CN114768498A - Magnesium desulfurization system and method - Google Patents
Magnesium desulfurization system and method Download PDFInfo
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- CN114768498A CN114768498A CN202210483790.8A CN202210483790A CN114768498A CN 114768498 A CN114768498 A CN 114768498A CN 202210483790 A CN202210483790 A CN 202210483790A CN 114768498 A CN114768498 A CN 114768498A
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 73
- 230000023556 desulfurization Effects 0.000 title claims abstract description 73
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 title claims abstract description 41
- 239000011777 magnesium Substances 0.000 title claims abstract description 41
- 229910052749 magnesium Inorganic materials 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 28
- 239000002002 slurry Substances 0.000 claims abstract description 153
- 238000006243 chemical reaction Methods 0.000 claims abstract description 108
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims abstract description 58
- 238000002425 crystallisation Methods 0.000 claims abstract description 53
- 230000008025 crystallization Effects 0.000 claims abstract description 53
- 238000010521 absorption reaction Methods 0.000 claims abstract description 36
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims abstract description 29
- 235000019341 magnesium sulphate Nutrition 0.000 claims abstract description 29
- 239000007788 liquid Substances 0.000 claims abstract description 20
- JESHZQPNPCJVNG-UHFFFAOYSA-L magnesium;sulfite Chemical compound [Mg+2].[O-]S([O-])=O JESHZQPNPCJVNG-UHFFFAOYSA-L 0.000 claims abstract description 19
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 19
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000003546 flue gas Substances 0.000 claims abstract description 11
- 230000003647 oxidation Effects 0.000 claims abstract description 11
- 239000012066 reaction slurry Substances 0.000 claims description 28
- 239000003054 catalyst Substances 0.000 claims description 13
- 238000005086 pumping Methods 0.000 claims description 13
- 230000003197 catalytic effect Effects 0.000 claims description 9
- 239000000395 magnesium oxide Substances 0.000 claims description 8
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 8
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 8
- 238000004321 preservation Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 6
- 238000003756 stirring Methods 0.000 claims description 6
- 239000000725 suspension Substances 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 3
- 238000011085 pressure filtration Methods 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims 1
- 239000007921 spray Substances 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 9
- 238000001556 precipitation Methods 0.000 description 6
- 239000002245 particle Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/402—Alkaline earth metal or magnesium compounds of magnesium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/602—Oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a magnesium desulfurization system and a method, the magnesium desulfurization system comprises an absorption tower, a cyclone and a reaction device, the absorption tower is suitable for purifying flue gas and generating desulfurization slurry, the cyclone is provided with a liquid inlet, a first outlet and a second outlet, the liquid inlet is communicated with the absorption tower, the desulfurization slurry can enter the cyclone through the liquid inlet, the cyclone is used for separating the desulfurization slurry into top flow slurry and bottom flow slurry, the top flow slurry can flow back into the absorption tower through the first outlet, the reaction device comprises a reaction box and a jet flow assembly, the second outlet is communicated with the reaction box so as to introduce the bottom flow slurry into the reaction box, the jet flow assembly is connected with the reaction box, and the reaction box is provided with a discharge port. The desulfurization slurry is separated by the cyclone, so that the concentration of magnesium sulfite entering the reaction box is improved, the oxidation efficiency is improved, the concentration of magnesium sulfate after oxidation reaction in the reaction box is increased, the subsequent crystallization efficiency is improved, and the energy consumption is reduced.
Description
Technical Field
The invention belongs to the technical field of flue gas desulfurization, and particularly relates to a magnesium desulfurization system and a magnesium desulfurization method.
Background
The magnesium oxide method flue gas desulfurization technology has high desulfurization efficiency, low operation energy consumption, small investment and strong operation reliability, is widely applied to the flue gas desulfurization process of industrial boilers in recent years, but is not popularized in the power industry due to the lack of an economic and effective magnesium sulfate recovery technology. Therefore, how to economically and efficiently recover the magnesium sulfate is a bottleneck problem of the magnesium oxide desulphurization technology.
In the traditional magnesium oxide method desulfurization process, because the solubility of magnesium sulfate is high (about 35g/100g at 400 ℃), the magnesium sulfate solution (with the concentration of about 5%) discharged from a desulfurization absorption tower has too high unsaturation degree, and if an evaporation concentration process is used, a large amount of energy consumption is generated, so that the economic and efficient concentration of magnesium sulfate becomes a bottleneck problem limiting the recycling of byproducts of the magnesium oxide method process. Meanwhile, the nitrogen recycling product (nitrate/nitrite) is taken as a coexisting component in the desulfurization slurry, and the concentration and crystallization processes of magnesium sulfate are accompanied, so that the influence on the sulfur recycling process is inevitably generated.
Disclosure of Invention
The present invention is directed to solving, at least in part, one of the technical problems in the related art. Therefore, the embodiment of the invention provides a magnesium desulphurization system, which improves the situations of low magnesium sulfate oxidation efficiency and low concentration in the original technical route, improves the oxidation efficiency and concentration of magnesium sulfate, and reduces the consumption of magnesium sulfate concentration and crystallization.
The embodiment of another aspect of the invention provides a magnesium desulfurization method.
The magnesium desulfurization system of the embodiment of the first aspect of the invention comprises: the absorption tower is suitable for purifying flue gas and generating desulfurization slurry, the cyclone is provided with a liquid inlet, a first outlet and a second outlet, the liquid inlet is communicated with the absorption tower, the desulfurization slurry can enter the cyclone through the liquid inlet, the cyclone is used for separating the desulfurization slurry into top flow slurry and bottom flow slurry, the top flow slurry can flow back into the absorption tower through the first outlet, the reaction device comprises a reaction box and a jet flow component, the second outlet is communicated with the reaction box so as to introduce the bottom flow slurry into the reaction box, the jet flow component is connected with the reaction box, the jet flow component is used for mixing part of the bottom flow slurry in the reaction box with air and introducing the bottom flow slurry into the reaction box again so as to stir the bottom flow slurry in the reaction box, the reaction box is provided with a discharge port, the underflow slurry in the reaction box generates reaction slurry after catalytic oxidation reaction, and the discharge port is used for discharging the reaction slurry.
According to the magnesium desulfurization system provided by the embodiment of the invention, the desulfurization slurry is separated through the cyclone, so that the concentration of magnesium sulfite entering the reaction box is increased, the catalytic oxidation reaction is facilitated, and the oxidation efficiency is increased. The underflow slurry in the reaction box is stirred by the jet assembly, so that magnesium sulfite precipitation and magnesium sulfate crystallization are prevented, catalyst particles are overturned and suspended in the reaction box, and the oxidation efficiency of the catalyst is ensured. The concentration of the magnesium sulfate after the oxidation reaction of the reaction box is increased, the subsequent crystallization efficiency is improved, and the energy consumption is reduced.
In some embodiments, the jet assembly includes a jet pump and a jet device, an inlet of the jet pump is communicated with the bottom of the reaction tank, an outlet of the jet pump is communicated with an inlet of the ejector, an outlet of the ejector is communicated with the reaction tank, and the ejector is further provided with an air inlet for introducing air into the ejector.
In some embodiments, the magnesium desulfurization system further comprises a screen disposed on at least one of the discharge port, the second outlet, the inlet of the jet pump, and the outlet of the jet ejector.
In some embodiments, the magnesium desulfurization system further comprises a crystallization device, the reaction tank is communicated with the crystallization device, so that the reaction slurry is introduced into the crystallization device, the crystallization device is used for performing pressure filtration on the slurry after the reaction in the reaction tank, or the crystallization device is used for performing evaporative crystallization on the reaction slurry.
In some embodiments, magnesium method desulfurization system still includes first row's stuff pump and second row's stuff pump, the import of first row's stuff pump with the absorption tower intercommunication, the export of first row's stuff pump with the inlet intercommunication, first row's stuff pump be used for with desulfurization thick liquid pump in the absorption tower is extremely in the swirler, the import of second row's stuff pump with the reaction box intercommunication, the export of second row's stuff pump with the crystallization device intercommunication, the second row's stuff pump be used for with reaction thick liquid pump send extremely in the crystallization device.
In some embodiments, valves are provided on both the first slurry pump and the second slurry pump.
The magnesium desulfurization method of the embodiment of the second aspect of the invention comprises the following steps:
carrying out desulfurization treatment on the flue gas through the absorption tower to form desulfurization slurry;
pumping the desulfurization slurry into the cyclone through the first slurry pump;
separating the desulfurization slurry into an overflow slurry containing a magnesium sulfate solution, a magnesium oxide solution and desalted water and an underflow slurry containing a magnesium sulfite precipitation suspension liquid through the cyclone, wherein the overflow slurry flows back into the absorption tower through the first outlet, and the underflow slurry is introduced into the reaction box through the second outlet;
performing catalytic reaction on the underflow slurry in the reaction box through a catalyst;
pumping the underflow slurry at the bottom of the reaction box into the ejector through the jet pump, sucking air into the ejector through an air inlet by the ejector, and spraying the air and the slurry into the reaction box together to stir the underflow slurry in the reaction box, wherein the underflow slurry in the reaction box generates reaction slurry after catalytic oxidation, and the reaction slurry contains magnesium sulfate solution;
through the second fan pump will the reaction thick liquid pump sending is to in the crystallization device, the crystallization device filters and crystallization the reaction thick liquid.
The magnesium desulfurization method in the embodiment of the second aspect of the invention can improve the concentration of magnesium sulfate entering the crystallization device, improve the crystallization efficiency and reduce the energy consumption.
In some embodiments, the concentration of magnesium sulfite in the desulfurization slurry pumped into the cyclone by the first slurry pump is 5-15% by mass; the concentration of the magnesium sulfite in the underflow slurry led into the reaction box through the second outlet is 10-20% by mass; and the magnesium sulfate mass percentage concentration of the reaction slurry pumped into the crystallization device by the second slurry pump is 15-20%.
In some embodiments, the slurry discharge from the absorber is equal to the slurry discharge from the reaction tank to maintain a balance of the slurry volume in the reaction tank.
In some embodiments, the magnesium desulfurization process further comprises the steps of:
it is right through temperature control device the absorption tower first row stuff pump the swirler the reaction box the jet pump the ejector with the second row stuff pump carries out the companion's heat preservation, and the heat preservation temperature is not less than 30 ℃.
Drawings
FIG. 1 is a schematic diagram of a magnesium desulfurization system according to an embodiment of the present invention.
Reference numerals are as follows:
1. an absorption tower;
2. a swirler; 21. a liquid inlet; 22. a first outlet; 23. a second outlet;
31. a reaction box; 32. a discharge port; 33. a jet pump; 34. an ejector; 35. an air inlet;
4. a first slurry discharging pump;
5. and a second slurry discharge pump.
Detailed Description
Reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings. The embodiments described below with reference to the accompanying drawings are illustrative and intended to explain the present invention and should not be construed as limiting the present invention.
The magnesium desulfurization system according to an embodiment of the present invention will be described with reference to fig. 1.
As shown in fig. 1, the magnesium desulfurization system according to the embodiment of the present invention includes an absorption tower 1, a cyclone 2, and a reaction apparatus. The absorption tower 1 is suitable for purifying flue gas and generating desulfurized slurry, the cyclone 2 is provided with a liquid inlet 21, a first outlet 22 and a second outlet 23, the liquid inlet 21 is communicated with the absorption tower 1, the desulfurized slurry can enter the cyclone 2 through the liquid inlet 21, the cyclone 2 is used for separating the desulfurized slurry into top flow slurry and bottom flow slurry, the top flow slurry can flow back into the absorption tower 1 through the first outlet 22, the reaction device comprises a reaction tank 31 and a jet assembly, the second outlet 23 is communicated with the reaction tank 31 so as to introduce the bottom flow slurry into the reaction tank 31, the jet assembly is connected with the reaction tank 31, the jet assembly is used for mixing part of the bottom flow slurry in the reaction tank 31 with air and re-introducing the bottom flow slurry into the reaction tank 31 so as to stir the bottom flow slurry in the reaction tank 31, the bottom flow slurry in the reaction tank 31 is subjected to catalytic oxidation reaction to generate reaction slurry, and the reaction tank 31 is provided with a discharge port 32, the discharge port 32 is used for discharging the reaction slurry.
It should be noted that, the absorbent in the absorption tower 1 absorbs the sulfur in the flue gas to form a desulfurization slurry containing magnesium sulfate and magnesium sulfite, the desulfurization slurry enters the cyclone 2 and is separated into an overflow slurry containing magnesium sulfate solution, magnesium oxide solution and demineralized water and an underflow slurry containing magnesium sulfite precipitation suspension, the overflow slurry flows back into the absorption tower 1 through the first outlet 22, the underflow slurry flows into the reaction tank 31 through the second outlet 23, the mass percentage concentration of the magnesium sulfite entering the reaction tank 31 is increased, a catalyst is stored in the reaction tank 31, the underflow slurry in the reaction tank 31 is stirred by the jet assembly to prevent the magnesium sulfite particles from precipitating and the high-concentration magnesium sulfate solution from crystallizing, and the catalyst is suspended in the reaction tank 31 by overturning, so as to enhance the reaction effect of the catalyst in the reaction tank 31, and the mass percentage concentration of the magnesium sulfite after catalytic oxidation is increased, thereby improving the crystallization efficiency of downstream equipment and reducing the energy consumption.
According to the magnesium desulfurization system provided by the embodiment of the invention, the desulfurization slurry is separated through the cyclone 2, so that the concentration of the underflow slurry entering the reaction box 31 is improved, the catalytic oxidation reaction is facilitated, and the oxidation efficiency is improved. The underflow slurry in the reaction tank 31 is stirred by the jet assembly, so that magnesium sulfite precipitation and magnesium sulfate crystallization are prevented, catalyst particles are enabled to be overturned and suspended in the reaction tank 31, and the oxidation efficiency of the catalyst is ensured. The concentration of the magnesium sulfate after the oxidation reaction of the reaction box 31 is increased, the subsequent crystallization efficiency is improved, and the energy consumption is reduced.
As shown in fig. 1, in some embodiments, the jet assembly includes a jet pump 33 and a jet device 34, an inlet of the jet pump 33 is communicated with the bottom of the reaction tank 31, an outlet of the jet pump 33 is communicated with an inlet of the jet device, an outlet of the jet device is communicated with the reaction tank 31, and the jet device is further provided with an air inlet 35, wherein the air inlet 35 is used for introducing air into the jet device.
Thus, in these embodiments, a portion of the underflow slurry at the bottom of the reaction tank 31 is pumped into the ejector 34 by the ejector 33, the ejector 34 ejects the underflow slurry into the reaction tank 31 together with air, and the underflow slurry in the reaction tank 31 is agitated, so that the precipitation of magnesium sulfite particles and the crystallization of the high-concentration magnesium sulfate solution are prevented, and the reaction effect of the catalyst in the reaction tank 31 is enhanced.
In some embodiments, the magnesium desulfurization system further includes a screen (not shown) disposed on at least one of the discharge outlet 32, the second outlet 23, the inlet of the jet pump 33, and the outlet of the jet device 34.
Preferably, the discharge port 32, the second outlet 23, the inlet of the jet pump 33 and the outlet of the jet device 34 are provided with a sieve.
It should be noted that the pore size of the filter is selected according to the size of the catalyst.
Thus, in these embodiments, catalyst is prevented from entering the tubes and damaging the equipment by the provision of the screens.
In some embodiments, the magnesium desulfurization system further includes a crystallization device (not shown), and the reaction tank 31 is communicated with the crystallization device to feed the reaction slurry into the crystallization device, the crystallization device is used for performing pressure filtration on the reaction slurry, or the crystallization device is used for performing evaporative crystallization on the reaction slurry.
Optionally, the crystallization apparatus is a plate and frame filter press.
Optionally, the crystallization device is an evaporative crystallization device.
As shown in fig. 1, in some embodiments, the magnesium desulfurization system further includes a first slurry discharge pump 4 and a second slurry discharge pump 5, an inlet of the first slurry discharge pump 4 is communicated with the absorption tower 1, an outlet of the first slurry discharge pump 4 is communicated with the liquid inlet 21, the first slurry discharge pump 4 is used for pumping the desulfurization slurry in the absorption tower 1 into the cyclone 2, an inlet of the second slurry discharge pump 5 is communicated with the reaction tank 31, an outlet of the second slurry discharge pump 5 is communicated with the crystallization device, and the second slurry discharge pump 5 is used for pumping the reaction slurry into the crystallization device.
Further, valves are arranged on the first slurry discharging pump 4 and the second slurry discharging pump 5.
Thus, in these embodiments, the slurry pumping into the cyclone 2 is selectively opened and closed by opening and closing the valve of the first slurry discharge pump 4, and the slurry pumping into the crystallization apparatus is selectively opened and closed by opening and closing the valve of the second slurry discharge pump 5.
The magnesium desulfurization method according to an embodiment of the present invention is described below with reference to fig. 1.
The magnesium desulfurization method of the second aspect of the present invention is implemented by using the magnesium desulfurization system of the above embodiment, wherein the magnesium desulfurization method includes the following steps:
carrying out desulfurization treatment on the flue gas through the absorption tower 1 to form desulfurization slurry;
pumping the desulfurization slurry into the cyclone 2 through a first slurry discharge pump 4;
separating the desulfurization slurry into an overflow slurry mainly containing a magnesium sulfate solution, a magnesium oxide solution and desalted water and an underflow slurry mainly containing a magnesium sulfite precipitation suspension through a cyclone 2, wherein the overflow slurry flows back into the absorption tower 1 through a first outlet 22, and the underflow slurry is introduced into a reaction tank 31 through a second outlet 23;
performing catalytic reaction on the underflow slurry in the reaction tank 31 by using a catalyst;
pumping the underflow slurry at the bottom of the reaction tank 31 into an ejector 34 through a jet pump 33, sucking air into the ejector 34 through an air inlet 35 by the ejector 34, and spraying the air and the underflow slurry into the reaction tank 31 together to stir the underflow slurry in the reaction tank 31, wherein the underflow slurry in the reaction tank is subjected to catalytic oxidation to generate reaction slurry which contains high-concentration magnesium sulfate solution;
the reaction slurry is pumped into a crystallization device through a second slurry discharge pump 5, and the crystallization device filters and crystallizes the reaction slurry.
The magnesium desulfurization method in the embodiment of the second aspect of the invention can improve the concentration of magnesium sulfate entering the crystallization device, improve the crystallization efficiency and reduce the energy consumption.
In some embodiments, the concentration of magnesium sulfite in the desulfurized slurry pumped into cyclone 2 via first slurry pump 4 is between 5 and 15% by mass, such as 5%, 7.5%, 10%, 12.5% or 15%.
The concentration of magnesium sulfite in the underflow slurry introduced into the reaction tank 31 through the second outlet 23 is 10 to 20% by mass, for example, 10%, 12.5%, 15%, 17.5% or 20%.
The magnesium sulfate mass percentage concentration of the reaction slurry pumped into the crystallization device by the second slurry pump 5 is 15-20%, for example, 15%, 16%, 17%, 18%, 19% or 20%.
Therefore, in the embodiments, the mass percentage concentration of the solute is gradually increased by the magnesium desulfurization method, the crystallization efficiency is improved, and the energy consumption is reduced.
In some embodiments, the amount of slurry discharged from the absorption tower 1 is equal to the amount of slurry discharged from the reaction tank 31, so as to maintain the balance of the amount of slurry in the reaction tank 31.
In some embodiments, the magnesium desulfurization method further comprises the steps of:
the absorption tower 1, the first slurry discharge pump 4, the cyclone 2, the reaction tank 31, the jet pump 33, the jet device 34, the second slurry discharge pump 5 and connecting pipelines therebetween are subjected to heat tracing and heat preservation through a temperature control device (not shown), and the heat preservation temperature is not lower than 30 ℃.
Therefore, in the embodiments, the temperature control device is used for heat tracing heat preservation, and the influence of the supercooling crystallization of the solute on the fluidity of the slurry is prevented.
In the description of the present invention, it is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are not to be considered limiting of the invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or to implicitly indicate the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of the feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; may be mechanically coupled, may be electrically coupled or may be in communication with each other; they may be directly connected or indirectly connected through intervening media, or they may be interconnected within two elements or in a relationship where two elements interact with each other unless otherwise specifically limited. The specific meanings of the above terms in the present invention can be understood according to specific situations by those of ordinary skill in the art.
In the present invention, unless expressly stated or limited otherwise, the first feature "on" or "under" the second feature may be directly contacting the second feature or the first and second features may be indirectly contacting each other through intervening media. Also, a first feature "on," "above," and "over" a second feature may be directly on or obliquely above the second feature, or simply mean that the first feature is at a higher level than the second feature. A first feature "under," "beneath," and "under" a second feature may be directly under or obliquely under the second feature, or may simply mean that the first feature is at a lesser elevation than the second feature.
In the present disclosure, the terms "one embodiment," "some embodiments," "an example," "a specific example," or "some examples" and the like mean that a specific feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present disclosure. In this specification, the schematic representations of the terms used above are not necessarily intended to refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
Although the above embodiments have been shown and described, it should be understood that they are exemplary and should not be construed as limiting the present invention, and that many changes, modifications, substitutions and alterations to the above embodiments may be made by those of ordinary skill in the art without departing from the scope of the present invention.
Claims (10)
1. A magnesium desulfurization system, comprising:
the absorption tower (1) is suitable for purifying flue gas and generating desulfurization slurry in the absorption tower (1);
the cyclone (2) is provided with a liquid inlet (21), a first outlet (22) and a second outlet (23), the liquid inlet (21) is communicated with the absorption tower (1), the desulfurization slurry can enter the cyclone (2) through the liquid inlet (21), the cyclone (2) is used for separating the desulfurization slurry into an overflow slurry and an underflow slurry, and the overflow slurry can flow back to the absorption tower (1) through the first outlet (22);
the reaction device comprises a reaction tank (31) and a jet assembly, the second outlet (23) is communicated with the reaction tank (31) to introduce the underflow slurry into the reaction tank (31), the jet assembly is connected with the reaction tank (31), the jet assembly is used for mixing part of the underflow slurry in the reaction tank (31) with air and re-introducing the mixed underflow slurry into the reaction tank (31) so as to stir the underflow slurry in the reaction tank (31), the underflow slurry in the reaction tank (31) is subjected to catalytic oxidation reaction to generate reaction slurry, a discharge port (32) is arranged on the reaction tank (31), and the discharge port (32) is used for discharging the reaction slurry.
2. The magnesium desulfurization system according to claim 1, wherein the jet assembly comprises a jet pump (33) and a jet device (34), an inlet of the jet pump (33) is communicated with the bottom of the reaction tank (31), an outlet of the jet pump (33) is communicated with an inlet of the jet device, an outlet of the jet device is communicated with the reaction tank (31), and the jet device is further provided with an air inlet (35), wherein the air inlet (35) is used for introducing air into the jet device.
3. The magnesium desulfurization system of claim 2, further comprising a screen disposed on at least one of the discharge port (32), the second outlet (23), an inlet of the jet pump (33), and an outlet of the jet ejector (34).
4. The magnesium desulfurization system according to claim 1, further comprising a crystallization device, wherein the reaction tank (31) is communicated with the crystallization device to introduce the reaction slurry into the crystallization device, the crystallization device is used for pressure filtration of the reaction slurry, or the crystallization device is used for evaporative crystallization of the reaction slurry.
5. The magnesium desulfurization system according to claim 4, characterized in that it further comprises a first slurry discharge pump (4) and a second slurry discharge pump (5), the inlet of the first slurry discharge pump (4) is communicated with the absorption tower (1), the outlet of the first slurry discharge pump (4) is communicated with the liquid inlet (21), the first slurry discharge pump (4) is used for pumping the desulfurization slurry in the absorption tower (1) into the cyclone (2), the inlet of the second slurry discharge pump (5) is communicated with the reaction tank (31), the outlet of the second slurry discharge pump (5) is communicated with the crystallization device, and the second slurry discharge pump (5) is used for pumping the reaction slurry into the crystallization device.
6. The magnesium desulphurization system according to claim 5, wherein the first slurry pump (4) and the second slurry pump (5) are provided with valves.
7. A magnesium desulfurization method using the magnesium desulfurization system according to any one of claims 1 to 6, comprising:
carrying out desulfurization treatment on the flue gas through the absorption tower (1) to form desulfurization slurry;
pumping the desulfurized slurry into the cyclone (2) by the first slurry pump (4);
separating the desulphurized slurry into an overhead slurry containing a magnesium sulphate solution, a magnesium oxide solution and demineralized water and an underflow slurry containing a suspension of precipitated magnesium sulphite through the cyclone (2), wherein the overhead slurry flows back into the absorption column (1) through the first outlet (22), and the underflow slurry is introduced into the reaction tank (31) through the second outlet (23);
catalytically reacting the underflow slurry in the reaction tank (31) with a catalyst;
pumping the underflow slurry at the bottom of the reaction box (31) into the ejector (34) through the ejector pump (33), wherein the ejector (34) sucks air into the ejector (34) through an air inlet (35) and sprays the air and the slurry into the reaction box (31) together to stir the underflow slurry in the reaction box (31), and the underflow slurry in the reaction box (31) generates reaction slurry after being subjected to catalytic oxidation, wherein the reaction slurry contains magnesium sulfate solution;
and pumping the reaction slurry into the crystallization device through the second slurry discharge pump (5), and filtering and crystallizing the reaction slurry by the crystallization device.
8. The magnesium desulphurization method according to claim 7, wherein the concentration of magnesium sulfite in the desulphurization slurry pumped into the cyclone (2) by the first slurry pump (4) is 5-15% by mass;
the concentration of the magnesium sulfite in the underflow slurry led into the reaction box (31) through the second outlet (23) is 10-20% by mass;
and the magnesium sulfate mass percentage concentration in the reaction slurry pumped into the crystallization device by the second slurry discharge pump (5) is 15-20%.
9. The magnesium desulfurization method according to claim 7, wherein the amount of the slurry discharged from the absorption tower (1) is equal to the amount of the slurry discharged from the reaction tank (31) so as to maintain the balance of the amount of the slurry in the reaction tank (31).
10. The magnesium desulfurization method according to claim 7, further comprising the steps of:
it is right through temperature control device absorption tower (1) first fan pump (4) swirler (2) reaction box (31) jet pump (33) ejector (34) with second fan pump (5) carry out the companion's heat preservation, and the heat preservation temperature is not less than 30 ℃.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114656076A (en) * | 2022-04-11 | 2022-06-24 | 重庆远达烟气治理特许经营有限公司科技分公司 | Desulfurization wastewater treatment method and desulfurization wastewater treatment equipment |
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| CN102019139A (en) * | 2010-12-31 | 2011-04-20 | 中电投远达环保工程有限公司 | Magnesium desulfurization system |
| CN107051171A (en) * | 2017-05-12 | 2017-08-18 | 常州联慧资源环境科技有限公司 | A kind of double tower magnesium method flue gas desulphurization technique |
| CN111054279A (en) * | 2019-12-31 | 2020-04-24 | 广东雪迪龙环境科技有限公司 | Catalytic oxidation process device and method for magnesium sulfite |
| CN113856429A (en) * | 2021-09-30 | 2021-12-31 | 沈阳工业大学 | Magnesium-method desulfurization device and method based on resource utilization |
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| CN102019139A (en) * | 2010-12-31 | 2011-04-20 | 中电投远达环保工程有限公司 | Magnesium desulfurization system |
| CN107051171A (en) * | 2017-05-12 | 2017-08-18 | 常州联慧资源环境科技有限公司 | A kind of double tower magnesium method flue gas desulphurization technique |
| CN111054279A (en) * | 2019-12-31 | 2020-04-24 | 广东雪迪龙环境科技有限公司 | Catalytic oxidation process device and method for magnesium sulfite |
| CN113856429A (en) * | 2021-09-30 | 2021-12-31 | 沈阳工业大学 | Magnesium-method desulfurization device and method based on resource utilization |
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| CN114656076A (en) * | 2022-04-11 | 2022-06-24 | 重庆远达烟气治理特许经营有限公司科技分公司 | Desulfurization wastewater treatment method and desulfurization wastewater treatment equipment |
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