CN116212635A - Seawater recycling flue gas desulfurization method - Google Patents
Seawater recycling flue gas desulfurization method Download PDFInfo
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- 239000013535 sea water Substances 0.000 title claims abstract description 90
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 63
- 239000003546 flue gas Substances 0.000 title claims abstract description 63
- 238000000034 method Methods 0.000 title claims abstract description 48
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 38
- 230000023556 desulfurization Effects 0.000 title claims abstract description 38
- 238000004064 recycling Methods 0.000 title claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims abstract description 36
- 238000002156 mixing Methods 0.000 claims abstract description 16
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims abstract description 13
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000000292 calcium oxide Substances 0.000 claims abstract description 8
- 238000010438 heat treatment Methods 0.000 claims abstract description 5
- 238000007254 oxidation reaction Methods 0.000 claims description 32
- 230000003647 oxidation Effects 0.000 claims description 24
- 239000011575 calcium Substances 0.000 claims description 20
- 230000008929 regeneration Effects 0.000 claims description 15
- 238000011069 regeneration method Methods 0.000 claims description 15
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 230000002378 acidificating effect Effects 0.000 claims description 4
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 3
- 244000005700 microbiome Species 0.000 claims description 3
- 238000001556 precipitation Methods 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 235000012255 calcium oxide Nutrition 0.000 abstract description 7
- 150000002500 ions Chemical class 0.000 abstract description 3
- 238000007599 discharging Methods 0.000 abstract description 2
- 230000001376 precipitating effect Effects 0.000 abstract description 2
- 238000000746 purification Methods 0.000 abstract description 2
- 150000003568 thioethers Chemical class 0.000 abstract description 2
- 238000004090 dissolution Methods 0.000 abstract 1
- 239000011777 magnesium Substances 0.000 description 25
- 238000005516 engineering process Methods 0.000 description 11
- 238000002485 combustion reaction Methods 0.000 description 8
- 229910019440 Mg(OH) Inorganic materials 0.000 description 6
- 238000005260 corrosion Methods 0.000 description 5
- 230000007797 corrosion Effects 0.000 description 4
- 230000003009 desulfurizing effect Effects 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000005507 spraying Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- RBORURQQJIQWBS-QVRNUERCSA-N (4ar,6r,7r,7as)-6-(6-amino-8-bromopurin-9-yl)-2-hydroxy-2-sulfanylidene-4a,6,7,7a-tetrahydro-4h-furo[3,2-d][1,3,2]dioxaphosphinin-7-ol Chemical compound C([C@H]1O2)OP(O)(=S)O[C@H]1[C@@H](O)[C@@H]2N1C(N=CN=C2N)=C2N=C1Br RBORURQQJIQWBS-QVRNUERCSA-N 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000010459 dolomite Substances 0.000 description 1
- 229910000514 dolomite Inorganic materials 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 238000003837 high-temperature calcination Methods 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000012492 regenerant Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002351 wastewater Substances 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
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- 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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- B01D2251/604—Hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/606—Carbonates
-
- 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)
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- Treating Waste Gases (AREA)
Abstract
The invention provides a flue gas desulfurization method for recycling seawater, which belongs to the technical field of flue gas purification and comprises the following steps: adding the filtered seawater and the flue gas to be desulfurized into a mixing reactor, wherein sulfides in the flue gas to be desulfurized are absorbed by the filtered seawater; heating the desulfurized flue gas and discharging the flue gas into the atmosphere; adding Mg (OH) into sea water absorbed with sulfide 2 Then air is filled to remove MgSO 3 Conversion to MgSO 4 The method comprises the steps of carrying out a first treatment on the surface of the Ca (OH) is then added 2 To generate Mg (OH) 2 Precipitating; ca (OH) 2 The heat generated by the reaction of the quicklime and water is used for heating the desulfurized flue gas. The invention absorbs SO in the flue gas by means of natural alkalinity in the seawater 2 Reaction to form SO 3 2‑ Recycled Mg (OH) 2 And dissolution in seawater at pH 5-6Oxygen, SO 3 2‑ Conversion to stable and harmless SO 4 2‑ The ions raise the overall desulfurization efficiency to over 95%.
Description
Technical Field
The invention belongs to the technical field of flue gas purification, and particularly relates to a flue gas desulfurization method by recycling seawater.
Background
The prior desulfurization technology mainly comprises three modes, namely a pre-combustion desulfurization technology, a desulfurization technology in combustion and a desulfurization technology after combustion, wherein the pre-combustion desulfurization technology mainly comprises the steps of crushing and cleaning raw coal, and the desulfurization mainly comprises the step of removing Huang Liutie ores in the coal in a physical mode. The desulfurization technology in combustion mainly comprises spraying desulfurizing agents such as limestone, dolomite and the like into a hearth, calcining the desulfurizing agents by utilizing a high-temperature environment of 1300-1500 ℃ in the hearth, and generating alkaline products such as CaO, mgO and the like and SO in high-temperature flue gas by high-temperature calcination 2 And SO 3 The reaction generates sulfate and sulfite, thereby achieving the purpose of desulfurization and reducing the sulfur content in the flue gas discharged to the atmosphere. However, the desulfurization efficiency of the direct calcium spraying desulfurization technology can only reach about 30% -40%, and can only meet the general environmental protection requirement, which is far from the existing ultra-low emission requirement. Therefore, the sulfur content in the discharged flue gas can be reduced to the environmental protection requirement by combining the post-combustion desulfurization technology.
The desulfurization technology after combustion mainly comprises dry method, semi-dry method and wet method desulfurization, and the three desulfurization technologies after combustion all utilize absorbent or adsorbent to remove SO in flue gas 2 And SO 3 And transform itAmong the three, the wet flue gas desulfurization is most widely used, and the three are mainly technical categories such as seawater desulfurization, ammonia absorption method, magnesium oxide method, gypsum method and the like. The invention patent of China, for example, application publication No. CN113144847A discloses a coupling device for desulfurizing flue gas and low-temperature multi-effect seawater desalination of a thermal power plant and a desulfurizing method, sulfide in the flue gas reacts with seawater, the sulfide is absorbed, desulfurized clean flue gas is discharged from an outlet above a vertical flue, and sodium hydroxide is added to adjust the pH value of the seawater after the reaction. Although the desulfurization efficiency of wet desulfurization can reach more than 90%, the problems of serious corrosion, high maintenance cost, easy secondary pollution and the like generally exist.
Disclosure of Invention
Aiming at the technical problems in the prior art, the invention provides a flue gas desulfurization method for recycling seawater, which absorbs SO in flue gas by means of natural alkalinity in seawater 2 Reaction to form SO 3 2- Recycled Mg (OH) 2 And dissolved oxygen in seawater at pH 5-6 to obtain SO 3 2- Conversion to stable and harmless SO 4 2- The ions raise the overall desulfurization efficiency to over 95%.
The technical scheme adopted by the invention is as follows: a flue gas desulfurization method for recycling seawater, comprising the steps of:
step 1: adding filtered seawater and flue gas to be desulfurized at 47-53 ℃ into a mixing reactor, reacting the flue gas to be desulfurized with the filtered seawater, and absorbing sulfide in the flue gas to be desulfurized by the filtered seawater;
step 2: the desulfurized flue gas enters a heater, is heated to 47-53 ℃ and is discharged into the atmosphere;
step 3: adding Mg (OH) into sea water absorbed with sulfide 2 ；
Step 4: feeding the reacted seawater into an oxidation process chamber, charging air into the oxidation process chamber, and using oxygen in the air to remove MgSO in the seawater 3 Oxidation to MgSO 4 The oxidation process chamber is kept in an acidic environment all the time;
step 5: the seawater after the oxidation reaction is conveyed to Mg (OH) 2 Regeneration chamber, then Ca (OH) is added 2 To generate Mg (OH) 2 Precipitation, used in step 3; wherein Ca (OH) 2 Calcium oxide and water in Ca (OH) 2 And (3) generating reaction in a reaction chamber, wherein heat generated in the reaction process is used for heating the desulfurized flue gas in the step (2).
Further, in the mixing reactor, the filtered seawater is in countercurrent contact with the flue gas to be desulfurized.
Further, the filtered seawater is seawater for filtering out microorganisms and solid particles.
Further, in step 3, sea water and Mg (OH) 2 After the reaction, the salinity of the seawater is measured, the salinity increase rate of the seawater relative to the filtered seawater is calculated, if the salinity increase rate exceeds 30%, the partially reacted seawater is discharged, and the filtered seawater with the corresponding quantity is added.
Further, in the oxidation process chamber, the pH value of the seawater is maintained at 5-6 by adding sulfuric acid.
Further, a stirrer is arranged in the oxidation process chamber and is used for breaking up large bubbles into small bubbles so as to accelerate the oxidation reaction and make the reaction uniformly proceed.
Further, mg (OH) 2 A drain valve is arranged in the regeneration chamber and is used for mixing Ca (OH) 2 The part of the reacted seawater exceeding the set water level is automatically discharged.
Compared with the prior art, the invention has the following beneficial effects:
(1) Compared with the traditional wet desulfurization technology, the desulfurization efficiency of about 90 percent, the method adopted by the invention firstly relies on natural alkalinity in seawater to absorb SO in the flue gas 2 Reaction to form SO 3 2- Mg (OH) is added again 2 Part of SO 3 2- Conversion to SO 4 2- Finally, at pH value of 5-6, the dissolved oxygen in the seawater is utilized to easily remove SO 3 2- Oxidation to stable harmless SO 4 2- The ions raise the overall desulfurization efficiency to over 95%.
(2) The invention is provided with an oxidation process chamber, and oxygen is delivered to the oxidation process chamber by a compressed air pumpMgSO in seawater 3 Complete oxidation to MgSO 4 While maintaining a pH of 5-6 to allow Mg (OH) 2 Completely dissolving, and delivering the solution after the oxidation process chamber is completely oxidized to Mg (OH) 2 The regeneration chamber can effectively reduce material loss and improve economy.
(3) The invention adopts Mg (OH) 2 A regeneration chamber for fully utilizing MgCL in seawater 2 And MgSO 4 With Ca (OH) 2 Reaction to Mg (OH) 2 Since only Mg (OH) is present in the regeneration chamber 2 The catalyst is a precipitate and is a required reactant, and the absorption and oxidation reaction products are easy to be carried out, so that the regeneration chamber has no scaling and deposition phenomena, no cleaning equipment is needed, and the structure is relatively simple and the cost is low.
(4) The invention fully considers the waste heat recycling and adopts the quicklime as Ca (OH) 2 The regenerant mainly considers that the quicklime is convenient to obtain and low in cost, and generates the required Ca (OH) when reacting with water 2 A large amount of heat can be released during the process. In order to prevent the problems of flue gas condensation, low-temperature corrosion and the like, a primary heat exchange device is required to be added before purified flue gas is discharged to a chimney, the temperature of the flue gas is raised to about 50 ℃, the flue gas is ensured to have enough lifting height when discharged from the chimney, and the condensation corrosion of the inner wall of the chimney is prevented. And a large amount of heat generated by the reaction of the quicklime and the water is recycled to heat the flue gas so as to reduce the energy consumption, and the energy utilization efficiency of the whole process flow is improved.
Drawings
Fig. 1 is a schematic diagram of an embodiment of the present invention.
Detailed Description
The present invention will be described in detail below with reference to the drawings and the specific embodiments, so that those skilled in the art can better understand the technical solutions of the present invention.
An embodiment of the present invention provides a flue gas desulfurization method for recycling seawater, as shown in fig. 1, comprising the steps of:
step 1: the temperature of the flue gas discharged from the boiler preheater terminal is about 150 ℃, and the flue gas is reduced to about 50 ℃ by a cooling system for improving SO 2 And simultaneously, the lower flue gas temperature can reduce the material requirement on the anti-corrosion material in the mixing reactor. The filtered seawater is seawater for filtering out microorganisms and solid particles.
Adding filtered seawater and flue gas to be desulfurized at 50 ℃ into a mixing reactor, conveying the filtered seawater to uniformly distributed spray heads at the inner top of the mixing reactor through a conveying pipeline, and uniformly spraying the seawater downwards; the flue gas to be desulfurized is sent to the middle part of the mixing reactor, the flue gas is sprayed upwards through uniformly distributed air nozzles, the filtered seawater is in countercurrent contact with the flue gas to be desulfurized, the contact area of the reaction is increased, and the reaction efficiency is improved. The flue gas to be desulfurized reacts with the filtered seawater, and sulfides in the flue gas to be desulfurized are absorbed by the filtered seawater.
Sulfide reacts with natural alkalinity in seawater, mainly HCO 3 - And CO 3 2- The reaction process is as follows:
SO 2 +H 2 O=H 2 SO 3
H 2 SO 3 =H + +HSO 3 -
HSO 3 - =H + +SO 4 2-
H + +HCO 3 - =CO 2 ↑+H 2 O
2H + +CO 3 2- =CO 2 ↑+H 2 O。
step 2: the desulfurized flue gas enters a heater, is heated to 50 ℃ and is discharged into the atmosphere. The higher flue gas temperature ensures that the flue gas is discharged from the chimney at enough lifting height, and prevents dew condensation corrosion on the inner wall of the chimney.
Step 3: the sea water absorbed with sulfide flows to the lower part of the mixing reactor, and Mg (OH) is added into the sea water absorbed with sulfide 2 . SO in flue gas 2 Sulfide and Mg (OH) remaining from natural alkalinity reaction in seawater 2 The reaction is continued, the process has higher desulfurization efficiency, and the reaction process is as follows:
H 2 SO 3 +Mg(OH) 2 =MgSO 3 +2H 2 O
MgSO 4 +H 2 SO 4 =Mg(HSO 4 ) 2
Mg(HSO 4 ) 2 +Mg(OH) 2 =2MgSO 4 +2H 2 O
2MgSO 3 +O 2 =2MgSO 4 。
sea water and Mg (OH) 2 After the reaction, measuring the salinity of the seawater, calculating the salinity increase rate of the seawater relative to the filtered seawater, and if the salinity increase rate exceeds 30%, discharging part of the reacted seawater, and adding the filtered seawater with a corresponding quantity until the salinity increase rate is not more than 30%. The filtered seawater is the same as the filtered seawater fed to the mixing reactor in step 1. If the salinity increase rate does not exceed 30%, the waste water is directly sent into the oxidation process chamber.
Step 4: will be with Mg (OH) 2 The reacted seawater is sent into an oxidation process chamber, air is filled into the oxidation process chamber through a compressed air pump, and MgSO in the seawater is carried out by oxygen in the air 3 All oxidized to MgSO 4 In the oxidation reaction process, the oxidation process chamber is kept in an acidic environment all the time, specifically, the pH value of the seawater is kept at 5-6, and the oxidation process chamber can be realized by adding sulfuric acid. The acidic environment causes Mg (OH) 2 The precipitate is completely dissolved for delivery to Mg (OH) in solution 2 In the regeneration chamber. The oxidation process chamber can be internally provided with a stirrer for breaking up large bubbles into small bubbles to accelerate the oxidation reaction and make the reaction proceed uniformly.
Step 5: the seawater after the oxidation reaction is conveyed to Mg (OH) 2 Regeneration chamber, then Ca (OH) is added 2 Mg (OH) produced 2 And (5) precipitation. Mg (OH) 2 The regeneration chamber is used for oxidizing MgSO conveyed in the process chamber 4 And Ca (OH) 2 Ca (OH) generated in the reaction chamber 2 Reaction to Mg (OH) 2 And the unreacted MgCl in the original seawater is treated 2 Mg (OH) is generated together 2 Precipitating, and refluxing to the mixing reactor to form a mixing reactor, an oxidation process chamber and Mg (OH) 2 Closed cycle of regeneration chamber, mg (OH) 2 The main reaction process of the regeneration chamber is as follows:
MgSO 4 +Ca(OH) 2 =Mg(OH) 2 ↓+CaSO 4 ·2H 2 O
MgCl 2 +Ca(OH) 2 =Mg(OH) 2 ↓+CaCl 2 。
Mg(OH) 2 a drain valve is arranged in the regeneration chamber and is used for mixing Ca (OH) 2 The part of the reacted seawater exceeding the set water level is automatically discharged.
Mg(OH) 2 Ca (OH) for regeneration Chamber 2 Calcium oxide and water in Ca (OH) 2 And (3) generating reaction in the reaction chamber, and transmitting heat generated in the reaction process to a heater through a heat conducting medium for heating the desulfurized flue gas in the step (2), so that the heat recovery and utilization efficiency is improved.
The present invention has been described in detail by way of examples, but the description is merely exemplary of the invention and should not be construed as limiting the scope of the invention. The scope of the invention is defined by the claims. In the technical scheme of the invention, or under the inspired by the technical scheme of the invention, similar technical schemes are designed to achieve the technical effects, or equivalent changes and improvements to the application scope are still included in the protection scope of the patent coverage of the invention.
Claims (7)
1. A flue gas desulfurization method for recycling seawater, comprising the steps of:
step 1: adding filtered seawater and flue gas to be desulfurized at 47-53 ℃ into a mixing reactor, reacting the flue gas to be desulfurized with the filtered seawater, and absorbing sulfide in the flue gas to be desulfurized by the filtered seawater;
step 2: the desulfurized flue gas enters a heater, is heated to 47-53 ℃ and is discharged into the atmosphere;
step 3: adding Mg (OH) into sea water absorbed with sulfide 2 ；
Step 4: feeding the reacted seawater into an oxidation process chamber, charging air into the oxidation process chamber, and using oxygen in the air to remove MgSO in the seawater 3 Oxidation to MgSO 4 Maintaining the oxidation process chamberFinally, an acidic environment is formed;
step 5: the seawater after the oxidation reaction is conveyed to Mg (OH) 2 Regeneration chamber, then Ca (OH) is added 2 To generate Mg (OH) 2 Precipitation, used in step 3; wherein Ca (OH) 2 Calcium oxide and water in Ca (OH) 2 And (3) generating reaction in a reaction chamber, wherein heat generated in the reaction process is used for heating the desulfurized flue gas in the step (2).
2. The flue gas desulfurization method of claim 1, wherein the filtered seawater is countercurrently contacted with the flue gas to be desulfurized in a mixing reactor.
3. The flue gas desulfurization method of seawater recirculation of claim 1, wherein the filtered seawater is seawater filtered of microorganisms and solid particulates.
4. The flue gas desulfurization method of seawater recirculation as claimed in claim 1, wherein in step 3, seawater and Mg (OH) 2 After the reaction, the salinity of the seawater is measured, the salinity increase rate of the seawater relative to the filtered seawater is calculated, if the salinity increase rate exceeds 30%, the partially reacted seawater is discharged, and the filtered seawater with the corresponding quantity is added.
5. The flue gas desulfurization method for recycling seawater according to claim 1, wherein the pH of the seawater is maintained at 5 to 6 in the oxidation process chamber by adding sulfuric acid.
6. The flue gas desulfurization method for recycling seawater according to claim 1, wherein a stirrer is provided in the oxidation process chamber for breaking up large bubbles into small bubbles to accelerate the oxidation reaction and make the reaction proceed uniformly.
7. A flue gas desulfurization process for recycling seawater according to claim 1, wherein Mg (OH) 2 A drain valve is arranged in the regeneration chamber and is used for mixing Ca (OH) 2 After the reactionThe part of the seawater exceeding the set water level is automatically discharged.
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Citations (5)
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| US4804523A (en) * | 1987-06-17 | 1989-02-14 | Bechtel Group, Incorporated | Use of seawater in flue gas desulfurization |
| CN101879406A (en) * | 2010-07-15 | 2010-11-10 | 煤炭工业济南设计研究院有限公司 | Dual-alkali flue gas desulfurization device and desulfurization method |
| CN102120138A (en) * | 2011-02-17 | 2011-07-13 | 大连海事大学 | Magnesium base-seawater method desulfurization system for ship |
| CN104959012A (en) * | 2015-04-17 | 2015-10-07 | 熊天渝 | Magnesium-calcium based wet method desulphurization system and method for removing sulfur dioxide in flue gas and producing gypsum |
| CN113893659A (en) * | 2021-11-13 | 2022-01-07 | 安徽恒夏环保科技有限公司 | High-sulfur flue gas treatment system and treatment method |
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2023
- 2023-05-09 CN CN202310513563.XA patent/CN116212635A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4804523A (en) * | 1987-06-17 | 1989-02-14 | Bechtel Group, Incorporated | Use of seawater in flue gas desulfurization |
| CN101879406A (en) * | 2010-07-15 | 2010-11-10 | 煤炭工业济南设计研究院有限公司 | Dual-alkali flue gas desulfurization device and desulfurization method |
| CN102120138A (en) * | 2011-02-17 | 2011-07-13 | 大连海事大学 | Magnesium base-seawater method desulfurization system for ship |
| CN104959012A (en) * | 2015-04-17 | 2015-10-07 | 熊天渝 | Magnesium-calcium based wet method desulphurization system and method for removing sulfur dioxide in flue gas and producing gypsum |
| CN113893659A (en) * | 2021-11-13 | 2022-01-07 | 安徽恒夏环保科技有限公司 | High-sulfur flue gas treatment system and treatment method |
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