CN107032547A - A kind of SO3Removing and the charging integrated apparatus and method of desulfurization wastewater zero-emission - Google Patents
A kind of SO3Removing and the charging integrated apparatus and method of desulfurization wastewater zero-emission Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 77
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 60
- 230000023556 desulfurization Effects 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 63
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims abstract description 57
- 229910000029 sodium carbonate Inorganic materials 0.000 claims abstract description 51
- 239000000243 solution Substances 0.000 claims abstract description 47
- 239000012528 membrane Substances 0.000 claims abstract description 40
- 239000007921 spray Substances 0.000 claims abstract description 39
- 239000013505 freshwater Substances 0.000 claims abstract description 34
- 239000003546 flue gas Substances 0.000 claims abstract description 25
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 25
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 24
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000004062 sedimentation Methods 0.000 claims abstract description 22
- 239000002250 absorbent Substances 0.000 claims abstract description 20
- 239000010802 sludge Substances 0.000 claims abstract description 20
- 238000005352 clarification Methods 0.000 claims abstract description 18
- 238000001704 evaporation Methods 0.000 claims abstract description 17
- 239000012530 fluid Substances 0.000 claims abstract description 16
- 230000008020 evaporation Effects 0.000 claims abstract description 14
- 238000002347 injection Methods 0.000 claims abstract description 9
- 239000007924 injection Substances 0.000 claims abstract description 9
- 238000002156 mixing Methods 0.000 claims abstract description 8
- 239000003513 alkali Substances 0.000 claims description 37
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Inorganic materials O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 claims description 37
- 239000007788 liquid Substances 0.000 claims description 30
- 239000011734 sodium Substances 0.000 claims description 25
- 239000012535 impurity Substances 0.000 claims description 18
- 230000002745 absorbent Effects 0.000 claims description 17
- 238000002360 preparation method Methods 0.000 claims description 12
- 239000008394 flocculating agent Substances 0.000 claims description 10
- 238000010790 dilution Methods 0.000 claims description 9
- 239000012895 dilution Substances 0.000 claims description 9
- 239000000706 filtrate Substances 0.000 claims description 9
- 238000000889 atomisation Methods 0.000 claims description 8
- 238000005507 spraying Methods 0.000 claims description 8
- 238000004140 cleaning Methods 0.000 claims description 6
- 235000017550 sodium carbonate Nutrition 0.000 claims description 6
- 239000011550 stock solution Substances 0.000 claims description 6
- 239000008235 industrial water Substances 0.000 claims description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 4
- 238000010521 absorption reaction Methods 0.000 claims description 3
- 229920006221 acetate fiber Polymers 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 239000002131 composite material Substances 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 239000006228 supernatant Substances 0.000 claims description 3
- 239000011780 sodium chloride Substances 0.000 claims description 2
- 238000003795 desorption Methods 0.000 claims 7
- 230000000694 effects Effects 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 238000007781 pre-processing Methods 0.000 abstract 1
- 208000028659 discharge Diseases 0.000 description 35
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 18
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 18
- 238000005516 engineering process Methods 0.000 description 8
- 239000003344 environmental pollutant Substances 0.000 description 5
- 231100000719 pollutant Toxicity 0.000 description 5
- 238000003756 stirring Methods 0.000 description 4
- 238000002425 crystallisation Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000000843 powder Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000011278 co-treatment Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- B01D53/14—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 by absorption
- B01D53/1456—Removing acid components
- B01D53/1481—Removing sulfur dioxide or sulfur trioxide
-
- 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
- B01D53/14—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 by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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
- B01D53/14—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 by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
-
- 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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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
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- C02F2001/007—Processes including a sedimentation step
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- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
- C02F2201/007—Modular design
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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Abstract
The invention provides a kind of SO3Removing and desulfurization wastewater zero-emission integrated apparatus and method, technique include：SO3Absorbent prepares part I, desulfurization wastewater zero-emission preprocessing part II, solution measures distribution portion III and injection evaporation section IV, specifically includes Na2CO3Dissolving tank 1, Na2CO3Fluid reservoir 21, fresh-water tank 22, online pipe-line mixer 23, concentrated water case 24, mixing dosing tank 3, clarification sedimentation basin 4, ultrafiltration apparatus 5, reverse osmosis membrane group 6, spray gun 7, sludge delivery pump 8, plate and frame filter press 9, coarse filter 14 and various pumps 10, flowmeter 11, pressure gauge 12 and valve 13.This technique is to SO3Removing and the process of wastewater zero discharge two carry out integrated design, and SO in power-plant flue gas can be realized simultaneously3Removing and desulfurization wastewater zero-emission, technical process is simple, energy consumption is relatively low, can reach preferable treatment effect.
Description
Technical Field
The invention belongs to the field of flue gas purification of coal-fired boilers, relates to a pollutant co-treatment system based on a wastewater zero discharge technology, and provides a SO (sulfur oxide) system3A device and a method for integrating removal and zero discharge of desulfurization waste water.
Background
The coal-fired power plant is an important component of a power system in China, and discharges a large amount of gas, liquid and solid pollutants in the operation process. As various pollutant treatment technologies and equipment become mature, the pollutant emission requirements become more stringent. In the flue gas, SO3The zero discharge of the removal and desulfurization waste water is of great concern.
SO3The removal technology can be divided into a wet method and a dry method, and the removal technology is achieved by spraying an alkaline absorbent into a flueTo remove SO from flue gas3The purpose of (1). The commonly used wastewater zero discharge technology mainly comprises evaporative crystallization and spraying in a flue. Wherein, the evaporative crystallization method can recycle water resources and crystallized salt, but is limited by overhigh process energy consumption and strict pretreatment requirements, and the large-scale application of the process is limited; the flue evaporation method has simple process and low operation cost, but has the problems of incapability of recovering water resources, influence on subsequent processes such as dust removal and the like, possible flue corrosion and the like.
The invention with application number of 201510298152.9 discloses SO in flue gas3The removal device sprays alkaline absorbent particles to the denitration inlet flue, SO that SO in the flue gas is effectively removed3And the influence of the device on equipment such as a denitration device, an air preheater and the like is reduced. However, the process can not eliminate SO generated again after the flue gas passes through the denitration device3The removal cannot be made to maximum efficiency.
The invention patent with application number 201510553944.6 discloses a bypass evaporator wastewater zero discharge treatment device. The evaporator strengthens heat exchange between the evaporator and the desulfurization waste water by introducing high-temperature flue gas, and the solid particles are dried and then collected after being completely evaporated, thereby realizing zero discharge of waste water. However, the desulfurization wastewater is not reduced, the treatment capacity of the evaporator is large, and the treatment effect of the dust removal device can be influenced by high-moisture-content flue gas.
The invention patent with application number 201510955608.4 discloses a treatment method for zero emission of flue gas waste heat evaporation desulfurization wastewater, which comprises three systems of dual-alkali pretreatment, membrane filtration, desalination, concentration and reduction and flue bypass evaporation, and can recycle desalted water and recycle gaseous water vapor, and crystals are discharged together with fly ash, so that zero emission of desulfurization water and high-salt wastewater is realized. However, the method is too complex, the used process equipment is various, and the equipment construction cost and the maintenance workload are greatly increased.
In the invention, SO3The removal technology and the wastewater zero discharge technology are combined, and an integrated process is adopted, so that the treatment of pollutants and the reutilization of resources and energy sources are better realized.
Disclosure of Invention
The invention provides a SO3The device and the method for removing and zero discharge of desulfurization waste water comprise Chinese SO of coal-fired flue gas of a power plant3The removal and the zero discharge of the desulfurization wastewater treated by the processes such as the triple box and the like in the wet desulfurization process are realized, the process is simple, the energy consumption is low, and a good treatment effect can be achieved.
SO (SO)3The device for removing and zero discharge of desulfurization waste water comprises SO3The system comprises an absorbent preparation part (I), a desulfurization wastewater zero-discharge pretreatment part (II), a solution metering and distributing part (III) and a jet evaporation part (IV). The SO3The absorbent preparation part (I) comprises Na2CO3Dissolving tank (1), Na2CO3A liquid storage tank (2-1), an online pipeline mixer (2-3), and Na2CO3Dissolving tank (1) and the Na2CO3The liquid storage tank (2-1) is connected with the Na2CO3The liquid storage tank (2-1) is connected with the online pipeline mixer (2-3); desulfurization waste water zero release preliminary treatment part (II) is including mixing dosing tank (3), clarification sedimentation tank (4), ultrafiltration device (5), reverse osmosis membrane group (6), fresh water tank (2-2), dense water tank (2-4), coarse filter (14), wherein, mix dosing tank (3) one end with Na2CO3Dissolving tank (1) is connected, the other end of mixed dosing tank (3) with clarification sedimentation tank (4) are connected, coarse filter (14) with clarification sedimentation tank (4) upper portion is connected, ultrafiltration device (5) with coarse filter (14) are connected, reverse osmosis membrane group (6) with ultrafiltration device (5) are connected, fresh water tank (2-2) respectively with the play water portion of ultrafiltration device (5) with the play water portion of reverse osmosis membrane group (6) and Na2CO3The dissolving tank (1) is connected, and the concentrated water tank (2-4) is respectively connected with the concentrated water outlet part of the reverse osmosis membrane group (6) and the online pipeline mixer (2-3); the solution metering and distributing section (III) comprises a plurality of injection branch lines (15) connected to the in-line pipe mixers (2-3);the spray evaporation part (IV) comprises a plurality of two-fluid atomization spray guns (7) connected with the spray branch pipelines (15).
Further, the SO3The absorbent preparation part (I) also comprises an impurity discharge pump (10-1), a dissolving tank delivery pump (10-2), an alkali liquor high-pressure pump (10-3), a flocculating agent flow meter (11-1), an alkali liquor flow meter (11-2), a concentrated water flow meter (11-3) and a fresh water flow meter (11-4), wherein the Na is contained in the solution, and the sodium chloride is dissolved in the solution2CO3The dissolving tank (1) is connected with the mixed dosing tank (3) through the impurity discharge pump (10-1), and the flocculating agent flow meter (11-1) is arranged between the impurity discharge pump (10-1) and the mixed dosing tank (3); the Na is2CO3The dissolving tank (1) is communicated with the Na through the dissolving tank delivery pump (10-2)2CO3The liquid storage tank (2-1) is connected, and the fresh water flow meter (11-4) is connected with the Na2CO3The dissolving tank (1) is connected with the Na2CO3The liquid storage tank (2-1) is connected with the online pipeline mixer (2-3) through the alkali liquor high-pressure pump (10-3), the alkali liquor flowmeter (11-2) is arranged between the alkali liquor high-pressure pump (10-3) and the online pipeline mixer (2-3), and the concentrated water flowmeter (11-3) is arranged on a connecting pipeline of the online pipeline mixer (2-3) and the concentrated water tank (2-4).
Further, the desulfurization wastewater zero-emission pretreatment part (II) further comprises a sludge treatment facility, a wastewater delivery pump (10-4), a coarse filtrate delivery pump (10-5), an ultrafiltrate delivery pump (10-6), a fresh water delivery pump (10-7) and a concentrated water high-pressure pump (10-8), wherein one end of the mixed dosing tank (3) is connected with the clarification sedimentation tank (4) through the wastewater delivery pump (10-4), the sludge treatment facility is connected with the bottom of the clarification sedimentation tank (4), the ultrafiltration device (5) is connected with the coarse filter (14) through the coarse filtrate delivery pump (10-5), and the reverse osmosis membrane group (6) is connected with the ultrafiltration device (5) through the ultrafiltrate delivery pump (10-6); the fresh water tank (2-2) is communicated with the Na through the fresh water delivery pump (10-7)2CO3The dissolving tank (1) is connected, and the concentrated water tank (2-4) is connected with the online pipeline mixer (2-3) through the concentrated water high-pressure pump (10-8).
Furthermore, each branch pipeline (15) is provided with a branch alkali liquor valve (13-1), a branch flow meter (11-5) and a branch hydraulic pressure meter (12-1), the branch alkali liquor valve (13-1), the branch flow meter (11-5) and the branch hydraulic pressure meter (12-1) are sequentially connected, and the branch hydraulic pressure meter (12-1) is connected with the two-fluid atomization spray gun (7).
Furthermore, one end of each two-fluid atomization spray gun (7) is provided with a plurality of nozzles (8-1), and the nozzles (8-1) are uniformly distributed in the flue; and a spray gun alkaline liquid valve (13-2), a spray gun hydraulic gauge (12-2) and a pipeline provided with a compressed air valve (13-3) and a compressed air pressure gauge (12-3) are arranged at the other end of the spray gun (7).
Preferably, the ultrafiltration device (5) can adopt an organic membrane, a metal membrane or a ceramic membrane, and the ultrafiltration device (5) is provided with an automatic cleaning module; the reverse osmosis membrane group (6) can adopt acetate fibers or composite membranes in organic membranes, and the reverse osmosis membrane group (6) is provided with an automatic cleaning module.
Further, the sludge treatment facility comprises a sludge delivery pump (8) and a plate-and-frame filter press (9), wherein the sludge delivery pump (8) is connected with the bottom of the clarification and sedimentation tank (4), and the plate-and-frame filter press (9) is connected with the sludge delivery pump (8).
Using SO3The method of the device integrating the removal and zero discharge of the desulfurization waste water is (1) SO3Preparing an absorbent:
in Na2CO3In the dissolving tank (1), Na is continuously stirred and dissolved at the constant temperature of 30-40 DEG C2CO3And respectively using industrial water and fresh water as dissolving water in the starting stage and the running stage of the process, wherein the using amount a of the dissolving water is controlled by a fresh water flow meter (11-4) and is finally prepared into a solution with the concentration of 20 wt.%;
dissolving tank bottom impurity along with Na2CO3The solution is conveyed to a mixing dosing tank (3) by an impurity discharge pump (10-1) and is measured by a flocculant flowmeter (11-1)Controlling the flow and recording as the usage b; the rest of the fully dissolved Na2CO3The solution is transferred to Na by a dissolving tank transfer pump (10-2)2CO3The liquid storage tank (2-1) is stored for standby;
na is respectively controlled by an alkali liquor flowmeter (11-2) and a concentrated water flowmeter (11-3)2CO3The stock solution was at flow c and flow d, Na2CO3Na in the liquid storage tank (2-1)2CO3The stock solution is conveyed by an alkali liquor high-pressure pump (10-3), mixed and diluted with concentrated water in an online pipeline mixer (2-3) according to a dilution ratio m, and conveyed to a solution metering and distributing part, wherein the dilution ratio m is 1.3-4;
SO3the amounts of the liquids a to d and Na in the absorbent preparation part (I)2CO3The solution dilution ratio m meets the following requirements: a ═ b + c; m is (c + d)/c.
(2) Desulfurization wastewater zero-discharge pretreatment:
the Na2CO3 solution and the desulfurization wastewater are stirred through a mixing and feeding box (3), the mixture is fully mixed and then is conveyed to a clarifying and settling tank (4) by a wastewater conveying pump (10-4) to separate impurities in the solution, and the amount of the desulfurization wastewater is x times of the amount b of the Na2CO3 solution used as a flocculating agent;
the supernatant fluid treated by the clarification and sedimentation tank (4) is further filtered by a coarse filter (14), and is conveyed to an ultrafiltration device (5) and a reverse osmosis membrane group (6) by a coarse filtrate conveying pump (10-5) for advanced treatment, the obtained fresh water is used as dissolving water of Na2CO3 to be stored in a fresh water tank (2-2) for later use, the concentrated water is conveyed to a concentrated water tank (2-4) for later use by an ultrafiltrate conveying pump (10-6), and the concentration multiple of the desulfurization wastewater is n, which accords with the following requirements: n ═ 1+ x) b/d;
(3) solution pre-spray dosing:
through the adjustment of the opening of a branch alkali liquor valve (13-1), absorption liquor diluted and mixed in an online pipeline mixer (2-3) respectively enters branch pipelines according to the set flow of each branch flowmeter (11-5), the pressure condition in the branch pipelines is monitored by a branch pressure gauge (12-1), the total consumption e of alkali liquor meets the condition that the molar ratio of an absorbent to sulfur trioxide in flue gas is 1.1-2.5, and the total consumption e of alkali liquor is c + d;
(4) and (3) spray evaporation:
na atomized by double-fluid spray gun and sprayed at designed flue position2CO3The spraying direction of the solution and the liquid is consistent with the flow direction of the flue gas, so that the diluted Na2CO3The solution is uniformly mixed with the high-temperature flue gas to realize SO in the flue gas simultaneously3And (4) removing and evaporating and crystallizing concentrated water.
In the step (2), x is 2-8, and n is 2-5.
The invention has the following beneficial effects:
1. the SO3The removal and zero discharge of the desulfurization waste water are integrated, SO that the removal of SO in the flue gas of a coal-fired power plant is realized3Meanwhile, zero emission of the desulfurization wastewater is realized;
2. the SO3The removal and zero discharge of the desulfurization waste water are integrated, and SO is used3Na in the removing process2CO3The solution is used for treating the desulfurization wastewater, so that the hardness of the desulfurization wastewater is further reduced;
3. the SO3Removal and zero discharge of desulfurized wastewater integrated process, Na2CO3The dissolved impurities can be discharged out of the system together with sludge generated by the softening pretreatment of the desulfurization wastewater after entering a clarification sedimentation tank, and no additional configuration is needed, so that the system is highly integrated;
4. the SO3The desulfurization wastewater is subjected to coarse filtration, ultrafiltration and reverse osmosis concentration reduction treatment, and the obtained fresh water is reused for SO3Remove Na in the system2CO3Powder dissolving process, concentrated water for SO3Remove Na in the system2CO3The solution is diluted, so that the reasonable utilization of resources is realized;
5. the SO3Removal and desulfurization wastewater zero discharge integrated chemical industryProcess, SO-pair by common metering and distributing system and injection module3The removal system and the wastewater zero discharge system are integrally designed, the process equipment is simple, and the equipment construction and maintenance workload is effectively reduced.
Drawings
FIG. 1 is a schematic view of an integrated device for SO3 removal and zero discharge of desulfurization wastewater.
FIG. 2 is a schematic top view of a portion of the arrangement of the lance of the present invention within a flue.
In the figure:
I.SO3absorbent preparation part, A. industrial water, 1.Na2CO3Dissolving tank, 2-1.Na2CO3A liquid storage tank, 2-3 parts of an online pipeline mixer, 10-1 parts of an impurity discharge pump, 10-2 parts of a dissolving tank delivery pump, 10-3 parts of an alkali liquor high-pressure pump, 11-1 parts of a flocculant flowmeter, 11-2 parts of an alkali liquor flowmeter and 11-3 parts of a concentrated water flowmeter;
II, desulfurization wastewater zero-discharge pretreatment part, B, desulfurization wastewater, 3, a mixed dosing tank, 4, a clarifying sedimentation tank, 14, a coarse filter, 5, an ultrafiltration device, 6, a reverse osmosis membrane group, 2-2, a fresh water tank, 2-4, a concentrated water tank, 8, a sludge delivery pump, 9, a filter, 10-4, a wastewater delivery pump, 10-5, a coarse filtrate delivery pump, 10-6, an ultrafiltrate delivery pump, 10-7, a fresh water delivery pump and 10-8, a concentrated water high-pressure pump;
III, a solution metering and distributing part, 15, a spraying branch pipeline, 13-1 branch alkali liquor valves, 11-5 branch flow meters and 12-1 branch hydraulic pressure meters;
IV, spraying an evaporation part, C, compressed air, 7, a two-fluid atomization spray gun, 8-1, a nozzle, 13-2, a spray gun alkali liquor valve, 13-3, a compressed air valve, 12-2, a spray gun hydraulic gauge and 12-3, a compressed air pressure gauge.
Detailed Description
In order to make the technical problems, technical solutions and advantages of the present invention more apparent, the following detailed description is given with reference to the accompanying drawings and specific embodiments, which are only used for explaining the present invention and are not used for limiting the scope of the present invention.
As shown in figure 1, an alkaline process SO3The integrated process of removing and zero discharge of desulfurization waste water comprises SO3The system comprises an absorbent preparation part I, a desulfurization wastewater zero-discharge pretreatment part II, a solution metering and distributing part III and a jet evaporation part IV.
The SO3Absorbent preparation part I comprises Na2CO3Dissolving tank 1, Na2CO3The system comprises a liquid storage tank 2-1, an online pipeline mixer 2-3, an impurity discharge pump 10-1, a dissolving tank delivery pump 10-2, an alkali liquor high-pressure pump 10-3, a flocculating agent flow meter 11-1, an alkali liquor flow meter 11-2, a concentrated water flow meter 11-3 and a fresh water flow meter 11-4. Wherein, Na2CO3Dissolving tank 1 and Na2CO3The liquid storage tanks 2-1 are all provided with a heat insulation layer, a metering temperature control device, an electric heating device and Na2CO3The dissolving tank 1 also comprises a blanking device and a stirring device.
Na2CO3The powder is dissolved in the dissolving tank 1 at a constant temperature of 30-40 ℃, industrial water and fresh water are respectively used as dissolving water in the starting stage and the running stage of the process, the dissolving water is dissolved under the continuous stirring of a stirrer, wherein the using amount a of the dissolving water is controlled by a fresh water flow meter 11-4, and the solution with the concentration of 20 wt.% is prepared finally.
Dissolving tank bottom impurity along with Na2CO3The solution is conveyed to a mixed dosing tank 3 through an impurity discharge pump 10-1, and the flow is controlled by a flocculating agent flowmeter 11-1 and is recorded as the consumption b; the rest of the fully dissolved Na2CO3The solution is delivered to Na by a dissolving tank delivery pump 10-22CO3The liquid storage tank 2-1 is stored for standby.
Respectively controlling Na by using alkali liquor flowmeter 11-2 and concentrated water flowmeter 11-32CO3The stock solution was at flow c and flow d, Na2CO3Na in liquid storage tank 2-12CO3The stock solution is conveyed by an alkali liquor high-pressure pump 10-3, mixed and diluted with concentrated water in an online pipeline mixer 2-3 according to a dilution ratio m, and conveyed to the solution metering and distributing part, wherein the dilution ratio m is 1.3-4.
Further, SO3The dosage of each liquid in the absorbent preparation part I is a to d and Na2CO3The solution dilution ratio m meets the following requirements: a ═ b + c; m is (c + d)/c.
The desulfurization wastewater zero-discharge pretreatment part II comprises a mixed dosing tank 3, a clarification sedimentation tank 4, a coarse filter 14, an ultrafiltration device 5, a reverse osmosis membrane group 6, a fresh water tank 2-2, a concentrated water tank 2-4, a sludge delivery pump 8, a plate-and-frame filter press 9, a wastewater delivery pump 10-4, a coarse filtrate delivery pump 10-5, an ultrafiltrate delivery pump 10-6, a fresh water delivery pump 10-7 and a concentrated water high-pressure pump 10-8.
The mixing and feeding box 3 is provided with a stirring device for stirring Na2CO3The solution and the desulfurization wastewater are fully mixed and then are conveyed to a clarifying sedimentation tank 4 by a wastewater conveying pump 10-4 to separate impurities in the solution, wherein the amount of the desulfurization wastewater is Na used as a flocculating agent2CO3X times (2-8) the amount b of the solution; the supernatant fluid treated by the clarifying sedimentation tank 4 is further filtered by a coarse filter 14, is conveyed to an ultrafiltration device 5 and a reverse osmosis membrane group 6 by a coarse filtrate conveying pump 10-5 and an ultrafiltrate conveying pump 10-6 for advanced treatment, and the obtained fresh water is used as Na2CO3The dissolving water is stored in the fresh water tank 2-2 for standby, and the concentrated water is conveyed to the concentrated water tank 2-4 for standby. The concentration multiple of the desulfurization wastewater is recorded as n (2-5), and the method accords with the following steps: n is (1+ x) b/d.
The fresh water is reusable water which is obtained after advanced treatment by the ultrafiltration device 5 and the reverse osmosis membrane group 6 and reaches the discharge standard.
The concentrated water is the water which is not up to the standard and is obtained after advanced treatment by the reverse osmosis membrane group 6.
Wherein the ultrafiltration device 5 can adopt an organic membrane, a metal membrane or a ceramic membrane, and the reverse osmosis membrane group 6 is acetate fiber or a composite membrane in the organic membrane; the two devices are provided with automatic cleaning modules, industrial water is used for automatically cleaning the membrane component at regular intervals, the service life of the membrane is prolonged, and the cleaned wastewater enters the mixed dosing tank 3 along with the desulfurization wastewater for treatment.
The desulfurization wastewater zero-discharge pretreatment part II is also matched with a sludge treatment facility. The sludge at the bottom of the sedimentation tank 4 is cleaned by a mud scraper, is conveyed by a sludge conveying pump 8, is compressed into a mud cake by a plate-and-frame filter press 9 so as to be beneficial to further conveying and disposing of the sludge, and the obtained clear liquid enters the clarification sedimentation tank 4 again. Wherein, the plate-and-frame filter press 9 can use the existing equipment in the desulfurization process of the power plant or can be configured independently.
The solution metering and distributing part III comprises a plurality of spraying branch pipelines 15, and each branch pipeline is provided with a branch alkali liquor valve 13-1, a branch flow meter 11-5 and a branch hydraulic pressure meter 12-1. By adjusting the opening of the branch alkali liquor valve 13-1, the absorption liquid diluted and mixed in the online pipeline mixer 2-3 respectively enters the branch pipelines according to the set flow of each branch flowmeter 11-5, and the pressure condition in the branch pipelines is monitored by the branch pressure gauge 12-1. And (3) spraying the total alkali liquor consumption e according to the condition that the molar ratio of the absorbent to sulfur trioxide in the flue gas is 1.1-2.5.
The injection evaporation part IV comprises a plurality of double-fluid atomization spray guns 7 communicated with an injection branch pipeline 15, one end of each spray gun is provided with a spray gun alkali liquor valve 13-2 and a spray gun hydraulic pressure meter 12-2 and is connected with a pipeline for introducing compressed air, and the pipeline is provided with a compressed air valve 13-3 and a compressed air pressure meter 12-3 and is provided with a pipeline filter; the other end of the spray gun is provided with a plurality of nozzles 8-1. By arranging a two-fluid atomizing spray gun 7 at the position of the flue before the ammonia injection grid or after the denitration device and injecting diluted Na into the flue2CO3Dissolving the Na in the solution2CO3The solution is uniformly mixed with the high-temperature flue gas, SO that the removal of SO3 in the flue gas and the evaporation and crystallization treatment of concentrated water are simultaneously realized.
As shown in fig. 2, the spray evaporation section IV has a plurality of two-fluid spray gun atomizing spray guns disposed at one end in the flue, and a plurality of spray guns, for example, 3, 5, 7, 9, etc., may be disposed, each spray gun communicating with one of the spray branch pipes 15. Each spray gun is uniformly distributed with a plurality of nozzles 8-1 to realize full mixing. In addition, the liquid is sprayed in the same direction as the flue gas to minimize the possibility of fouling and blockage of the spray gun.
In conclusion, the invention provides an integrated treatment technology with low cost and high efficiency, and realizes SO in flue gas of a power plant3The removal process and the wet desulphurization process have zero discharge of waste water.
While the foregoing is directed to the preferred embodiment of the present invention, it will be understood by those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention as defined in the appended claims.
Claims (10)
1. SO (SO)3The device for removing and zero discharge of desulfurization waste water is characterized by comprising SO3The system comprises an absorbent preparation part (I), a desulfurization wastewater zero-discharge pretreatment part (II), a solution metering and distributing part (III) and a jet evaporation part (IV); wherein,
the SO3The absorbent preparation part (I) comprises Na2CO3Dissolving tank (1), Na2CO3A liquid storage tank (2-1), an online pipeline mixer (2-3), and Na2CO3Dissolving tank (1) and the Na2CO3The liquid storage tank (2-1) is connected with the Na2CO3The liquid storage tank (2-1) is connected with the online pipeline mixer (2-3);
the desulfurization wastewater zero-emission pretreatment part (II) comprises a mixed dosing tank (3), a clarification sedimentation tank (4), an ultrafiltration device (5), a reverse osmosis membrane group (6), a fresh water tank (2-2), a concentrated water tank (2-4) and a coarse filter (14), wherein one end of the mixed dosing tank (3) is connected with the Na2CO3Dissolving tank (1) is connected, the other end of mixed dosing tank (3) with clarification sedimentation tank (4) are connected, coarse filter (14) with clarification sedimentation tank (4) upper portion is connected, ultrafiltration device (5) with coarse filter (14) are connected, reverse osmosis membrane group (6) with ultrafiltration device (5) are connected, fresh water tank (2-2) respectively with the play water portion of ultrafiltration device (5) with the play water portion of reverse osmosis membrane group (6) and Na2CO3The dissolving tank (1) is connected, and the concentrated water tank (2-4) is respectively connected with the concentrated water outlet part of the reverse osmosis membrane group (6) and the online pipeline mixer (2-3);
the solution metering and distributing section (III) comprises a plurality of injection branch pipes (15) connected to the in-line pipe mixer (2-3);
the injection evaporation part (IV) comprises a plurality of double-fluid atomization spray guns (7) connected with the injection branch pipelines (15).
2. SO according to claim 13Desorption and desulfurization waste water zero release integrated device, its characterized in that: the SO3The absorbent preparation part (I) also comprises an impurity discharge pump (10-1), a dissolving tank delivery pump (10-2), an alkali liquor high-pressure pump (10-3), a flocculating agent flow meter (11-1), an alkali liquor flow meter (11-2), a concentrated water flow meter (11-3) and a fresh water flow meter (11-4), wherein the Na is contained in the solution, and the sodium chloride is dissolved in the solution2CO3The dissolving tank (1) is connected with the mixed dosing tank (3) through the impurity discharge pump (10-1), and the flocculating agent flow meter (11-1) is arranged between the impurity discharge pump (10-1) and the mixed dosing tank (3); the Na is2CO3The dissolving tank (1) is communicated with the Na through the dissolving tank delivery pump (10-2)2CO3The liquid storage tank (2-1) is connectedThe fresh water flow meter (11-4) is connected with the Na2CO3The dissolving tank (1) is connected with the Na2CO3The liquid storage tank (2-1) is connected with the online pipeline mixer (2-3) through the alkali liquor high-pressure pump (10-3), the alkali liquor flowmeter (11-2) is arranged between the alkali liquor high-pressure pump (10-3) and the online pipeline mixer (2-3), and the concentrated water flowmeter (11-3) is arranged on a connecting pipeline of the online pipeline mixer (2-3) and the concentrated water tank (2-4).
3. SO according to claim 13Desorption and desulfurization waste water zero release integrated device, its characterized in that: the desulfurization wastewater zero-emission pretreatment part (II) further comprises a sludge treatment facility, a wastewater delivery pump (10-4), a coarse filtrate delivery pump (10-5), an ultrafiltrate delivery pump (10-6), a fresh water delivery pump (10-7) and a concentrated water high-pressure pump (10-8), wherein one end of the mixed dosing tank (3) is connected with the clarification sedimentation tank (4) through the wastewater delivery pump (10-4), the sludge treatment facility is connected with the bottom of the clarification sedimentation tank (4), the ultrafiltration device (5) is connected with the coarse filter (14) through the coarse filtrate delivery pump (10-5), and the reverse osmosis membrane group (6) is connected with the ultrafiltration device (5) through the ultrafiltrate delivery pump (10-6); the fresh water tank (2-2) is communicated with the Na through the fresh water delivery pump (10-7)2CO3The dissolving tank (1) is connected, and the concentrated water tank (2-4) is connected with the online pipeline mixer (2-3) through the concentrated water high-pressure pump (10-8).
4. SO according to claim 13Desorption and desulfurization waste water zero release integrated device, its characterized in that: each branch pipeline (15) is provided with a branch alkali liquor valve (13-1), a branch flow meter (11-5) and a branch hydraulic pressure meter (12-1), the branch alkali liquor valve (13-1), the branch flow meter (11-5) and the branch hydraulic pressure meter (12-1) are sequentially connected, and the branch hydraulic pressure meter (12-1) is connected with the double-fluid atomization spray gun (7).
5. SO according to claim 13Desorption and desulfurization waste water zero release integrated device, its characterized in that: one end of each two-fluid atomization spray gun (7) is provided with a plurality of nozzles (8-1), and the nozzles (8-1) are uniformly distributed in the flue; and a spray gun alkaline liquid valve (13-2), a spray gun hydraulic gauge (12-2) and a pipeline provided with a compressed air valve (13-3) and a compressed air pressure gauge (12-3) are arranged at the other end of the spray gun (7).
6. SO according to claim 1 or 33Desorption and desulfurization waste water zero release integrated device, its characterized in that: the ultrafiltration device (5) can adopt an organic membrane, a metal membrane or a ceramic membrane, and the ultrafiltration device (5) is provided with an automatic cleaning module.
7. SO according to claim 1 or 33Desorption and desulfurization waste water zero release integrated device, its characterized in that: the reverse osmosis membrane group (6) can adopt acetate fibers or composite membranes in organic membranes, and the reverse osmosis membrane group (6) is provided with an automatic cleaning module.
8. SO according to claim 33Desorption and desulfurization waste water zero release integrated device, its characterized in that: the sludge treatment facility comprises a sludge delivery pump (8) and a plate-and-frame filter press (9), wherein the sludge delivery pump (8) is connected with the bottom of the clarification sedimentation tank (4), and the plate-and-frame filter press (9) is connected with the sludge delivery pump (8).
9. Use of a SO according to preceding claim3The method of the device integrating the removal and the zero discharge of the desulfurization wastewater is characterized in that: the method comprises the following steps:
(1)SO3preparing an absorbent:
in Na2CO3In the dissolving tank (1), Na is continuously stirred and dissolved at the constant temperature of 30-40 DEG C2CO3And respectively using industrial water and fresh water as dissolving water in the starting stage and the running stage of the process, wherein the using amount of the dissolving water is generalA freshwater flow meter (11-4) control, finally configured into a solution with a concentration of 20 wt.%;
dissolving tank bottom impurity along with Na2CO3Conveying the solution to a mixing dosing tank (3) through an impurity discharge pump (10-1), and controlling the flow by a flocculating agent flowmeter (11-1) to be recorded as a dosage b; the rest of the fully dissolved Na2CO3The solution is transferred to Na by a dissolving tank transfer pump (10-2)2CO3The liquid storage tank (2-1) is stored for standby;
na is respectively controlled by an alkali liquor flowmeter (11-2) and a concentrated water flowmeter (11-3)2CO3The stock solution was at flow c and flow d, Na2CO3Na in the liquid storage tank (2-1)2CO3The stock solution is conveyed by an alkali liquor high-pressure pump (10-3), mixed and diluted with concentrated water in an online pipeline mixer (2-3) according to a dilution ratio m, and conveyed to a solution metering and distributing part, wherein the dilution ratio m is 1.3-4;
SO3the amounts of the liquids a to d and Na in the absorbent preparation part (I)2CO3The solution dilution ratio m meets the following requirements: a ═ b + c; m is (c + d)/c.
(2) Desulfurization wastewater zero-discharge pretreatment:
the Na2CO3 solution and the desulfurization wastewater are stirred through a mixing and feeding box (3), the mixture is fully mixed and then is conveyed to a clarifying and settling tank (4) by a wastewater conveying pump (10-4) to separate impurities in the solution, and the amount of the desulfurization wastewater is x times of the amount b of the Na2CO3 solution used as a flocculating agent;
the supernatant fluid treated by the clarification and sedimentation tank (4) is further filtered by a coarse filter (14), and is conveyed to an ultrafiltration device (5) and a reverse osmosis membrane group (6) by a coarse filtrate conveying pump (10-5) for advanced treatment, the obtained fresh water is used as dissolving water of Na2CO3 to be stored in a fresh water tank (2-2) for later use, the concentrated water is conveyed to a concentrated water tank (2-4) for later use by an ultrafiltrate conveying pump (10-6), and the concentration multiple of the desulfurization wastewater is n, which accords with the following requirements: n ═ 1+ x) b/d;
(3) solution pre-spray dosing:
through the adjustment of the opening of a branch alkali liquor valve (13-1), absorption liquor diluted and mixed in an online pipeline mixer (2-3) respectively enters branch pipelines according to the set flow of each branch flowmeter (11-5), the pressure condition in the branch pipelines is monitored by a branch pressure gauge (12-1), the total consumption e of alkali liquor meets the condition that the molar ratio of an absorbent to sulfur trioxide in flue gas is 1.1-2.5, and the total consumption e of alkali liquor is c + d;
(4) and (3) spray evaporation:
na atomized by double-fluid spray gun and sprayed at designed flue position2CO3The spraying direction of the solution and the liquid is consistent with the flow direction of the flue gas, so that the diluted Na2CO3The solution is uniformly mixed with the high-temperature flue gas to realize SO in the flue gas simultaneously3And (4) removing and evaporating and crystallizing concentrated water.
10. Use of SO according to claim 93The method of the device integrating the removal and the zero discharge of the desulfurization wastewater is characterized in that: in the step (2), x is 2-8, and n is 2-5.
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| CN108383310A (en) * | 2018-03-19 | 2018-08-10 | 中国大唐集团科学技术研究院有限公司火力发电技术研究院 | A kind of quenched desulfurization wastewater flue evaporation and cooperation-removal SO3Method |
| CN108434950A (en) * | 2018-03-15 | 2018-08-24 | 东南大学 | A kind of devices and methods therefor of the evaporation of coordinated desulfurization waste water flue and enhancing fine particle and sulfur trioxide removing |
| CN112850974A (en) * | 2021-04-14 | 2021-05-28 | 丽水市太行环境科技有限公司 | Sewage treatment system and sewage treatment method thereof |
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Application publication date: 20170811 |