt magnesia to carry out desulfurization, and what finally produce is Adlerika, but how effective recycling does not still have good scheme.
Summary of the invention
The present invention is intended to address the deficiencies of the prior art, and a kind of sintering device flue gas wet-type magnesia desulfated waste-liquid recovery method is provided.The present invention can generate Magnesium sulfate heptahydrate, and rate of recovery height is for enterprise provides new income increase point.
The present invention is achieved in that
A kind of fume wet-type magnesia desulfated waste-liquid recovery method, this method system adopts flash concentration to handle Adlerika, and this method comprises the following steps:
One of Adlerika is imitated concentration step,
This step adopts positive pressure operation, and its heater adopts live steam as thermal source, and Adlerika is concentrated into 20%-25%;
Two of Adlerika is imitated concentration step,
Utilize one to imitate the indirect steam heated solution that evaporation produces, thereby constantly evaporation removes redundant moisture in the Adlerika, reach concentration 30%～35% to Adlerika;
The triple effect concentration step of Adlerika,
Utilize barometric condenser and vaccum-pumping equipment, utilize two to imitate three Steam Heating that produce, triple effect is operated under vacuum state, thereby constantly flash vaporization removes redundant moisture in the Adlerika, reach normal concentration until Adlerika, become supersaturated solution;
The magnesium sulfate crystallisation step:
Described supersaturated solution is transported to crystallization apparatus, makes magnesium sulfate become the epsom salt crystal and constantly separate out; And,
The recycling step of epsom salt,
Rotary dryer is delivered in the epsom salt crystallization that crystallization is separated out, obtained the epsom salt finished product by heated-air drying, retracting device.
Described sintering device flue gas wet-type magnesia desulfated waste-liquid recovery method, described two heats of imitating concentration step are to be provided by the steam that an effect flash distillation step is produced.
Described fume wet-type magnesia desulfated waste-liquid recovery method, the heat of described triple effect concentration step are to be provided by the steam that two effect flash distillation steps are produced.
Described fume wet-type magnesia desulfated waste-liquid recovery method in the described magnesium sulfate crystallisation step, is to be that crystallization process provides the crystallization motive force in the mode that removes crystallization heat.
Described sintering device flue gas wet-type magnesia desulfated waste-liquid recovery method, in the described magnesium sulfate crystallisation step, described oversaturated Adlerika is delivered to crystallizer by pipeline.
Described fume wet-type magnesia desulfated waste-liquid recovery method, in the described magnesium sulfate crystallisation step, described certain concentration is 57.8%-58.3%.
Described fume wet-type magnesia desulfated waste-liquid recovery method, one of Adlerika is imitated in the concentration step, and temperature is: 120-135 ℃, pressure is: 0.4-0.8Mpa.
Described fume wet-type magnesia desulfated waste-liquid recovery method, two of Adlerika is imitated in the concentration step, and temperature is: 105-115 ℃, pressure is: pressure is: 0.4-0.8Mpa 0.2-0.4Mpa.
Described fume wet-type magnesia desulfated waste-liquid recovery method, in the triple effect concentration step of Adlerika, temperature is: 70-80 ℃, vacuum is: 0.8-0.9Mpa.
The present invention and prior art contrast tool desulfuration efficiency can be produced the magnesium sulfate of higher degree up to more than 98% in the time of desulfurization, rise a little for the user sets up a recycling economy; The magnesium sulfate rate of recovery (by the MgO that drops into) 〉=70%.The present invention is only imitated concentration step one and is adopted live steam, and two imitate, triple effect concentrates and all adopts steam that preceding step produces as thermal source, saved the energy greatly, simultaneously, the crystallization heat of crystallization process can also be as the additional heat energy of system, further reduce energy consumption, effectively reduced the magnesium sulfate cost recovery.
The specific embodiment
The present invention is achieved in that a kind of fume wet-type magnesia desulfated waste-liquid recovery method, and this method system adopts flash concentration to handle Adlerika, and this method comprises the following steps:
One of Adlerika is imitated concentration step,
This step adopts positive pressure operation, and pressure is: 0.4-0.8Mpa, its heater adopt live steam as thermal source; Being heated to temperature is: 120-135 ℃, Adlerika is concentrated into 20%-25%;
Two of Adlerika is imitated concentration step,
Utilize one to imitate the indirect steam heated solution that evaporation produces, for this step provides heat, temperature is: 105-115 ℃, pressure is: thus 0.2-0.4Mpa constantly evaporation remove redundant moisture in the Adlerika, reach concentration 30%～35% to Adlerika;
Utilize barometric condenser and vaccum-pumping equipment, utilize two to imitate three Steam Heating that produce, temperature is: 70-80 ℃, and triple effect is operated under vacuum state, vacuum is: 0.8-0.9Mpa; Thereby constantly flash vaporization removes redundant moisture in the Adlerika, and reaching concentration until Adlerika is 57.8%-58.3%, becomes supersaturated solution;
The magnesium sulfate crystallisation step:
Described supersaturated solution is delivered to crystallization apparatus by pipeline, is that crystallization process provides the crystallization motive force in the mode that removes crystallization heat, makes magnesium sulfate become the epsom salt crystal and constantly separates out; And,
The recycling step of epsom salt,
Fluidized bed dryer is delivered in the epsom salt crystallization that crystallization is separated out, obtained the epsom salt finished product by heated-air drying, retracting device.
Those of ordinary skill in the art should recognize that above-mentioned embodiment only is used to claim of the present invention is described, rather than limitation of the invention.Any substantive identical modification that content in the technical scheme of the present invention is done all will fall in the present invention's scope required for protection.
Claims (9)
1. fume wet-type magnesia desulfated waste-liquid recovery method, this method system adopts flash concentration to handle Adlerika, it is characterized in that this method comprises the following steps:
One of Adlerika is imitated concentration step,
This step adopts positive pressure operation, and its heater adopts live steam as thermal source, and Adlerika is concentrated into 20%-25%;
Two of Adlerika is imitated concentration step,
Utilize one to imitate the indirect steam heated solution that evaporation produces, thereby constantly evaporation removes redundant moisture in the Adlerika, reach concentration to Adlerika; 30%～35%;
The triple effect concentration step of Adlerika,
Utilize barometric condenser and vaccum-pumping equipment, utilize two to imitate three Steam Heating that produce, triple effect is operated under vacuum state, thereby constantly flash vaporization removes redundant moisture in the Adlerika, reach normal concentration until Adlerika, become supersaturated solution;
The magnesium sulfate crystallisation step:
Described supersaturated solution is transported to crystallization apparatus, makes magnesium sulfate become the epsom salt crystal and constantly separate out; And,
The recycling step of epsom salt,
Rotary dryer is delivered in the epsom salt crystallization that crystallization is separated out, obtained the epsom salt finished product by heated-air drying, retracting device.
2. sintering device flue gas wet-type magnesia desulfated waste-liquid recovery method according to claim 1 is characterized in that, described two heats of imitating concentration step are to be provided by the steam that an effect flash distillation step is produced.
3. fume wet-type magnesia desulfated waste-liquid recovery method according to claim 1 is characterized in that, the heat of described triple effect concentration step is to be provided by the steam that two effect flash distillation steps are produced.
4. fume wet-type magnesia desulfated waste-liquid recovery method according to claim 1 is characterized in that, in the described magnesium sulfate crystallisation step, is to be that crystallization process provides the crystallization motive force in the mode that removes crystallization heat.
5. sintering device flue gas wet-type magnesia desulfated waste-liquid recovery method according to claim 1 is characterized in that, in the described magnesium sulfate crystallisation step, described oversaturated Adlerika is delivered to crystallizer by pipeline.
6. fume wet-type magnesia desulfated waste-liquid recovery method according to claim 1 is characterized in that, in the described magnesium sulfate crystallisation step, described certain concentration is 57.8%-58.3%.
7. fume wet-type magnesia desulfated waste-liquid recovery method according to claim 1 is characterized in that, one of Adlerika is imitated in the concentration step, and temperature is: 120-135 ℃, pressure is: 0.4-0.8Mpa.
8. fume wet-type magnesia desulfated waste-liquid recovery method according to claim 1 is characterized in that, two of Adlerika is imitated in the concentration step, and temperature is: 105-115 ℃, pressure is 0.2-0.4Mpa.
9. fume wet-type magnesia desulfated waste-liquid recovery method according to claim 1 is characterized in that, in the triple effect concentration step of Adlerika, temperature is: 70-80 ℃, vacuum is: 0.8-0.9Mpa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100356716A CN101549210B (en) | 2008-04-03 | 2008-04-03 | Fume wet-type magnesia desulfated waste-liquid recovery method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100356716A CN101549210B (en) | 2008-04-03 | 2008-04-03 | Fume wet-type magnesia desulfated waste-liquid recovery method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101549210A true CN101549210A (en) | 2009-10-07 |
| CN101549210B CN101549210B (en) | 2011-04-13 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2008100356716A Active CN101549210B (en) | 2008-04-03 | 2008-04-03 | Fume wet-type magnesia desulfated waste-liquid recovery method |
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| CN (1) | CN101549210B (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102139180A (en) * | 2010-02-02 | 2011-08-03 | 天华化工机械及自动化研究设计院 | Refining catalyst spray drying tail gas/roasting tail gas purifying treatment method and equipment |
| CN102205201A (en) * | 2011-06-10 | 2011-10-05 | 赵玉斌 | Recovering process for desulphurized ammonium sulfate/magnesium sulfate |
| CN102806004A (en) * | 2011-05-30 | 2012-12-05 | 中国石油化工股份有限公司 | Recovery process of magnesium desulfurization by-products |
| CN105329923A (en) * | 2015-11-17 | 2016-02-17 | 朱冲 | Crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate |
| CN106745106A (en) * | 2016-12-21 | 2017-05-31 | 武汉工程大学 | A kind of method that nanometric magnesium hydroxide is prepared by phosphorus ore de-magging waste liquid |
| CN108889099A (en) * | 2018-08-06 | 2018-11-27 | 山东艾凯恩环保工程有限公司 | A kind of circulation magnesium processes desulfurization of steam source and magnesium sulfate preparation system and method |
| CN108910921A (en) * | 2018-08-06 | 2018-11-30 | 山东艾凯恩环保工程有限公司 | A kind of system and method preparing magnesium sulfate using flue gas heat-source Cycles |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3637226A1 (en) * | 1986-11-03 | 1988-05-19 | Kali & Salz Ag | METHOD FOR PRODUCING MAGNESIUM SULFAT |
| CN1225405C (en) * | 2003-11-14 | 2005-11-02 | 天津市昌昊化工股份合作公司 | Magnesium sulfate production method using magnesium oxide and desulfurated waste fluid |
-
2008
- 2008-04-03 CN CN2008100356716A patent/CN101549210B/en active Active
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102139180A (en) * | 2010-02-02 | 2011-08-03 | 天华化工机械及自动化研究设计院 | Refining catalyst spray drying tail gas/roasting tail gas purifying treatment method and equipment |
| CN102806004A (en) * | 2011-05-30 | 2012-12-05 | 中国石油化工股份有限公司 | Recovery process of magnesium desulfurization by-products |
| CN102205201A (en) * | 2011-06-10 | 2011-10-05 | 赵玉斌 | Recovering process for desulphurized ammonium sulfate/magnesium sulfate |
| CN102205201B (en) * | 2011-06-10 | 2012-11-21 | 赵玉斌 | Recovering process for desulphurized ammonium sulfate/magnesium sulfate |
| CN105329923A (en) * | 2015-11-17 | 2016-02-17 | 朱冲 | Crystallization process of magnesium method flue gas desulfurization by-product magnesium sulfate |
| CN106745106A (en) * | 2016-12-21 | 2017-05-31 | 武汉工程大学 | A kind of method that nanometric magnesium hydroxide is prepared by phosphorus ore de-magging waste liquid |
| CN106745106B (en) * | 2016-12-21 | 2018-07-17 | 武汉工程大学 | A method of nanometric magnesium hydroxide is prepared by phosphorus ore de-magging waste liquid |
| CN108889099A (en) * | 2018-08-06 | 2018-11-27 | 山东艾凯恩环保工程有限公司 | A kind of circulation magnesium processes desulfurization of steam source and magnesium sulfate preparation system and method |
| CN108910921A (en) * | 2018-08-06 | 2018-11-30 | 山东艾凯恩环保工程有限公司 | A kind of system and method preparing magnesium sulfate using flue gas heat-source Cycles |
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| Publication number | Publication date |
|---|---|
| CN101549210B (en) | 2011-04-13 |
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Owner name: HEBEI GUOHUI ENVIRONMENTAL TECHNOLOGY CO., LTD. Free format text: FORMER OWNER: SHANGHAI RUIHUI MACHINERY EQUIPMENT MANUFACTURING CO., LTD. Effective date: 20130122 |
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Free format text: CORRECT: ADDRESS; FROM: 201315 NANHUI, SHANGHAI TO: 052360 SHIJIAZHUANG, HEBEI PROVINCE |
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Effective date of registration: 20130122 Address after: Xinji City, Hebei province 052360, South Shijiazhuang City Economic Development Zone, Industrial Road on the west side of the road Patentee after: HEFEI GUOHUI ENVIRONMENTAL PROTECTION TECHNOLOGY CO., LTD. Address before: The eight group Tanzhi town Nanhui District Renyi village of Shanghai city in 201315 Patentee before: Shanghai Ruihui Machinery Equipment Manufacturing Co., Ltd. |