CN111298627B - Flue gas desulfurization system and method - Google Patents
Flue gas desulfurization system and method Download PDFInfo
- Publication number
- CN111298627B CN111298627B CN201911286375.8A CN201911286375A CN111298627B CN 111298627 B CN111298627 B CN 111298627B CN 201911286375 A CN201911286375 A CN 201911286375A CN 111298627 B CN111298627 B CN 111298627B
- Authority
- CN
- China
- Prior art keywords
- absorption tower
- slurry
- alkali
- sodium
- absorption
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000034 method Methods 0.000 title claims abstract description 44
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 239000003546 flue gas Substances 0.000 title claims abstract description 29
- 238000006477 desulfuration reaction Methods 0.000 title abstract description 13
- 230000023556 desulfurization Effects 0.000 title abstract description 13
- 239000003513 alkali Substances 0.000 claims abstract description 93
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims abstract description 91
- 238000002425 crystallisation Methods 0.000 claims abstract description 75
- 230000008025 crystallization Effects 0.000 claims abstract description 74
- 239000007788 liquid Substances 0.000 claims abstract description 61
- 235000010265 sodium sulphite Nutrition 0.000 claims abstract description 45
- 239000011734 sodium Substances 0.000 claims abstract description 12
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 12
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims abstract description 10
- 238000010521 absorption reaction Methods 0.000 claims description 142
- 239000002002 slurry Substances 0.000 claims description 89
- 239000012452 mother liquor Substances 0.000 claims description 36
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 35
- 238000001704 evaporation Methods 0.000 claims description 35
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical group [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 34
- 230000008020 evaporation Effects 0.000 claims description 34
- 238000006386 neutralization reaction Methods 0.000 claims description 32
- XONPDZSGENTBNJ-UHFFFAOYSA-N molecular hydrogen;sodium Chemical compound [Na].[H][H] XONPDZSGENTBNJ-UHFFFAOYSA-N 0.000 claims description 25
- 238000003756 stirring Methods 0.000 claims description 23
- 239000007787 solid Substances 0.000 claims description 19
- 230000003472 neutralizing effect Effects 0.000 claims description 14
- 239000006096 absorbing agent Substances 0.000 claims description 13
- 239000007789 gas Substances 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 235000017550 sodium carbonate Nutrition 0.000 claims description 9
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 9
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 8
- 239000007790 solid phase Substances 0.000 claims description 8
- 239000011593 sulfur Substances 0.000 claims description 8
- 229910052717 sulfur Inorganic materials 0.000 claims description 8
- 239000000243 solution Substances 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 5
- 230000001186 cumulative effect Effects 0.000 claims description 4
- 238000005191 phase separation Methods 0.000 claims description 4
- 238000002347 injection Methods 0.000 claims description 3
- 239000007924 injection Substances 0.000 claims description 3
- 230000002093 peripheral effect Effects 0.000 claims description 2
- 230000003009 desulfurizing effect Effects 0.000 claims 1
- 239000000047 product Substances 0.000 abstract description 15
- 239000006227 byproduct Substances 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 5
- HRZFUMHJMZEROT-UHFFFAOYSA-L sodium disulfite Chemical compound [Na+].[Na+].[O-]S(=O)S([O-])(=O)=O HRZFUMHJMZEROT-UHFFFAOYSA-L 0.000 abstract description 5
- 235000010262 sodium metabisulphite Nutrition 0.000 abstract description 5
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 229940001584 sodium metabisulfite Drugs 0.000 abstract description 4
- 229910052938 sodium sulfate Inorganic materials 0.000 abstract description 3
- 235000011152 sodium sulphate Nutrition 0.000 abstract description 3
- 239000002910 solid waste Substances 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 abstract 1
- 230000002745 absorbent Effects 0.000 abstract 1
- 239000002250 absorbent Substances 0.000 abstract 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 12
- 238000004519 manufacturing process Methods 0.000 description 7
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 239000002245 particle Substances 0.000 description 3
- 239000013078 crystal Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- AKHNMLFCWUSKQB-UHFFFAOYSA-L sodium thiosulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=S AKHNMLFCWUSKQB-UHFFFAOYSA-L 0.000 description 2
- 235000019345 sodium thiosulphate Nutrition 0.000 description 2
- PQUCIEFHOVEZAU-UHFFFAOYSA-N Diammonium sulfite Chemical compound [NH4+].[NH4+].[O-]S([O-])=O PQUCIEFHOVEZAU-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- RWPGFSMJFRPDDP-UHFFFAOYSA-L potassium metabisulfite Chemical compound [K+].[K+].[O-]S(=O)S([O-])(=O)=O RWPGFSMJFRPDDP-UHFFFAOYSA-L 0.000 description 1
- 229940043349 potassium metabisulfite Drugs 0.000 description 1
- 235000010263 potassium metabisulphite Nutrition 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical class [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Images
Classifications
-
- 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
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/16—Purification
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/18—Dehydration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Biomedical Technology (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Materials Engineering (AREA)
- Inorganic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Treating Waste Gases (AREA)
Abstract
A flue gas desulfurization system and a method belong to the field of chemical industry. The method adopts sodium alkali as an absorbent to produce sulfate as a byproduct, the purity of a main product is controllable, typical byproducts such as sodium sulfate, sodium sulfite, sodium metabisulfite and the like belong to a large number of commodities in the market, the sodium sulfate, the sodium sulfite, the sodium metabisulfite and the like are easy to enter the commodity market, no solid waste or waste liquid is generated, and the environment-friendly benefit is good. Through reasonable process layout, the evaporative crystallization system can be bypassed intermittently to directly produce sodium sulfite, the steam consumption can be saved by 20-50% under the same working medium, and meanwhile, the novel evaporative crystallizer is adopted, so that the operation flexibility of the evaporative crystallization system is improved, and the industrial problem of high energy consumption of frequently starting and stopping the evaporative crystallization system is solved.
Description
Technical Field
The invention relates to the field of chemical devices, in particular to a flue gas desulfurization system and a flue gas desulfurization method.
Background
Sulfite is an important reducing agent, and common industrial sulfite includes sodium metabisulfite, sodium sulfite, ammonium sulfite, sodium thiosulfate, potassium metabisulfite and the like, wherein sodium sulfite is the most easily obtained product in the production of the sulfite. In order to control the index of free alkali, the traditional sodium sulfite production process involves evaporation, concentration and crystallization, and has the advantages of higher energy consumption per unit product, high production cost and relatively lower market competitiveness of sodium sulfite compared with other sulfites of the same family.
Meanwhile, the production processes of sodium sulfite, sodium metabisulfite and sodium thiosulfate of the same family are different, the particle size of sodium sulfite crystal particles obtained by most evaporative crystallization systems is relatively small, after the slurry enters a centrifugal machine, the separation efficiency of liquid and solid phases is low, and in order to reduce the production cost, measures for efficient concentration are often adopted, the relative density of the sodium sulfite slurry is concentrated to 1.72-1.95 through evaporative crystallization, but the process pipeline is frequently blocked, so that the stable production is not facilitated.
Disclosure of Invention
The invention provides a flue gas desulfurization system and a flue gas desulfurization method aiming at the existing technical problems.
The purpose of the invention can be realized by the following technical scheme:
a kind of flue gas desulfurization system, this system includes absorption tower, slurry conditioner, evaporation crystallization chamber and lye tank, the said absorption tower is divided into lower section of absorption tower and upper section of absorption section, there are Venturi absorbers and links with it in the lower section of absorption tower, the bottom of the said absorption tower links with sodium hydrogen tank, the output end of the said sodium hydrogen tank links with slurry conditioner through linking with slurry conditioner, the said slurry conditioner links with mother liquor tank through the centrifuge, the output end of the said mother liquor tank links with evaporation crystallization chamber and/or upper section of absorption section and/or lye tank, the bottom of the said evaporation crystallization chamber links with top input end of the slurry conditioner; and the output end of the alkali liquor tank is connected with the upper section of the absorption section and the upper part of the slurry conditioner.
The technical scheme of the invention is as follows: the center of this evaporation crystallization chamber is equipped with the agitator pivot, and the bottom of agitator pivot is equipped with the stirring rake, and preferred is anchor stirring rake, and the upper portion of evaporation crystallization chamber is equipped with the clear and turbid liquid separator, still be equipped with circulation thick liquid feed back pipe in the evaporation crystallization chamber, the export of circulation thick liquid feed back pipe passes through the heater and links to each other with the circulation thick liquid inlet pipe that is located clear and turbid liquid separator lower part.
The technical scheme of the invention is as follows: the lower periphery of the circulating slurry return pipe is provided with a baffle.
The technical scheme of the invention is as follows: the distance between the stirring paddle and the bottom of the evaporative crystallization chamber is controlled to be 2-20 cm, and the preferable distance is 5-8 cm. The circulating slurry return pipe is coaxial with the rotating shaft of the stirrer after entering the evaporative crystallization chamber and extends downwards to the upper edge of the anchor type stirring paddle; preferably, the height of the anchor type stirring paddle is 10-20 cm.
The circulating slurry return pipe is provided with a baffle, the horizontal inclination angle of the baffle is 1.1-1.5 times of the material repose angle, and the ratio of the vertical projection area of the baffle to the cross sectional area of the evaporation crystallization chamber on the same horizontal plane is 0.4-0.8.
The technical scheme of the invention is as follows: the gas output end at the top of the evaporation crystallization chamber is connected with an alkali liquor tank, the top of the alkali liquor tank is provided with an alkali bin connected with the alkali bin, and the output end at the bottom of the alkali liquor tank is connected with a slurry conditioner.
The technical scheme of the invention is as follows: one liquid output end of the lower section of the absorption tower is connected with the Venturi absorber through a primary absorption pump, the other liquid output end of the lower section of the absorption tower is connected with the upper part of the lower section of the absorption tower through a secondary absorption pump, and the liquid output end of the bottom of the upper section of the absorption section is connected with the middle part of the upper section of the absorption section through a tertiary absorption pump.
A method for realizing flue gas desulfurization by using the system comprises the following steps:
1) the sulfur-containing flue gas is absorbed with absorption liquid conveyed from the lower section of the absorption tower in the Venturi absorber and then enters the lower part of the absorption tower, then the countercurrent absorption is continued in the lower section of the absorption tower and the upper section of the absorption tower, and the absorbed tail gas leaves the system from the top of the absorption tower; conveying the alkali liquor in the alkali liquor tank to the upper section of the absorption section, conveying the absorption liquid of the upper section of the absorption section for absorbing the flue gas to the lower section of the absorption tower, and transferring the absorption liquid of the lower section of the absorption tower for absorbing the flue gas to a sodium hydrogen tank;
2) conveying the solution in the sodium hydrogen tank to a slurry conditioner for neutralization, wherein the neutralization reaction is carried out according to the following steps:
a. neutralizing with solid soda: the adding amount of alkali per minute is less than 3.0 percent of the stoichiometric ratio of theoretical complete neutralization, when the adding amount of alkali per minute reaches 50 to 65 percent of the stoichiometric ratio of the neutralization reaction, the adding amount of alkali per minute is adjusted to be less than 1.2 percent of the stoichiometric ratio of theoretical complete neutralization, and when the adding amount of soda reaches 65 to 73 percent of the stoichiometric ratio of the neutralization reaction, solid soda is stopped being added;
b. neutralizing with soda ash slurry: continuously neutralizing with sodium alkali slurry with the relative density of 1.16-1.42, wherein the sodium alkali addition per minute is less than 0.8% of the theoretical total alkali addition for complete neutralization, and stopping adding alkali until the cumulative alkali addition reaches 100% -103% of the stoichiometric coefficient;
c. and (4) continuously stirring for 4-72 hours to complete the neutralization reaction.
3) Sending the slurry neutralized in the step 2) into a centrifuge for liquid-solid separation, wherein the separated solid-phase product is the target product of wet sodium sulfite; and (3) feeding the separated mother liquor into a mother liquor tank, and opening an evaporative crystallization chamber for evaporative crystallization when the solid content in the mother liquor is more than 8-10%.
The method comprises the following steps: the steps of evaporative crystallization are as follows:
the first step is as follows: transferring sodium sulfite alkali liquor in the mother liquor tank to an evaporation crystallization chamber, and maintaining the liquid level of the evaporation crystallization chamber at 1/2 position of a clear-turbid liquid separator;
the second step is that: injecting process water into an inlet of a sodium sulfite circulating pump, wherein the injection amount of the process water is 0.3-2 times of the volume of a pipeline between the sodium sulfite circulating pump and the clear-and-turbid liquid separator, and then starting the sodium sulfite circulating pump according to a starting step of the sodium sulfite circulating pump;
the third step: turning on a heater, concentrating and crystallizing the slurry, and controlling the liquid level of an evaporative crystallization chamber to be at 1/2 position of a clear-turbid liquid separator by a mother liquid pump in the process;
the fourth step: and when the relative density of the slurry in the evaporation crystallization chamber reaches 1.45-1.75, transferring the slurry in the evaporation crystallization chamber to a slurry conditioner by a sodium sulfite pump, and performing liquid-solid phase separation by a centrifuge.
The method comprises the following steps: the alkali liquor in the step 1) is a sodium hydroxide solution or a sodium carbonate solution, and the relative density of the alkali liquor is 1.0-1.5.
The method comprises the following steps: when the pH value of the slurry at the upper section of the absorption tower is reduced to 7.6-8.0, transferring the slurry at the upper section of the absorption tower to the lower section (101) of the absorption tower, wherein the reduced liquid level at the upper section of the absorption tower is supplemented by a mother liquor tank or an alkali liquor tank; and transferring the lower section of the absorption tower to a sodium hydrogen tank when the pH value of the lower section of the absorption tower is reduced to 4.6-7.0, wherein the reduced liquid level of the lower section of the absorption tower is supplemented by an upper section of the absorption tower or a mother liquor tank or an alkali liquor tank.
The method comprises the following steps: and stirring by using a stirrer in the solid soda slurry neutralization process, wherein the stirring speed is 35-45 r/min, stirring by using the stirrer in the soda slurry neutralization process is 28-33 r/min, and stirring speed after the soda slurry neutralization is 24-30 r/min.
The invention has the beneficial effects that:
the invention can realize the resource utilization of sulfur dioxide gas, can utilize low-concentration sulfur dioxide and byproduct high-quality sulfite, reduces environmental pollution and realizes certain economic benefit;
secondly, a target product can be directly centrifugally separated, under the same process working medium, the steam consumption of a unit product is less than 0.5-0.8 t/t, the steam consumption of the sodium sulfite by the current two-effect evaporation crystallization method is 1.6-2.3 t/t, and the details are shown in the following table.
Thirdly, sodium alkali is used as a desulfurizer, and possible byproducts comprise sodium sulfate, sodium sulfite, sodium pyrosulfite and the like, which belong to large commodities in the market, have obvious economic benefit and do not generate solid waste;
and fourthly, the evaporative crystallization system is reasonably used, redundant water in the system can be balanced, and no waste water or waste liquid is generated.
The operation flexibility of evaporative crystallization is strong, and the operation of starting and stopping the evaporative circulation pump in a short time can be realized.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention;
FIG. 2 is a schematic view of the structure of an evaporative crystallization apparatus according to the present invention;
in the figure, 1. an absorption tower; 2. a sodium hydrogen tank; 3. a slurry conditioner; 4. a mother liquor tank; 5. evaporating the crystallization chamber; 6, a heater; 7. a steam condenser; 8. an alkali liquor tank; 9. an alkali bin; 101, the lower section of the absorption tower; 102. a venturi absorber; 103. an absorption section II section; 201. a primary absorption pump; 202. a secondary absorption pump; 203. a tertiary absorption pump; 204. a sodium hydrogen pump; 205 a mother liquor pump; 206 sodium sulfite pump; 207 an evaporation crystallization circulating pump; 208 a lye pump; 301 a stirrer; 302. a centrifuge; 401. a sulfur-containing gas; 402. tail gas; 403. wet sodium sulfite; 404. soda ash; 405. process water; 501, rotating a stirrer rotating shaft; 502. a circulating slurry return pipe; 503. a clear and turbid liquid separator; 504 circulating slurry feed pipe; 505. a baffle plate; 506. an anchor type stirring paddle; 507. a discharge outlet; 508. a feed inlet; 509 exhaust port.
Detailed Description
The invention is further illustrated by the following examples, without limiting the scope of the invention:
as shown in fig. 1-2, a flue gas desulfurization system comprises an absorption tower 1, a slurry conditioner 3, an evaporative crystallization chamber 5 and an alkali liquor tank 8, wherein the absorption tower is divided into an absorption tower lower section 101 and an absorption section upper section 103, the absorption tower lower section 101 is further provided with a venturi absorber 102 connected thereto, the bottom end of the absorption tower 1 is connected with a sodium hydrogen tank 2, the output end of the sodium hydrogen tank 2 is connected with the slurry conditioner 3 through a sodium hydrogen pump 204, a stirrer 301 is arranged in the slurry conditioner 3, the slurry conditioner 3 is connected with a mother liquor tank 4 through a centrifuge 302, the output end of the mother liquor tank 4 is connected with the evaporative crystallization chamber 5 and/or the absorption section upper section 103 and/or the alkali liquor tank (8) through a mother liquor pump 205, and the bottom end of the evaporative crystallization chamber 5 is connected with the top input end of the slurry conditioner 3 through a sodium sulfite pump 206; the output end of the lye tank is connected with the upper section 103 of the absorption section and the upper part of the slurry conditioner 3.
The center of the evaporative crystallization chamber 5 is provided with a stirrer rotating shaft 501, the bottom end of the stirrer rotating shaft 501 is provided with an anchor type stirring paddle 506, the upper part of the evaporative crystallization chamber 5 is provided with a clear and turbid liquid separator 503, the evaporative crystallization chamber 5 is also internally provided with a circulating slurry return pipe 502, and the outlet of the circulating slurry return pipe 502 is connected with a circulating slurry feeding pipe 504 positioned at the lower part of the clear and turbid liquid separator 503 through a heater 6 and an evaporative crystallization circulating pump 207. A baffle 505 is arranged on the lower peripheral side of the circulating slurry return pipe 502. The distance between the anchor type stirring paddle and the bottom of the evaporative crystallization chamber is controlled to be 2-20 cm, and the preferable distance is 5-8 cm. The circulating slurry return pipe is coaxial with the rotating shaft of the stirrer after entering the evaporative crystallization chamber and extends downwards to the upper edge of the anchor type stirring paddle; preferably, the height of the anchor type stirring paddle is 10-20 cm.
The circulating slurry return pipe is provided with a baffle, the horizontal inclination angle of the baffle is 1.1-1.5 times of the material repose angle, and the ratio of the vertical projection area of the baffle to the cross sectional area of the evaporation crystallization chamber on the same horizontal plane is 0.4-0.8.
The output end of the gas at the top of the evaporative crystallization chamber 5 is connected with an alkali liquor tank 8 through a steam condenser 7, the top of the alkali liquor tank 8 is provided with an alkali bin 9 connected with the alkali liquor tank, and the output end at the bottom of the alkali liquor tank 8 is connected with the slurry conditioner 3.
One liquid output end of the lower section 101 of the absorption tower is connected with the Venturi absorber 102 through a first-stage absorption pump 201, the other liquid output end of the lower section 101 of the absorption tower is connected with the upper part of the lower section 101 of the absorption tower through a second-stage absorption pump 202, and the liquid output end of the bottom of the upper section 103 of the absorption tower is connected with the middle part of the upper section 103 of the absorption tower through a third-stage absorption pump 203.
The process of flue gas desulfurization by using the system comprises the following steps:
the sulfur-containing flue gas 401 is mixed with the alkali liquor output by the first-stage absorption pump 201 in the Venturi absorber 102, then enters the lower part of the absorption tower 1, and is absorbed by the alkali liquor output by the second-stage absorption pump 202 and the alkali liquor output by the third-stage absorption pump 203 in sequence, and then the tail gas 402 leaves the system from the top of the absorption tower. Sodium hydrogen slurry which is absorbed in the absorption tower and qualified is transferred into a sodium hydrogen tank 2 through overflow or a primary absorption pump or a secondary absorption pump, then transferred into a slurry conditioner 3 through a sodium hydrogen pump 204 and neutralized through sodium alkali, after the completely neutralized slurry is subjected to liquid-solid phase separation through a centrifuge 302, wet sodium sulfite 404 and sodium sulfite mother liquor which are target products are obtained, the mother liquor overflows to a mother liquor tank 4 through a potential difference mother liquor, the mother liquor in the mother liquor tank is conveyed to an absorption tower or an evaporative crystallization chamber 5 through a mother liquor pump 205, the mother liquor entering the evaporative crystallization chamber is forcedly disturbed through a stirrer 303 and an evaporative crystallization circulating pump 207, concentration and crystallization of the mother liquor are realized through a heater 6, the crystallized slurry is conveyed to the slurry conditioner through a sodium sulfite pump 206, and solid-liquid separation is realized through the centrifuge.
The secondary steam from the evaporation crystallization chamber is recycled with condensed water by a steam condenser 7, the condensed water overflows to an alkali liquor tank 8 to prepare alkali liquor again, and the prepared alkali liquor is conveyed to an absorption tower or a slurry conditioner by an alkali liquor pump.
The specific process is as follows:
example 1
A flue gas desulfurization byproduct sodium sulfite system using solid soda ash as a sodium source. The method mainly comprises the following steps:
alkali liquor preparation and gas absorption. The sulfur-containing flue gas enters the lower part of an absorption tower (1) after being absorbed by absorption liquid conveyed from the lower section (101) of the absorption tower in a venturi absorber (102), then the sulfur-containing flue gas continues to carry out countercurrent absorption in the lower section (101) of the absorption tower and the upper section (103) of the absorption tower, and the absorbed tail gas (402) leaves a system from the top of the absorption tower; conveying the alkali liquor in the alkali liquor tank to an upper section (103) of an absorption section, conveying absorption liquid of the upper section (103) of the absorption section for absorbing the flue gas to a lower section (101) of an absorption tower, and transferring the absorption liquid of the lower section (101) of the absorption tower for absorbing the flue gas to a sodium hydrogen tank (2);
sodium carbonate slurry with the relative density of 1.16-1.26 is prepared by using sodium carbonate and process water or evaporative crystallization condensate in an alkali liquor tank 8.
② preparing hydrogen-sodium slurry. Conveying the prepared alkali liquor to the upper section 103 of the absorption tower through an alkali liquor pump 208, transferring the slurry of the upper section of the absorption tower to the lower section 101 of the absorption tower when the pH value of the slurry of the upper section of the absorption tower is reduced to 7.6-8.0, and supplementing the liquid level reduced by the upper section of the absorption tower by a mother liquor pump 205 or the alkali liquor pump; when the pH value of the lower section of the absorption tower is reduced to 4.6-7.0, transferring the lower section of the absorption tower to a sodium hydrogen tank 2, wherein the reduced liquid level of the lower section of the absorption tower is supplemented by an upper section of the absorption tower or a mother liquor pump or an alkaline liquor pump; the slurry in the sodium hydrogen tank is conveyed to a slurry conditioner 3 by a sodium hydrogen pump for neutralization.
And thirdly, neutralizing the sodium hydrogen.
And I, neutralizing by using solid soda ash. Adjusting the rotating speed of a stirrer 301 of the slurry conditioner to 35-45 r/min, wherein the alkali addition amount per minute is less than 3.0% of the theoretical total neutralization alkali amount, adjusting the alkali addition amount per minute to less than 1.2% of the theoretical total neutralization alkali amount when the stoichiometric ratio reaches 50-58%, and stopping adding solid soda when the soda addition amount reaches 65-73% of the stoichiometric ratio of the neutralization reaction.
And II, neutralizing by using soda slurry. Adjusting the rotating speed of a stirrer of the slurry conditioner to 28-33 r/min, continuously neutralizing with sodium-alkali slurry with the relative density of 1.16-1.42, wherein the sodium-alkali addition per minute is less than 0.8% of the theoretical total alkali consumption, and stopping adding alkali until the cumulative alkali addition reaches 100% -103% of the stoichiometric coefficient.
And III, adjusting the rotating speed of a stirrer of the slurry conditioner to 24-30/min, and continuously stirring for 4-72 hours to complete the neutralization reaction.
And fourthly, separating the product. And (4) feeding the slurry obtained in the third step into a centrifuge 302 for liquid-solid separation, wherein a separated solid-phase product is the target product of the wet sodium sulfite 403, and the separated mother liquor enters a mother liquor tank 4.
Evaporation and crystallization of sodium sulfite. And (4) when the solid content of the mother liquor separated in the step (iv) is more than 8-10%, opening the evaporative crystallization chamber (5) for evaporative crystallization.
Transferring the sodium sulfite lye in the mother liquor tank to an evaporation crystallization chamber, and maintaining the liquid level of the evaporation crystallization chamber at the 1/2 position of a clear-turbid liquid separator 503.
And II, injecting process water into the pump inlet of the sodium sulfite circulating pump 207, wherein the injection amount of the process water is 0.3-2 times of the volume of a pipeline between the sodium sulfite circulating pump and the clear and turbid liquid separator, and then starting the sodium sulfite circulating pump according to the start-up step of the sodium sulfite circulating pump.
And III, turning on the heater 6 to concentrate and crystallize the slurry, wherein the liquid level in the evaporative crystallization chamber is controlled at the 1/2 position of the turbid-liquid separator 503 by a mother liquid pump in the process.
And IV, when the relative density of the slurry in the evaporation crystallization chamber reaches 1.45-1.75, transferring the slurry in the evaporation crystallization chamber to a slurry conditioner by a sodium sulfite pump, and performing liquid-solid phase separation by a centrifuge.
Example 2
A flue gas desulfurization by-product sodium sulfite system taking solid caustic soda flakes or sodium hydroxide powder as a sodium source. The method mainly comprises the following steps:
preparing alkali liquor. The sulfur-containing flue gas enters the lower part of an absorption tower (1) after being absorbed by absorption liquid conveyed from the lower section (101) of the absorption tower in a venturi absorber (102), then the sulfur-containing flue gas continues to carry out countercurrent absorption in the lower section (101) of the absorption tower and the upper section (103) of the absorption tower, and the absorbed tail gas (402) leaves a system from the top of the absorption tower; conveying the alkali liquor in the alkali liquor tank to an upper section (103) of an absorption section, conveying absorption liquid of the upper section (103) of the absorption section for absorbing the flue gas to a lower section (101) of an absorption tower, and transferring the absorption liquid of the lower section (101) of the absorption tower for absorbing the flue gas to a sodium hydrogen tank (2);
and (3) preparing the alkali liquor with the relative density of 1.32-1.41 in the alkali liquor tank 8 by using sodium hydroxide and process water or evaporative crystallization condensate.
② preparing hydrogen-sodium slurry. The same as in embodiment 1.
And thirdly, neutralizing the sodium hydrogen.
And I, neutralizing with solid sodium hydroxide. Adjusting the rotating speed of a stirrer 301 of the slurry conditioner to 35-45 r/min, wherein the alkali addition amount per minute is less than 3.0% of the theoretical total neutralization alkali amount, when the stoichiometric ratio reaches 55-65%, the alkali addition amount per minute is adjusted to less than 1.5% of the theoretical total neutralization alkali amount, and when the soda addition amount reaches 70-75% of the stoichiometric ratio of the neutralization reaction, the solid soda is stopped being reinforced.
And II, neutralizing with a sodium hydroxide solution. Adjusting the rotating speed of a stirrer of the slurry conditioner to 28-33 r/min, continuously neutralizing with sodium hydroxide with the relative density of 1.37-1.42, wherein the addition of sodium alkali per minute is less than 1.2% of the theoretical total alkali consumption for neutralization, and stopping adding alkali until the cumulative alkali addition reaches 100-102% of the stoichiometric coefficient.
And III, adjusting the rotating speed of a stirrer of the slurry conditioner to 24-30/min, and continuously stirring for 4-72 hours to complete the neutralization reaction.
And fourthly, separating the product. The same as in embodiment 1.
Evaporation and crystallization of sodium sulfite. The same as in embodiment 1.
And (3) performance detection:
1. quality: the median diameter of the sodium sulfite products in the embodiment 1 and the embodiment 2 of the invention is 50-80 μm, the quality meets the first-class product and the above requirements of HG/T2967-2010 Process anhydrous sodium sulfate,
2. energy consumption:
the invention has the greatest advantage that the product has a large proportion of crystals with particles larger than 10 microns and can directly separate out solids through centrifugation, thereby having low energy consumption. Compared with the conventional sodium sulfite production process, evaporative crystallization, such as single-effect evaporative crystallization or double-effect evaporative crystallization, is required.
Claims (6)
1. A method for desulfurizing flue gas, which is characterized in that: the method comprises the following steps:
1) the sulfur-containing flue gas is absorbed by absorption liquid conveyed from the lower section (101) of the absorption tower in a Venturi absorber (102) and then enters the lower part of the absorption tower (1), then the countercurrent absorption is continued in the lower section (101) of the absorption tower and the upper section (103) of the absorption tower, and the absorbed tail gas (402) leaves the system from the top of the absorption tower; conveying the alkali liquor in the alkali liquor tank to an upper section (103) of an absorption tower, conveying an absorption liquid of the upper section (103) of the absorption tower for absorbing the flue gas to a lower section (101) of the absorption tower, and transferring the absorption liquid of the lower section (101) of the absorption tower for absorbing the flue gas to a sodium hydrogen tank (2);
2) the solution in the sodium hydrogen tank (2) is conveyed to a slurry conditioner (3) for neutralization, and the neutralization reaction is carried out according to the following steps:
a. neutralizing with solid soda: the adding amount of alkali per minute is less than 3.0 percent of the stoichiometric ratio of theoretical complete neutralization, when the adding amount of alkali per minute reaches 50 to 65 percent of the stoichiometric ratio of the neutralization reaction, the adding amount of alkali per minute is adjusted to be less than 1.2 percent of the stoichiometric ratio of theoretical complete neutralization, and when the adding amount of soda reaches 65 to 73 percent of the stoichiometric ratio of the neutralization reaction, solid soda is stopped being added;
b. neutralizing with soda ash slurry: continuously neutralizing with sodium alkali slurry with the relative density of 1.16-1.42, wherein the sodium alkali addition per minute is less than 0.8% of the theoretical total alkali addition for complete neutralization, and stopping adding alkali until the cumulative alkali addition reaches 100% -103% of the stoichiometric coefficient;
c. continuously stirring for 4-72 h to complete the neutralization reaction;
3) sending the slurry neutralized in the step 2) into a centrifuge (302) for liquid-solid separation, and separating out a solid-phase product, namely a target product, namely wet sodium sulfite (403); the separated mother liquor enters a mother liquor tank (4), and when the solid content in the mother liquor is more than 8-10%, an evaporation crystallization chamber (5) needs to be opened for evaporation crystallization;
the system for realizing the method comprises an absorption tower (1), a slurry conditioner (3), an evaporative crystallization chamber (5) and an alkali liquor tank (8), wherein the absorption tower is divided into an absorption tower lower section (101) and an absorption tower upper section (103), the absorption tower lower section (101) is also provided with a Venturi absorber (102) connected with the Venturi absorber, the bottom end of the absorption tower (1) is connected with a sodium hydrogen tank (2), the output end of the sodium hydrogen tank (2) is connected with the slurry conditioner (3), the slurry conditioner (3) is connected with a mother liquor tank (4) through a centrifugal machine (302), the output end of the mother liquor tank (4) is connected with the evaporative crystallization chamber (5) and/or the absorption tower upper section (103) and/or the alkali liquor tank (8), and the bottom end of the evaporative crystallization chamber (5) is connected with the top input end of the slurry conditioner (3); the output end of the alkali liquor tank is connected with the upper section (103) of the absorption tower and the upper part of the slurry conditioner (3);
wherein: when the pH value of the slurry at the upper section of the absorption tower is reduced to 7.6-8.0, transferring the slurry at the upper section of the absorption tower to the lower section (101) of the absorption tower, wherein the reduced liquid level at the upper section of the absorption tower is supplemented by a mother liquor tank or an alkali liquor tank; when the pH value of the slurry at the lower section of the absorption tower is reduced to 4.6-7.0, transferring the slurry at the lower section of the absorption tower to a sodium hydrogen tank (2), wherein the reduced liquid level at the lower section of the absorption tower is supplemented by an upper section of the absorption tower or a mother liquor tank or an alkali liquor tank, the alkali liquor is a sodium hydroxide solution or a sodium carbonate solution, and the relative density of the alkali liquor is 1.0-1.5;
wherein: the steps of evaporative crystallization are as follows:
the first step is as follows: transferring sodium sulfite alkali liquor in the mother liquor tank to an evaporation crystallization chamber, and maintaining the liquid level of the evaporation crystallization chamber at the 1/2 position of a clear-turbid liquid separator (503);
the second step is that: injecting process water into a pump inlet of a sodium sulfite circulating pump (207), wherein the injection amount of the process water is 0.3-2 times of the volume of a pipeline between the sodium sulfite circulating pump and a clear-and-turbid liquid separator, and then starting the sodium sulfite circulating pump according to a starting step of the sodium sulfite circulating pump;
the third step: turning on a heater (6), concentrating and crystallizing the slurry, and controlling the liquid level of the evaporation crystallization chamber to be at the 1/2 position of the clear and turbid liquid separator (503) by a mother liquid pump in the process;
the fourth step: and when the relative density of the slurry in the evaporation crystallization chamber reaches 1.45-1.75, transferring the slurry in the evaporation crystallization chamber to a slurry conditioner by a sodium sulfite pump, and performing liquid-solid phase separation by a centrifuge.
2. The method of claim 1, wherein: and stirring by using a stirrer in the solid soda slurry neutralization process, wherein the stirring speed is 35-45 r/min, stirring by using the stirrer in the soda slurry neutralization process is 28-33 r/min, and stirring speed after the soda slurry neutralization is 24-30 r/min.
3. The method of claim 1, wherein: the center of this evaporation crystallization room (5) is equipped with agitator pivot (501), and the bottom of agitator pivot (501) is equipped with anchor stirring rake (506), and the upper portion of evaporation crystallization room (5) is equipped with clear turbid liquid separator (503), still be equipped with circulation thick liquid feed back pipe (502) in evaporation crystallization room (5), the export of circulation thick liquid feed back pipe (502) is passed through heater (6) and is linked to each other with circulation thick liquid inlet pipe (504) that are located clear turbid liquid separator (503) lower part.
4. The method of claim 1, wherein: a baffle plate (505) is arranged on the lower peripheral side of the circulating slurry return pipe (502).
5. The method of claim 1, wherein: the gas output end at the top of the evaporation crystallization chamber (5) is connected with an alkali liquor tank (8), the top of the alkali liquor tank (8) is provided with an alkali bin (9) connected with the alkali liquor tank, and the output end at the bottom of the alkali liquor tank (8) is connected with a slurry conditioner (3).
6. The method of claim 1, wherein: one liquid output end of the lower section (101) of the absorption tower is connected with the Venturi absorber (102) through a first-stage absorption pump (201), the other liquid output end of the lower section (101) of the absorption tower is connected with the upper part of the lower section (101) of the absorption tower through a second-stage absorption pump (202), and the liquid output end of the bottom of the upper section (103) of the absorption tower is connected with the middle part of the upper section (103) of the absorption tower through a third-stage absorption pump (203).
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911286375.8A CN111298627B (en) | 2019-12-13 | 2019-12-13 | Flue gas desulfurization system and method |
| PCT/CN2020/089517 WO2021114563A1 (en) | 2019-12-13 | 2020-05-10 | Flue gas desulfurization system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911286375.8A CN111298627B (en) | 2019-12-13 | 2019-12-13 | Flue gas desulfurization system and method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN111298627A CN111298627A (en) | 2020-06-19 |
| CN111298627B true CN111298627B (en) | 2021-07-20 |
Family
ID=71154435
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911286375.8A Active CN111298627B (en) | 2019-12-13 | 2019-12-13 | Flue gas desulfurization system and method |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN111298627B (en) |
| WO (1) | WO2021114563A1 (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103977689A (en) * | 2014-05-30 | 2014-08-13 | 陕西智惠环保科技有限公司 | Device and method for removing sulfur dioxide in smoke by two-step alkalifying reproducing and sodium sulfite method |
| CN206955655U (en) * | 2017-03-28 | 2018-02-02 | 黄河三角洲京博化工研究院有限公司 | A kind of reactor that sodium sulfite is produced using sulfur dioxide in tail gas |
| CN109316964A (en) * | 2018-11-15 | 2019-02-12 | 中石化炼化工程（集团）股份有限公司 | A kind of method of catalytic cracking flue gas desulfurization recycling sodium sulfite |
| CN110255585A (en) * | 2019-07-10 | 2019-09-20 | 南京工业大学 | Device and method for preparing sulfite |
| CN110433637A (en) * | 2019-07-30 | 2019-11-12 | 大连汉诺工程技术有限公司 | A kind of Method of Soda flue gas desulfurization device and technique |
| CN211635911U (en) * | 2019-12-13 | 2020-10-09 | 南京工业大学 | Flue gas desulfurization system |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4207299A (en) * | 1977-02-16 | 1980-06-10 | Davy Powergas, Inc. | Sulphur dioxide removal process |
| JPS593209B2 (en) * | 1978-06-21 | 1984-01-23 | 日鉄化工機株式会社 | Post-treatment method for desulfurization absorption liquid |
| JP3004531B2 (en) * | 1994-04-19 | 2000-01-31 | 三菱重工業株式会社 | Method and apparatus for desulfurizing low-concentration sulfurous acid gas |
| CN101332409A (en) * | 2008-08-05 | 2008-12-31 | 北京博奇电力科技有限公司 | Flue-gas desulfurization system and method capable of reutilizing desulfurization by-products |
| CN102160960A (en) * | 2011-02-25 | 2011-08-24 | 中冶华天工程技术有限公司 | Soda wet desulphurization process and system for sintering flue gas |
| CN103736383B (en) * | 2014-01-17 | 2015-12-02 | 长沙有色冶金设计研究院有限公司 | Soda ash flue gas desulfurization technique and flue gas desulphurization system |
| CN107648948A (en) * | 2017-11-13 | 2018-02-02 | 中钢集团天澄环保科技股份有限公司 | A kind of catalytic cracking flue gas dust-removal and desulfurizing reclaims sodium sulfite technique |
| CN108079762B (en) * | 2018-01-30 | 2020-07-24 | 中石化南京工程有限公司 | Flue gas desulfurization system and method for flue gas desulfurization by using same |
-
2019
- 2019-12-13 CN CN201911286375.8A patent/CN111298627B/en active Active
-
2020
- 2020-05-10 WO PCT/CN2020/089517 patent/WO2021114563A1/en active Application Filing
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103977689A (en) * | 2014-05-30 | 2014-08-13 | 陕西智惠环保科技有限公司 | Device and method for removing sulfur dioxide in smoke by two-step alkalifying reproducing and sodium sulfite method |
| CN206955655U (en) * | 2017-03-28 | 2018-02-02 | 黄河三角洲京博化工研究院有限公司 | A kind of reactor that sodium sulfite is produced using sulfur dioxide in tail gas |
| CN109316964A (en) * | 2018-11-15 | 2019-02-12 | 中石化炼化工程（集团）股份有限公司 | A kind of method of catalytic cracking flue gas desulfurization recycling sodium sulfite |
| CN110255585A (en) * | 2019-07-10 | 2019-09-20 | 南京工业大学 | Device and method for preparing sulfite |
| CN110433637A (en) * | 2019-07-30 | 2019-11-12 | 大连汉诺工程技术有限公司 | A kind of Method of Soda flue gas desulfurization device and technique |
| CN211635911U (en) * | 2019-12-13 | 2020-10-09 | 南京工业大学 | Flue gas desulfurization system |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2021114563A1 (en) | 2021-06-17 |
| CN111298627A (en) | 2020-06-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2021004122A1 (en) | Device and method for preparing sulfite | |
| CN103570043B (en) | Method for producing high-purity potassium chloride solution for preparation of potassium carbonate and co-producing low sodium salt | |
| CN107758962A (en) | A kind of system of the preparing magnesium sulfate from desulfurization wastewater | |
| CN211635911U (en) | Flue gas desulfurization system | |
| CN103588230A (en) | Magnesium sulfate preparation system | |
| CN111003717B (en) | Method for preparing alkali salt by evaporating and crystallizing sea water desalination strong brine | |
| CN102515112B (en) | Method for preparing sodium sulfide from hydrogen sulfide waste gas produced in production of viscose fibre | |
| CN102275955B (en) | Method for preparing mirabilite by using sulfonated end gas absorption solution, and apparatus thereof | |
| CN108328839A (en) | A kind of sodium alkali flue gas desulfurization wastewater treatment system and application method | |
| CN111298627B (en) | Flue gas desulfurization system and method | |
| CN102730879B (en) | A kind of method of continuous preparation essence halogen | |
| CN112279277A (en) | System and method for high-end resource utilization of flue gas desulfurization by magnesium method | |
| CN112357939A (en) | Method for preparing magnesium hydroxide and calcium chloride by treating desulfurization wastewater of coal-fired power plant | |
| CN115159753B (en) | Zero discharge system for magnesium desulfurization wastewater and treatment method thereof | |
| CN219489757U (en) | Desulfurization waste water treatment device for coal-fired power plant | |
| CN212425465U (en) | Reaction crystallization equipment for extracting sodium sulfite product by sodium desulfurization post-treatment | |
| CN215439698U (en) | Device of resourceful treatment sodium sulfate waste liquid | |
| CN114455612B (en) | Process for preparing sodium carbonate byproduct gypsum by using sodium sulfate and carbon dioxide as raw materials | |
| CN206955655U (en) | A kind of reactor that sodium sulfite is produced using sulfur dioxide in tail gas | |
| CN216226123U (en) | Sodium-based dry-method desulfurized fly ash resource utilization device | |
| CN109095483A (en) | A kind of system and its application method of oxalate precipitation method recycling power plant desulfurization wastewater calcium and magnesium | |
| CN111320762B (en) | System and process for preparing acid-out lignin and sodium lignosulfonate from pulping black liquor | |
| CN210419274U (en) | Device for preparing sulfite | |
| CN218530906U (en) | Low-concentration carbon dioxide absorbs system calcium carbonate three-phase fluidized bed system | |
| CN214087744U (en) | Device for concentrating and recovering magnesium sulfate heptahydrate from wet magnesium oxide desulfurization waste liquid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB03 | Change of inventor or designer information | ||
| CB03 | Change of inventor or designer information |
Inventor after: Xu Haitao Inventor after: Xu Yanzhong Inventor after: Li Mingbo Inventor after: Chen Renyuan Inventor after: Liu Dahua Inventor after: Wu Zhenshan Inventor after: Song Jing Inventor after: Xu Meng Inventor before: Xu Haitao Inventor before: Xu Yanzhong Inventor before: Li Mingbo |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |