CN1481926A - Technology for magnesia wet method stack gas desulfurization and recovering the products - Google Patents
Technology for magnesia wet method stack gas desulfurization and recovering the products Download PDFInfo
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- CN1481926A CN1481926A CNA031098053A CN03109805A CN1481926A CN 1481926 A CN1481926 A CN 1481926A CN A031098053 A CNA031098053 A CN A031098053A CN 03109805 A CN03109805 A CN 03109805A CN 1481926 A CN1481926 A CN 1481926A
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- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 title claims abstract description 67
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 49
- 230000023556 desulfurization Effects 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 38
- 239000000395 magnesium oxide Substances 0.000 title claims abstract description 34
- 238000005516 engineering process Methods 0.000 title claims description 27
- 239000007787 solid Substances 0.000 claims abstract description 4
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims abstract 10
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims abstract 5
- 235000019341 magnesium sulphate Nutrition 0.000 claims abstract 5
- 238000010521 absorption reaction Methods 0.000 claims description 37
- 239000003546 flue gas Substances 0.000 claims description 36
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 35
- 239000007788 liquid Substances 0.000 claims description 27
- 239000000047 product Substances 0.000 claims description 22
- 238000002425 crystallisation Methods 0.000 claims description 19
- 230000008025 crystallization Effects 0.000 claims description 18
- 239000012535 impurity Substances 0.000 claims description 15
- 230000003647 oxidation Effects 0.000 claims description 12
- 238000007254 oxidation reaction Methods 0.000 claims description 12
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 8
- 238000001914 filtration Methods 0.000 claims description 8
- 239000012452 mother liquor Substances 0.000 claims description 8
- 229910052717 sulfur Inorganic materials 0.000 claims description 8
- 239000011593 sulfur Substances 0.000 claims description 8
- 238000006298 dechlorination reaction Methods 0.000 claims description 7
- 230000018044 dehydration Effects 0.000 claims description 7
- 238000006297 dehydration reaction Methods 0.000 claims description 7
- 239000007789 gas Substances 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 239000000706 filtrate Substances 0.000 claims description 5
- 125000004122 cyclic group Chemical group 0.000 claims description 4
- 235000011389 fruit/vegetable juice Nutrition 0.000 claims description 4
- 239000012263 liquid product Substances 0.000 claims description 4
- 239000000843 powder Substances 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- 238000009413 insulation Methods 0.000 claims description 3
- 238000005192 partition Methods 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 claims description 2
- 238000011027 product recovery Methods 0.000 claims description 2
- 238000005406 washing Methods 0.000 claims description 2
- 239000010440 gypsum Substances 0.000 abstract description 7
- 229910052602 gypsum Inorganic materials 0.000 abstract description 7
- 230000003009 desulfurizing effect Effects 0.000 abstract description 6
- 239000002893 slag Substances 0.000 abstract description 4
- 239000013078 crystal Substances 0.000 abstract description 3
- 239000003517 fume Substances 0.000 abstract description 2
- 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 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 6
- 238000011084 recovery Methods 0.000 description 6
- 239000002994 raw material Substances 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 239000000779 smoke Substances 0.000 description 4
- 235000019738 Limestone Nutrition 0.000 description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 239000006028 limestone Substances 0.000 description 3
- 239000011777 magnesium Substances 0.000 description 3
- 229910052749 magnesium Inorganic materials 0.000 description 3
- 239000007790 solid phase Substances 0.000 description 3
- ZGBSOTLWHZQNLH-UHFFFAOYSA-N [Mg].S(O)(O)(=O)=O Chemical compound [Mg].S(O)(O)(=O)=O ZGBSOTLWHZQNLH-UHFFFAOYSA-N 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000000347 magnesium hydroxide Substances 0.000 description 2
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 2
- 210000002966 serum Anatomy 0.000 description 2
- 238000005979 thermal decomposition reaction Methods 0.000 description 2
- 238000009825 accumulation Methods 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000010410 dusting Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- SMDQFHZIWNYSMR-UHFFFAOYSA-N sulfanylidenemagnesium Chemical compound S=[Mg] SMDQFHZIWNYSMR-UHFFFAOYSA-N 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Abstract
The present invention is one improvement of available wet magnesia fume desulfurizing and product recovering process. Technologically, the present invention features that air is blown in during desulfurization with circular absorbing solution to oxidize the desulfurized product MgSO3 into MgSO4 timely and continuously and high concentration MgSO4 solution is led out from the tower and further filtered and crystallized to separate coarse MgSO4.7H2O crystal. The technological process is simple, lower sulfite radical level inside the circulating solution and greatly lowered recovering cost. The recovered MgSO4.7H2O has industrial value greatly higher than gypsum and available solid desulfurized slag.
Description
Technical field
The invention belongs to the flue gas desulfurization technique field, particularly a kind of new technology of utilizing flue gas desulfurization by magnesia wet method and product to reclaim.
Background technology
Flue gas desulfurization technique is to cut down SO
2Discharge capacity and control acid rain pollute one of the most effective basic means.Flue gas desulfurization has become world today's control SO as the limestone/gypsum method
2The dominant technology of discharging also is the generating plant flue gas desulfur technology that China's emphasis is introduced and applied.Recycle angle from desulfurization product, the gypsum of this method accessory substance has the low relatively and big characteristics of potential market of quality requirements as the building materials raw material, and domestic industrial technology and the equipment of successfully having developed desulfurization of gypsum slag thermal decomposition system sulfuric acid and co-producing cement.But China abounds with gypsum, and is cheap, and recovery value is little, is faced with the immense pressure of market competition, can not effectively compensate the desulfurization operation cost again.Desulphurization system is long more running time, and the user sustains economic losses many more, causes the desulfurizer that has built up can not normal operation input.Exploitation is fit to the new process for fume desulfurization of national conditions, and solving the medium-and-large-sized boiler of China (comprising station boiler) flue gas desulfurization problem cost-effectively is a great problem that the present invention is devoted to solve.
Existing flue gas desulfurization technique is of a great variety, wherein magnesia wet desulfurizing process and limestone/gypsum method are quite similar, and China's magnesia (magnesia) aboundresources, as desulfurizing agent, expense exceeds seldom than lime stone, and has the advantage of desulfurization of being more conducive to and recovery.On existing magnesium method sulfur removal technology basis, in conjunction with the actual conditions of China's magnesium resource and large medium-size boiler smoke evacuation, make process choice more targetedly, have the effect of getting twice the result with half the effort.
Existing flue gas desulfurization by magnesia wet method typical process as shown in Figure 1.Be cooled to 80～100 ℃ from the boiler sulfur-containing smoke gas after the dedusting through flue gas reheat and venturi pre-wash, after cyclonic separation, enter SO again
2The absorption tower desulfurization.Flue gas after being purified is through the demist dehydration and be sent to smoke stack emission after the heat intensification again.Utilize magnesia to be mixed with desulfurizer slurry through slaking and send into desulfuration absorbing tower, desulfurizing agent concentration is generally got about 10%, presses sulphur magnesium and supplies slurry than≤1.1.Desulfurization degree is regulated and control by the liquid-gas ratio and the pH value of circulating absorption solution.It is that the part circulating absorption solution is drawn that desulfurization product reclaims, and through multiviscosisty, centrifugal filtration and oven dry, directly leaches solid-state desulfurization product.This technology makes MgSO earlier in the absorption liquid circulating slot
3Crystallization, the crystal grain enormous amount crystallization motive force that provides because of solid phase particle in the circulating absorption solution is little, causes crystal grain tiny, and follow-up centrifugal filtration power consumption is big and the dehydration degree of depth is low; More can not finish and the solid phase separate impurities, generally as thermal decomposition regeneration MgO and recovery SO
2The raw material of relieving haperacidity, thus with fuel oil combustion heat supply drying and dewatering, from and draw the problem of product secondary recovery and flue gas double purification.The MgSO that the desulfurization main reaction generates in the while absorption liquid
3Easily oxidation generates the MgSO of a part of solubilised state
4, in filter process, run off, and new MgSO arranged in dry run
4Generate; In fact dehydration and dried desulfurization product are with MgSO
3Be main, contain MgSO
4, MgO and impurity and flue dust mixture, when higher and MgO desulfurizing agent purity is low at dust content especially, will seriously reduce quality and the value thereof that reclaims product.Though China is rich in fine quality magnesium ore deposit, as natural mineral products, purity is limited after all, general impurity content about 15%.And China's general deficiency of the large medium-size boiler flue gas ash removal degree of depth and oxygen content height, if indiscriminately imitate this technology, the recycling of desulfurization product can become a mere formality, impurity content is very high, the MgSO that liquid phase runs off
4Measure also greatly, reclaim and difficult the utilization though have.
Summary of the invention
The purpose of this invention is to provide a kind of flue gas desulfurization by magnesia wet method and product and reclaim new technology, promptly propose a kind of flue gas desulfurization by magnesia wet method and reclaim MgSO
4.7H
2The technology of O, this technology are enabled cheap common magnesia powder and are made desulfurizing agent, and utilize MgSO
3Easily oxidizable, with the MgSO in the circulating absorption solution
3In time be oxidized to MgSO
4Reduce the MgSO in the circulation fluid greatly
3Content is beneficial to desulfurization and antiscale; The MgSO of high dissolving
4Both be convenient to and the separating of various solid impurities, and can have finished and the liquid phase separate impurities by crystallization again, and can significantly reduce the processing flow of liquid filtration and Crystallization Separation, thereby solve the problem that existing technology exists cost-effectively, improve the technical and economic performance of desulfurization and recycling comprehensively.
Technical scheme of the present invention is as follows:
A kind of flue gas desulfurization by magnesia wet method and product reclaim new technology, mainly comprise the dechlorination of venturi pre-wash, and cyclonic separation enters the absorption tower with common magnesia powder preparation desulfurizer slurry and absorbs SO
2The washing, purifying flue gas, demist and flue gas reheat sulfur removal technology step, and absorption liquid cyclic oxidation and partially absorb the liquid product and reclaim technology is characterized in that described absorption liquid cyclic oxidation and partially absorb the liquid product reclaiming technology and carrying out as follows:
(1) in the circulating absorption solution sweetening process, blasts air, with once desulfurization product MgSO
3In time and constantly be oxidized to MgSO
4,, make the MgSO of solubilised state through juice circulation
4Mass percent concentration＞25%;
(2) draw a part in the tower and contain MgSO
4Absorption liquid is removed solid impurity after filtration;
(3) filtrate is cooled to 10～20 ℃, makes its crystallization separate out coarse grained MgSO
4.7H
2O finishes and mother liquor main body and liquid phase separate impurities thereof;
(4) MgSO that crystallization is separated out
4.7H
2O enters the centrifugal filtration dehydration, finishes and grain surface residual moisture and separate impurities, makes MgSO after the oven dry
4.7H
2The O finished product;
(5) the remaining mother liquor of crystallization and the discharge liquid of centrifugal dehydration return the absorption tower circulation desulfurization again.
The venturi pre-wash is adopted in pre-wash dechlorination described in the present invention, and its liquid-gas ratio is 1.0～1.5.Described juice circulation is to utilize the heating of flue gas partition to strengthen the insulation of absorption liquid oxidation trough, makes the MgSO of solubilised state
4Mass percent concentration is preferably 30～32%.
In crystallization process, separate out coarse grained MgSO for making crystallization
4.7H
2O, filtrate can slowly be cooled off the formation nucleus through air earlier, makes it quicken crystallization with the jacket type water-cooled again.
The present invention compared with prior art has the following advantages and the high-lighting progress:
The present invention is more simpler than existing technology, and commercial test results shows: only use simple and easy oxidation measure, just can make the SO in the circulation fluid
3 2-Be stabilized under the level of hundreds of ppm, very help SO
2To mass transfer in liquid phase; At MgSO
4Continuous accumulation is incremented to more than 30% and even in 35% the process, desulfurization degree remains at about 95%.The MgSO of high-dissolvability
4And SO
3 2-Low-level fouling and the obstruction that can avoid desulphurization system more reliably, and make the absorption liquid flow of drawing the do recycling reduce 2/3rds, thus reduce the cost of recycling significantly.The MgSO that reclaims
4.7H
2O, not only use value is directly isolated the main MgSO that contains far above gypsum than existing technology from absorption liquid
3.6H
2Solid-state desulfurization slag or the MgSO of O
3Dried slag also has higher industrial utilization to be worth.Through conservative estimation, one ton of content is 85% common magnesia, by the MgO utilization rate 90% and the rate of recovery 75%, on the 35t/h of coal-fired sulfur-bearing 2% boiler, moves 8 hours and just can change 1 ton of common magnesia into 3.5tMgSO
4.7H
2O.From the recovery that is fed into desulfurization product of desulfurization material, produce MgSO with reference to MgO raw material of the same race and strong sulfuric acid response
4.7H
2The price of O is also deducted the MgO raw material cost, 231 yuan/h of unit interval increment, and the charges for water and electricity of whole desulphurization system operation are by 0.5 yuan/Kwh and 1 yuan/m
3Meter generally is no more than 180 yuan/h.Desulfurization product of the present invention reclaims benefit and can maintain an equal level with the power and the consumption of raw materials of desulfurization when coal-fired sulfur-bearing 1.5%.Coal-fired sulfur-bearing is high more, and the flue gas desulfurization scale is big more, and benefit is good more.
Description of drawings
Fig. 1 is existing flue gas desulfurization by magnesia wet method and product recovery processing technique flow chart.
Fig. 2 is flue gas desulfurization by magnesia wet method provided by the invention and crystallization reclaim sulfuric acid magnesium process chart.
Fig. 3 is the system architecture schematic diagram of flue gas desulfurization by magnesia wet method provided by the invention and crystallization reclaim sulfuric acid magnesium process implementing example.
Among the figure: 1-pre-wash dechlorination device, 2-liquid cyclonic wind separator, 3-SO
2The absorption tower, 4-demister, 5-flue gas reheat device, 6-magnesium hydroxide slurry-supplying can, 7-magnesia serum pot, 8-absorption liquid oxidation trough, 9-absorption liquid filter, 10-cooler crystallizer, 11-centrifugal filter, 12-MgSO
4.7H
2The O drier, the 13-mother liquor tank
The specific embodiment
The invention will be further described below in conjunction with accompanying drawing.
As Fig. 2, shown in Figure 3, from the sulfur-containing smoke gas behind the boiler dusting, after 5 coolings of flue gas reheat device, enter pre-wash dechlorination device 1, enable the short venturi that closely contacts with gas-liquid two-phase of the time of staying, make pre-wash, reduce SO with 1.0～1.5 low liquid-gas ratio
2Loss and relative more effectively dechlorination make SO in the circulating absorption solution
4 2-And Cl
-Concentration difference increase.Flue gas after the pre-wash enters gas-liquid separation device 2, utilizes the heating of flue gas partition to strengthen the insulation of absorption liquid oxidation trough 8 simultaneously.Flue gas after the gas-liquid separation enters SO
2Demister 4 and flue gas reheat device 5 are passed through in absorption tower 3 desulfurization again, cause the chimney emptying by the desulfurization blower fan.Magnesia powder enters SO by magnesium hydroxide slurry-supplying can 6 at magnesia serum pot 7 after slaking
2 Absorption tower 3 forms circulating absorption solution and absorbs SO
2Absorption liquid oxidation trough 8 is located at SO
2The bottom on absorption tower 3 blasts air in the circulating absorption solution sweetening process in absorption liquid oxidation trough 8, with once desulfurization product MgSO
3In time and constantly be oxidized to MgSO
4, through the quasi saturation concentration of circulation enrichment to the circulation fluid temperature.Generally make the MgSO of solubilised state
4Mass percent concentration＞25% preferably remains in 30～32% the scope.To partially absorb liquid leads to filter 9 and does depth-type filtration and remove solid phase impurity; Filtrate flows into cooler crystallizer 10, in crystallization process, can slowly cool off through air earlier, again through jacket type water-cooled to 10～20 ℃, makes its crystallization and forms the coarse grained MgSO of mm level
4.7H
2O finishes and mother liquor main body and liquid phase separate impurities thereof; Last finishing in centrifugal filter 11 with the degree of depth of mother liquor and liquid phase impurity thereof separated, and 12 oven dry of drying device get final product again.The MgSO that reclaims
4.7H
2The MgSO that O quality and magnesia and strong sulfuric acid response are produced
4.7H
2O is suitable.The mother liquor that is come out by cooler crystallizer 10 and centrifugal filter 11 returns absorption tower 3, cl to the tower
-Concentration can efflux in the time of will be above 20g/l.
Claims (4)
1. flue gas desulfurization by magnesia wet method and product reclaim new technology, mainly comprise the pre-wash dechlorination, and gas-liquid separation enters absorption tower absorption SO with common magnesia powder preparation desulfurizer slurry
2, washing, purifying flue gas, demist and flue gas reheat sulfur removal technology step, and absorption liquid cyclic oxidation and partially absorb the liquid product and reclaim technology is characterized in that described absorption liquid cyclic oxidation and partially absorb the liquid product reclaiming technology and carrying out as follows:
(1) blast air in the circulating absorption solution sweetening process, MgSO3 in time and constantly is oxidized to MgSO4 with the once desulfurization product, through juice circulation, makes MgSO4 mass percent concentration＞25% of solubilised state;
(2) draw a part in the tower and contain the MgSO4 absorption liquid, remove solid impurity after filtration;
(3) filtrate is cooled to 10～20 ℃ of phase separate impurities, makes its crystallization separate out coarse grained MgSO47H2O, finish and mother liquor main body and liquid thereof;
(4) MgSO47H2O that crystallization is separated out enters the centrifugal filtration dehydration, finishes and grain surface residual moisture and separate impurities, makes the MgSO47H2O finished product;
(5) the remaining mother liquor of crystallization and the discharge liquid of centrifugal dehydration return the absorption tower circulation desulfurization again, and cl-concentration will be above effluxing behind the 20g/l to the tower.
2. reclaim new technology according to described flue gas desulfurization by magnesia wet method of claim 1 and product, it is characterized in that: the venturi pre-wash is adopted in described pre-wash dechlorination, and its liquid-gas ratio is 1.0～1.5.
3. according to claim 1 or 2 described flue gas desulfurization by magnesia wet method and product recovery new technology, it is characterized in that: described juice circulation is to utilize the heating of flue gas partition to strengthen the insulation of absorption liquid oxidation trough (8), makes the MgSO of solubilised state
4Mass percent concentration remains on 30～32%.
4. reclaim new technology according to described flue gas desulfurization by magnesia wet method of claim 1 and product, it is characterized in that: in crystallization process, filtrate is slowly cooled off the formation nucleus through air earlier, makes it quicken crystallization with the jacket type water-cooled again.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03109805 CN1207083C (en) | 2003-04-11 | 2003-04-11 | Technology for magnesia wet method stack gas desulfurization and recovering the products |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 03109805 CN1207083C (en) | 2003-04-11 | 2003-04-11 | Technology for magnesia wet method stack gas desulfurization and recovering the products |
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| Publication Number | Publication Date |
|---|---|
| CN1481926A true CN1481926A (en) | 2004-03-17 |
| CN1207083C CN1207083C (en) | 2005-06-22 |
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| CN 03109805 Expired - Fee Related CN1207083C (en) | 2003-04-11 | 2003-04-11 | Technology for magnesia wet method stack gas desulfurization and recovering the products |
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Cited By (18)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1332000C (en) * | 2006-01-12 | 2007-08-15 | 张新明 | Desulfate agent for fuel coal and preparation process thereof |
| CN100335154C (en) * | 2005-09-09 | 2007-09-05 | 清华大学 | Magnesium oxide flue gas desulfurization and outgrowth thick-slurry method oxidation reclaim process |
| CN101628199A (en) * | 2008-07-17 | 2010-01-20 | 中国石化集团宁波工程有限公司 | Improved magnesium method flue gas desulphurization technique |
| 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 |
| CN101016175B (en) * | 2006-02-12 | 2011-10-05 | 滨化集团股份有限公司 | Method of eliminating magnesium sulfate from magnesium sulfate containing waste water solution |
| CN102350197A (en) * | 2011-07-11 | 2012-02-15 | 华东理工大学 | Fume desulfurizing and denitrifying device based on magnesia and method |
| CN102631836A (en) * | 2012-04-20 | 2012-08-15 | 深圳市粤华机电技术开发有限公司 | New process for recycling magnesium sulfate heptahydrate by utilizing magnesium oxide flue gas desulfurization |
| CN102806004A (en) * | 2011-05-30 | 2012-12-05 | 中国石油化工股份有限公司 | Magnesium desulfurization byproduct recovery process |
| CN103387247A (en) * | 2012-05-09 | 2013-11-13 | 中节能六合天融环保科技有限公司 | Process for preparing magnesium sulfate heptahydrate and liquid sulfur dioxide by comprehensively utilizing magnesium desulfurization byproducts |
| CN103387246A (en) * | 2012-05-09 | 2013-11-13 | 中节能六合天融环保科技有限公司 | Treatment process suitable for rapidly oxidizing magnesium sulfite to magnesium sulfate |
| CN103394281A (en) * | 2013-08-08 | 2013-11-20 | 常州联慧资源环境科技有限公司 | Water expansion control and desulfurization product slurry concentration method for magnesium-method flue gas desulfurization system |
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| CN104556157A (en) * | 2014-12-03 | 2015-04-29 | 北京中晶佳镁环境科技股份有限公司 | Magnesium sulfate production device and method by flue gas desulfurization |
| CN104556159A (en) * | 2014-12-15 | 2015-04-29 | 北京中晶佳镁环境科技股份有限公司 | Device and method for producing magnesium sulfite by flue gas desulfurization |
| WO2016086735A1 (en) * | 2014-12-03 | 2016-06-09 | 童裳慧 | Apparatus and method for producing magnesium sulphate from coal-fired boiler flue gas |
| CN105771598A (en) * | 2016-04-01 | 2016-07-20 | 四川明晶光电科技有限公司 | Method for de-dusting and desulfurating smoke through wet process of large touch area tower |
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Cited By (24)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100335154C (en) * | 2005-09-09 | 2007-09-05 | 清华大学 | Magnesium oxide flue gas desulfurization and outgrowth thick-slurry method oxidation reclaim process |
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