WO2020108135A1 - 一种脱硫废水处理系统及脱硫废水处理方法 - Google Patents

一种脱硫废水处理系统及脱硫废水处理方法 Download PDF

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Publication number
WO2020108135A1
WO2020108135A1 PCT/CN2019/111241 CN2019111241W WO2020108135A1 WO 2020108135 A1 WO2020108135 A1 WO 2020108135A1 CN 2019111241 W CN2019111241 W CN 2019111241W WO 2020108135 A1 WO2020108135 A1 WO 2020108135A1
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Prior art keywords
flue gas
desulfurization
evaporator
desulfurization wastewater
water
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English (en)
French (fr)
Inventor
黄锐
刘强
秦福初
杨洋
荆黎
徐杨华
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Spic Yuanda Environmental Protection Engineering Co Ltd Chongqing Science And Technology Branch
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Spic Yuanda Environmental Protection Engineering Co Ltd Chongqing Science And Technology Branch
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • 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
    • 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes

Definitions

  • the invention relates to the technical field of industrial wastewater treatment, in particular to a desulfurization wastewater treatment system and a desulfurization wastewater treatment method.
  • SO 2 is one of the main atmospheric pollutants facing human beings today. Too much SO 2 content in the air can cause acid rain and damage crops and buildings. SO 2 will also adsorb on the dust in the air and enter the human body through the respiratory tract, seriously damaging human health. The vast majority of SO 2 emissions come from coal combustion, such as: thermal power plants, industrial coal combustion, heating, etc., in the process of coal combustion will produce a large amount of SO 2 .
  • flue gas desulfurization is a widely adopted treatment method.
  • the limestone/gypsum wet flue gas desulfurization process is usually used to desulfurize flue gas.
  • a large amount of desulfurization wastewater containing solid suspended solids, heavy metal ions, high hardness and high pollution will be generated in the wet desulfurization process.
  • Embodiments of the present invention provide a desulfurization wastewater treatment system and a desulfurization wastewater treatment method, to solve the problem of high operating cost of the desulfurization wastewater zero discharge system in the prior art.
  • the present invention adopts the following technical solutions:
  • a desulfurization wastewater treatment system is provided.
  • the desulfurization wastewater treatment system is applied to a coal-fired power plant, and the flue gas generated by the coal-fired power plant passes through a flue gas main pipe to a denitration device and air in sequence.
  • the main flue gas pipeline includes a first side pipeline located on the side of the air preheater near the denitration device and a In the second side duct on the other side of the air preheater, the temperature of the flue gas in the first side duct is greater than the temperature of the flue gas in the second side duct, and the desulfurization wastewater treatment system includes:
  • a pre-settling tank connected to the outlet of the wet desulfurization absorption tower for collecting desulfurization wastewater in the wet desulfurization absorption tower;
  • the water inlet of the concentration tower communicates with the water outlet of the pre-sedimentation tank, and the air inlet of the concentration tower communicates with the second side duct for using the flue gas in the second side duct Concentrate the desulfurization wastewater;
  • the water inlet of the evaporator communicates with the water outlet of the concentration tower, and the air inlet of the evaporator communicates with the first side duct for evaporating the flue gas in the first side duct Desulfurization wastewater after drying and concentration.
  • the air outlet of the concentration tower and the air outlet of the evaporator are both in communication with a portion of the second side pipe between the air preheater and the wet desulfurization absorption tower.
  • both the water inlet and the air outlet of the concentration tower are provided at the top of the concentration tower, and the water outlet and the air inlet of the concentration tower are provided at the lower part of the concentration tower.
  • both the air inlet and the water inlet of the evaporator are provided at the top of the evaporator, and the air outlet of the evaporator is provided at the bottom of the evaporator.
  • a coagulation and sedimentation device is connected between the water outlet of the concentration tower and the water inlet of the evaporator for separating and clarifying the concentrated desulfurized wastewater through the clarification of the coagulation and sedimentation device Liquid and sediment to drain the clear liquid into the evaporator.
  • an atomizer is further provided between the water outlet of the coagulation and sedimentation device and the water inlet of the evaporator for discharging the clarified liquid discharged from the coagulation and sedimentation device after atomization Into the evaporator.
  • the atomizer is a two-fluid atomizing spray gun.
  • the two-fluid atomizing spray gun includes an air compressor and a spray water pump.
  • the air compressor atomizes the clarified liquid sprayed by the spray water pump into Water mist with a particle size of 20 ⁇ m to 200 ⁇ m, wherein the spray water pump connects the water outlet of the coagulation sedimentation device and the water inlet of the evaporator, and the water outlet of the two-fluid atomizing spray gun is provided at the evaporation The water inlet of the device.
  • a booster fan is provided between the air inlet of the concentration tower and the second side duct, and the flue gas in the second side duct enters the concentration tower after being boosted by the booster fan Inside.
  • a desulfurization wastewater treatment method which is applied to a coal-fired power plant, and the flue gas generated by the coal-fired power plant is sequentially passed through a flue gas main pipe to a denitration device, an air preheater, and a dust collector And a wet desulfurization absorption tower, which is then discharged to the outside world
  • the flue gas main pipe includes a first side pipe located on the side of the air preheater near the denitration device and another on the air preheater On the second side duct on one side, the temperature of the flue gas in the first side duct is greater than the temperature of the flue gas in the second side duct
  • the method includes:
  • the method further includes:
  • the flue gas after concentration of the desulfurization wastewater is discharged into the wet desulfurization absorption tower for desulfurization;
  • the flue gas after evaporating the desulfurization waste water is sequentially discharged into the dust collector and the wet desulfurization absorption tower for dust removal and desulfurization.
  • the flue gas discharged from the coal-fired power plant is used to concentrate the desulfurized wastewater in a concentration tower, and the concentrated desulfurized wastewater is evaporated in an evaporator to achieve zero discharge of desulfurized wastewater.
  • the chemical pretreatment of desulfurization wastewater is omitted, so the cost of chemical pretreatment is saved, and the energy discharged from coal-fired power plants is used to dry the desulfurization wastewater twice, without providing energy for the drying of desulfurization wastewater, thereby reducing the The energy consumption of desulfurization wastewater treatment, therefore, the desulfurization wastewater treatment system provided by the embodiment of the present invention can reduce the cost of processing desulfurization wastewater.
  • FIG. 1 is a schematic structural diagram of a coal-fired power plant and a desulfurization wastewater treatment system in an embodiment of the present invention
  • FIG. 2 is a schematic structural diagram of a desulfurization wastewater treatment system provided by an embodiment of the present invention
  • FIG. 3 is a flowchart of a desulfurization wastewater treatment method provided by an embodiment of the present invention.
  • FIG. 4 is a flowchart of another desulfurization wastewater treatment method provided by an embodiment of the present invention.
  • FIG. 1 is a schematic structural diagram of a coal-fired power plant and a desulfurization wastewater treatment system according to an embodiment of the present invention
  • FIG. 2 is a schematic structural diagram of a desulfurization wastewater treatment system provided by an embodiment of the present invention. Desulfurization wastewater treatment system, used in coal-fired power plants.
  • the flue gas generated by the coal-fired power plant passes through the flue gas main pipeline 11, passes through the denitration device 12, the air preheater 13, the dust remover 14, and the wet desulfurization absorption tower 15 in order to be discharged to the outside, and the flue gas
  • the main duct 11 includes a first side duct 111 located on the side of the air preheater 13 close to the denitration device 12 and a second side duct 112 located on the other side of the air preheater 13.
  • the flue gas temperature is greater than the flue gas temperature in the second side duct 112.
  • the desulfurization wastewater treatment system includes:
  • a pre-sedimentation tank 21 connected to the water outlet (not shown) of the wet desulfurization absorption tower 15 is used to collect the desulfurization wastewater in the wet desulfurization absorption tower 15;
  • Concentration tower 22 the water inlet 221 of the concentration tower 22 communicates with the water outlet 211 of the pre-sedimentation tank 21, and the air inlet 222 of the concentration tower 22 communicates with the second side duct 112 for concentration of the flue gas in the second side duct 112
  • the desulfurization wastewater
  • the evaporator 23 the water inlet 231 of the evaporator 23 communicates with the water outlet 223 of the concentration tower 22, and the air inlet 232 of the evaporator 23 communicates with the first side pipe 111 for evaporating and drying using the flue gas in the first side pipe 111 Concentrated desulfurization wastewater.
  • the boiler of coal-fired power plant 100 undergoes coal-burning reaction, which generates high-temperature flue gas.
  • the flue gas is mixed with dust, sulfur dioxide, SO2, and nitrogen oxide compounds (for example: NO2).
  • NO2 nitrogen oxide compounds
  • Flue gas can only be discharged into the atmosphere after various treatments including denitrification, cooling, dust removal, and desulfurization.
  • the temperature of the flue gas discharged by the coal-fired power plant is very high, for example, between 150°C and 220°C, which may be called high-temperature flue gas.
  • the flue gas still has a high residual heat, for example, between 90°C and 110°C, which can be called low-temperature flue gas.
  • the volume of desulfurized wastewater can be concentrated by 60 to 80% through the concentration tower 22, which greatly reduces the volume of desulfurized wastewater entering the evaporator 23.
  • the low-temperature flue gas is first used to concentrate the desulfurized wastewater to reduce the water content of the desulfurized wastewater, thereby reducing the volume of the desulfurized wastewater.
  • the high-temperature flue gas is then used to completely evaporate the concentrated desulfurized wastewater to achieve zero wastewater discharge.
  • the usage rate of high-temperature flue gas can be reduced to avoid reducing the thermal efficiency of the boiler.
  • the coal-fired power plant is also provided with a chimney 16, and the wet desulfurization absorption tower 15 communicates with the chimney 16 to discharge flue gas after denitrification, cooling, dust removal, and desulfurization into the atmosphere .
  • the denitration device 12 may be a selective catalytic reduction denitration device (SCR) (referred to as "SCR reactor” as shown in FIG. 2 for short), of course, it may also be a flue gas recirculation denitration device, selective non-catalytic Any one of reduction denitration equipment (SNCR), etc.
  • SCR selective catalytic reduction denitration device
  • SNCR selective non-catalytic Any one of reduction denitration equipment
  • the air preheater 13 may be referred to as an “air preheater” as shown in FIG. 2, and the air preheater 13 may use the temperature of the flue gas to preheat the air entering the boiler to reduce the smoke At the same time as the gas temperature, the heat can also be recycled.
  • the air outlet 224 of the concentration tower 22 and the air outlet 233 of the evaporator 23 are both in communication with the portion of the second side duct 112 between the air preheater 13 and the wet desulfurization absorption tower 15.
  • the flue gas will take part of the water vapor through the wet desulfurization absorption tower 15, it is necessary to add process water to the wet desulfurization absorption tower 15 to ensure the efficiency of the wet desulfurization absorption tower 15 for wet desulfurization.
  • the air outlet 233 of the concentration tower 22 and the air outlet 224 of the evaporator 23 are both communicated with the second side pipe 112, so that the water vapor formed by the evaporation in the concentration tower 22 and the evaporator 23 can enter the wet desulfurization through the second side pipe 112
  • the absorption tower 15 supplements the amount of water in the wet desulfurization absorption tower 15.
  • the water in the desulfurization wastewater can be recycled to reduce the amount of water added to the wet desulfurization absorption tower.
  • the air inlet 222 and the air outlet 224 of the concentration tower 22 are both in communication with the portion of the second side duct 112 between the dust collector 14 and the wet desulfurization absorption tower 15.
  • the desulfurized waste water is concentrated by using the dedusted flue gas to prevent the dust in the flue gas from entering the desulfurized waste water, resulting in repeated dust removal of the dust, thereby improving the treatment efficiency of the desulfurized waste water.
  • the air outlet 233 of the evaporator 23 communicates with a portion of the second side duct 112 between the air preheater 13 and the dust remover 14.
  • the crystallized crystals of the desulfurized wastewater can be collected by a dust collector to prevent the crystals of the desulfurized wastewater from being discharged to the outside and causing environmental pollution.
  • the residual crystals after the desulfurization wastewater is dried enter the fly ash through the dust of the dust collector, the quality of the crystal is small, and the quality of the flue gas dust emitted by the boiler is large, so the desulfurization wastewater crystals will not affect the powder coal
  • the comprehensive utilization of ash will not cause the problem of crystal disposal, thereby facilitating the recycling of fly ash.
  • the water inlet 221 and the air outlet 224 of the concentration tower 22 are both disposed at the top of the concentration tower 22, and the water outlet 223 and the air inlet 222 of the concentration tower 22 are both disposed at the lower portion of the concentration tower 22.
  • the air inlet 222 of the concentration tower 22 is provided at the lower part of the concentration tower 22 and above the liquid level in the concentration tower.
  • the upper part of the concentration tower 22 is provided with a sprinkler 225 communicating with the water inlet 221 for increasing the contact area between the desulfurized wastewater and flue gas, so as to increase the concentration efficiency of the desulfurized wastewater.
  • reverse heat exchange between the desulfurized wastewater and flue gas (that is, the desulfurized wastewater and flue gas move in the opposite direction during heat exchange) can increase the speed of relative movement between the desulfurized wastewater and flue gas, thereby improving desulfurization Wastewater concentration efficiency.
  • a booster fan 28 may be provided at the air inlet 222 of the concentration tower 22 to pressurize the flue gas entering the concentration tower 22 to increase the flow rate of the flue gas, thereby improving the concentration efficiency of desulfurization wastewater.
  • the air inlet 232 and the water inlet 231 of the evaporator 23 are both provided at the top of the evaporator 23, and the air outlet 233 of the evaporator 23 is provided at the bottom of the evaporator 23.
  • the flue gas in the evaporator and the desulfurized wastewater can be moved in the same direction.
  • the obtained crystals are blown out from the air outlet of the evaporator, so that the flue gas and the crystal enter the dust removal
  • the dedusting is carried out in the device to prevent the crystallized crystals of desulfurization waste water from being discharged into the atmosphere, thereby facilitating the collection of crystals of desulfurization waste water and improving the environmental performance of the desulfurization waste water treatment system.
  • a coagulation and sedimentation device 24 is connected between the water outlet 223 of the concentration tower 22 and the water inlet 231 of the evaporator 23 for separating and clarifying the concentrated desulfurized wastewater through the clarification of the coagulation and sedimentation device 24 Liquid and sediment to discharge the clear liquid into the evaporator 23.
  • the impurities in the desulfurization wastewater entering the evaporator can be reduced, the work load of impurity recovery can be reduced, the impurity content in the flue gas discharged to the outside can be reduced, and the environmental performance of the desulfurization wastewater treatment system can be improved.
  • a triple tank 241, a concentration clarification tank 242 communicating with the water outlet of the triple tank 241, and a water outlet tank 243 communicating with the water outlet of the clarification tank 242 are used as the coagulation and sedimentation device 24 And the water outlet tank 243 communicates with the water inlet 231 of the evaporator 23.
  • the concentrated desulfurization wastewater is subjected to a flocculation reaction using a triple tank provided in the coal-fired power plant itself, and a clarification tank is used for clarification to separate clarified liquid and precipitated impurities. And discharge the clarified liquid into the outlet tank for it to flow into the evaporator, thereby removing the large particle suspended matter in the desulfurization wastewater entering the evaporator, which is convenient for the atomization of the desulfurization wastewater without excessive impurities or impurities The particles are too large and block the spray outlet.
  • the precipitated impurities in the concentration and clarification tank can be collected uniformly after settling to a certain amount, thereby facilitating the collection of impurities in the desulfurization wastewater.
  • an atomizer 25 is further provided between the water outlet 241 of the coagulation and sedimentation device 24 and the water inlet 231 of the evaporator 23 for discharging the clarified liquid discharged from the coagulation and sedimentation device 24 after atomization Into the evaporator 23.
  • the contact area between the desulfurization wastewater and the flue gas in the evaporator can be increased, and the efficiency of the additional desulfurization wastewater is greatly improved, thereby improving the overall working efficiency of the desulfurization wastewater treatment system.
  • the atomizer 25 is a two-fluid atomizing spray gun.
  • the two-fluid atomizing spray gun includes an air compressor 251 (also called compressed air storage tank) and a spray water pump 252.
  • the air compressor 251 sprays
  • the clarified liquid sprayed by the water pump 252 is atomized into a water mist with a particle size of 20 ⁇ m to 200 ⁇ m.
  • the water outlet 253 of the fluid atomizing spray gun is provided at the water inlet 231 of the evaporator 23.
  • the pressure of compressed air in the air compressor 251 is between 0.2 and 0.7 MPa.
  • the air compressed in the air compressor 251 may be the flue gas in the second side duct 112.
  • the air compressor can be used to atomize the desulfurization wastewater to greatly increase the contact area between the desulfurization wastewater and the flue gas, thereby improving the drying efficiency of the flue gas to the desulfurization wastewater.
  • the water inlet of the pre-sedimentation tank 21 and the water outlet of the wet desulfurization absorption tower 15 are connected by a cyclone 26.
  • the cyclone can be used to centrifuge the desulfurized waste water and then discharged into the pre-deposition tank, so that the impurities and liquid in the desulfurization waste water can be quickly separated in the pre-deposition tank.
  • a valve 27 is provided at the water inlet 221, the air inlet 222 of the concentration tower 22, and the air inlet 232 of the evaporator 23 to control the amount of flue gas and water entering the concentration tower 22, and the amount of air entering the evaporator 23 The amount of smoke.
  • various valves can be adjusted according to changes in flue gas temperature, desulfurization wastewater volume, etc., to ensure that flue gas can completely evaporate desulfurization wastewater into water vapor and crystals, to avoid incomplete evaporation and zero wastewater discharge, or to avoid smoke Too much air flow increases the high-temperature flue gas consumption of the desulfurization wastewater treatment system and affects the thermal efficiency of the boiler, thereby improving the reliability of the desulfurization wastewater treatment system.
  • a sewage pump 29 may also be provided at the water outlet of the pre-settling tank 21 and the water outlet 223 of the concentration tower 22 to drive the flow of desulfurized wastewater.
  • the flue gas discharged from the coal-fired power plant is used to concentrate the desulfurized wastewater in a concentration tower, and the concentrated desulfurized wastewater is evaporated in an evaporator to achieve zero discharge of desulfurized wastewater. Omitting the chemical pretreatment of the desulfurization wastewater, thus saving the cost of the chemical pretreatment agent, and using the energy discharged by the coal-fired power plant to dry the desulfurization wastewater twice, without providing additional energy for the desulfurization wastewater drying, thus The energy consumption of desulfurization wastewater treatment is reduced, so the desulfurization wastewater treatment system provided by the embodiments of the present invention can reduce the cost of treating desulfurization wastewater.
  • FIG. 3 is a flowchart of a desulfurization wastewater treatment method provided by an embodiment of the present invention.
  • the method is applied to a coal-fired power plant, and the flue gas generated by the coal-fired power plant passes through a flue gas main pipeline in sequence to a denitration device, an air preheater, a dust collector, and a wet desulfurization absorption tower, and then is discharged to the outside world.
  • the main flue gas duct includes a first side duct located on one side of the air preheater near the denitration device and a second side duct located on the other side of the air preheater, in the first side duct
  • the flue gas temperature is greater than the flue gas temperature in the second side duct
  • Step 301 Collect the desulfurization wastewater in the wet desulfurization absorption tower.
  • Step 302 Use the flue gas in the second side pipeline to concentrate the desulfurization wastewater.
  • Step 303 Use the flue gas in the first side pipe to dry the concentrated desulfurization wastewater to dry the desulfurization wastewater into crystals.
  • the method further includes:
  • Step 304 The flue gas after concentration of the desulfurization wastewater is discharged into the wet desulfurization absorption tower for desulfurization.
  • Step 305 The flue gas after evaporating the desulfurization waste water is sequentially discharged into the dust collector and the wet desulfurization absorption tower for dust removal and desulfurization.
  • the method provided by the embodiment of the present invention can be applied to the desulfurization wastewater treatment system provided in FIG. 1 and FIG. 2, and can achieve the same beneficial effects. To avoid repetition, details are not described herein again.

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Abstract

本发明提供了一种脱硫废水处理系统和脱硫废水处理方法，应用于燃煤电厂，燃煤电厂产生的烟气通过烟气主管道依次通入脱硝装置、空气预热器、除尘器以及湿法脱硫吸收塔，然后被排放至外界，烟气主管道包括第一侧管道和第二侧管道，第一侧管道内的烟气温度大于第二侧管道内的烟气温度；脱硫废水处理系统包括与湿法脱硫吸收塔的出水口连通的预沉池；浓缩塔，浓缩塔的入水口与预沉池的出水口连通，浓缩塔的入风口与第二侧管道连通，用于利用第二侧管道内的烟气浓缩脱硫废水；蒸发器，蒸发器的入水口与浓缩塔的出水口连通，蒸发器的入风口与第一侧管道连通，用于利用第一侧管道内的烟气蒸发干燥浓缩后的脱硫废水。本发明实施例能够降低处理脱硫废水的成本。

Description

一种脱硫废水处理系统及脱硫废水处理方法
本申请要求于2018年11月29日递交中国专利局的、申请号为201811443284.6的中国专利申请的权益，该申请的全部公开内容以引用方式并入本文。
技术领域
本发明涉及工业废水处理技术领域，尤其涉及一种脱硫废水处理系统及脱硫废水处理方法。
背景技术
SO 2是当今人类面临的主要大气污染物之一，空气中SO 2含量过高会引起酸雨，破坏农作物和建筑物。SO 2还会吸附在空气中的粉尘上，经呼吸道进入人体，严重损害人类健康。而绝大部分SO 2的排放来源于燃煤，例如：火力发电厂、工业燃煤、供暖等，在煤炭的燃烧过程中会产生大量的SO 2。
为了减少燃煤过程中SO 2的排放，烟气脱硫是目前被广泛采用的处理方式。例如：在燃煤电厂中，通常采用石灰石/石膏湿法烟气脱硫工艺对烟气进行脱硫处理。但湿法脱硫工艺中会产生大量含有固体悬浮物、重金属离子、高硬度且高污染的脱硫废水。
当前，为实现脱硫废水零排放，通常采用包括：化学预处理、浓缩减量、浓水末端处理三个阶段的处理技术。在现有技术中，由于化学预处理阶段所用的药剂成本较高，且在浓缩减量和浓水末端处理阶段中进行蒸发结晶的能耗成本高，造成脱硫废水零排放系统的运行成本高。
由此可知，现有技术中的脱硫废水零排放系统的运行成本高。
发明内容
本发明实施例提供一种脱硫废水处理系统及脱硫废水处理方法，以解决现有技术中脱硫废水零排放系统存在的运行成本高的问题。
为解决以上技术问题，本发明采用如下技术方案：
根据本发明的第一方面，提供了一种脱硫废水处理系统，所述脱硫废水处理系统应用于燃煤电厂，所述燃煤电厂产生的烟气通过烟气主管道依次通入脱硝装置、空气预热器、除尘器以及湿法脱硫吸收塔，然后被排放至外界，所述烟气主管道包括位于所述空气预热器的靠近所述脱硝装置一侧的第一侧管道和位于所述空气预热器的另一侧的第二侧管道，所述第一侧管道内的烟气温度大于所述第二侧管道内的烟气温度，所述脱硫废水处理系统包括：
与所述湿法脱硫吸收塔的出水口连通的预沉池，用于收集所述湿法脱硫吸收塔中的脱硫废水；
浓缩塔，所述浓缩塔的入水口与所述预沉池的出水口连通，所述浓缩塔的入风口与所述第二侧管道连通，用于利用所述第二侧管道内的烟气浓缩所述脱硫废水；
蒸发器，所述蒸发器的入水口与所述浓缩塔的出水口连通，所述蒸发器的入风口与所述第一侧管道连通，用于利用所述第一侧管道内的烟气蒸发干燥浓缩后的脱硫废水。
可选的，所述浓缩塔的出风口和所述蒸发器的出风口均与所述第二侧管道的位于所述空气预热器和所述湿法脱硫吸收塔之间的部分连通。
可选的，所述浓缩塔的入水口和出风口均设置于所述浓缩塔的顶部，所述浓缩塔的出水口和入风口均设置于所述浓缩塔的下部。
可选的，所述蒸发器的入风口和入水口均设置于所述蒸发器的顶部，所述蒸发器的出风口设置于所述蒸发器的底部。
可选的，所述浓缩塔的出水口与所述蒸发器的入水口之间连通有混凝沉淀装置，用于使浓缩后的脱硫废水经过所述混凝沉淀装置的澄清作用而分离出澄清液体和沉淀物，以将所述澄清液体排入所述蒸发器内。
可选的，所述混凝沉淀装置的出水口与所述蒸发器的入水口之间还设置有雾化器，用于将所述混凝沉淀装置排出的所述澄清液体经过雾化后排入所述蒸发器内。
可选的，所述雾化器为双流体雾化喷枪，所述双流体雾化喷枪包括空气压缩器和喷雾水泵，所述空气压缩器将所述喷雾水泵喷出的所述澄清液体雾化成粒径为20μm～200μm的水雾，其中，所述喷雾水泵连通所述混凝沉淀装置的 出水口和所述蒸发器的入水口，所述双流体雾化喷枪的出水口设置于所述蒸发器的入水口处。
可选的，所述浓缩塔的入风口与所述第二侧管道之间设置有增压风机，所述第二侧管道内的烟气经过所述增压风机增压后进入所述浓缩塔内。
根据本发明的第二方面，提供了一种脱硫废水处理方法，应用于燃煤电厂，所述燃煤电厂产生的烟气通过烟气主管道依次通入脱硝装置、空气预热器、除尘器以及湿法脱硫吸收塔，然后被排放至外界，所述烟气主管道包括位于所述空气预热器的靠近所述脱硝装置一侧的第一侧管道和位于所述空气预热器的另一侧的第二侧管道，所述第一侧管道内的烟气温度大于所述第二侧管道内的烟气温度，所述方法包括：
收集所述湿法脱硫吸收塔内的脱硫废水；
利用所述第二侧管道内的烟气对所述脱硫废水进行浓缩；
利用所述第一侧管道内的烟气对浓缩后的所述脱硫废水进行干燥，以使干燥后的所述脱硫废水干燥成晶体。
可选的，所述方法还包括：
将浓缩所述脱硫废水后的烟气排入所述湿法脱硫吸收塔内进行脱硫；
将蒸发所述脱硫废水后的烟气依次排入所述除尘器和所述湿法脱硫吸收塔，以进行除尘和脱硫。
在本发明实施例中，利用燃煤电厂排放的烟气在浓缩塔中对脱硫废水进行浓缩，在蒸发器中对浓缩后的脱硫废水进行蒸发，以实现脱硫废水的零排放。省略了对脱硫废水进行的化学预处理，因此节省了化学预处理的药剂成本，且利用燃煤电厂排放的能量对脱硫废水进行两次干燥处理，无需为脱硫废水的干燥提供能源，从而降低了处理脱硫废水的能耗，因此本发明实施例提供的脱硫废水处理系统能够降低处理脱硫废水的成本。
附图说明
为了更清楚地说明本发明实施例的技术方案，下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图仅仅是本发明的一些实施例，对于本领域普通技术人员来讲，在不付出创造性劳动 的前提下，还可以根据这些附图获得其他的附图。
图1是本发明实施例中燃煤电厂与脱硫废水处理系统的结构示意图；
图2是本发明实施例提供的一种脱硫废水处理系统的结构示意图；
图3是本发明实施例提供的一种脱硫废水处理方法的流程图；
图4是本发明实施例提供的另一种脱硫废水处理方法的流程图。
具体实施方式
下面将结合本发明实施例中的附图，对本发明实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例，都属于本发明保护的范围。
请参阅图1与图2，其中，图1是本发明实施例中燃煤电厂与脱硫废水处理系统的结构示意图；图2是本发明实施例提供的一种脱硫废水处理系统的结构示意图。脱硫废水处理系统，应用于燃煤电厂。
如图1所示，燃煤电厂产生的烟气通过烟气主管道11，依次通入脱硝装置12、空气预热器13、除尘器14以及湿法脱硫吸收塔15后排放至外界，烟气主管道11包括位于空气预热器13的靠近所述脱硝装置12一侧的第一侧管道111和位于空气预热器13的另一侧的第二侧管道112，第一侧管道111内的烟气温度大于第二侧管道112内的烟气温度。
如图1和2所示，所述脱硫废水处理系统包括：
与湿法脱硫吸收塔15的出水口(未图示)连通的预沉池21，用于收集湿法脱硫吸收塔15中的脱硫废水；
浓缩塔22，浓缩塔22的入水口221与预沉池21的出水口211连通，浓缩塔22的入风口222与第二侧管道112连通，用于利用第二侧管道112内的烟气浓缩所述脱硫废水；
蒸发器23，蒸发器23的入水口231与浓缩塔22的出水口223连通，蒸发器23的入风口232与第一侧管道111连通，用于利用第一侧管道111内的烟气蒸发干燥浓缩后的脱硫废水。
其中，燃煤电厂100的锅炉进行燃煤反应，从而产生温度很高的烟气，该 烟气中夹杂有粉尘、二氧化硫SO2，氮氧化合物(例如：NO2)，为了避免烟气污染环境，需要对烟气进行包括：脱硝、降温、除尘、脱硫在内的多种处理之后，才能排放至大气中。
另外，在降温之前，所述燃煤电厂排除的烟气的温度很高，例如：150℃至220℃之间，其可以称之为高温烟气。在降温之后，该烟气任然具有较高的余热，例如：90℃至110℃之间，其可以称之为低温烟气。
而且，通过浓缩塔22可以将脱硫废水体积浓缩60～80％，大大减少了进入蒸发器23中的脱硫废水的体积。
这样，先利用低温烟气对脱硫废水进行浓缩，以减少脱硫废水的含水量，从而减少脱硫废水的体积。再利用高温烟气将浓缩后的脱硫废水完全蒸发，达到废水零排放。可以减少对高温烟气的使用率，以避免降低锅炉的热效率。
可选的，如图1所示，燃煤电厂还设置有烟囱16，湿法脱硫吸收塔15与烟囱16连通，以将经过脱硝、降温、除尘、脱硫等处理后的烟气排放至大气中。
另外，脱硝装置12可以是选择性催化还原脱硝装置(SCR)(简称为如图2中所示的“SCR反应器”)，当然，其还可以是烟气再循环脱硝装置、选择性非催化还原脱硝装置(SNCR)等中的任意一种。
另外，空气预热器13可以称之为如图2中所示的“空预器”，所述空气预热器13可以利用烟气的温度对进入锅炉的空气进行预热，以在降低烟气温度的同时，还可以对该热量进行循环利用。
可选的，浓缩塔22的出风口224和蒸发器23的出风口233均与第二侧管道112的位于空气预热器13和湿法脱硫吸收塔15之间的部分连通。
其中，由于烟气通过湿法脱硫吸收塔15会带走部分水蒸气，因此，需要向湿法脱硫吸收塔15内补充工艺水，以确保湿法脱硫吸收塔15进行湿法脱硫的效率。将浓缩塔22的出风口233和蒸发器23的出风口224均与第二侧管道112连通，可以使浓缩塔22和蒸发器23内蒸发形成的水蒸气通过第二侧管道112进入湿法脱硫吸收塔15，以补充湿法脱硫吸收塔15内的水量。
这样，可以对脱硫废水内的水分进行循环利用，达到减少向湿法脱硫吸收塔内补充水量。
如图1所示，浓缩塔22的入风口222和出风口224均与第二侧管道112的位于除尘器14和湿法脱硫吸收塔15之间的部分连通。
本实施方式中，利用除尘后的烟气对脱硫废水进行浓缩，避免烟气中的粉尘进入脱硫废水中，造成对粉尘进行重复除尘，从而可以提升脱硫废水的处理效率。
另外，如图1所示，蒸发器23的出风口233与第二侧管道112的位于空气预热器13和除尘器14之间的部分连通。
其中，由于在蒸发器23中脱硫废水被完全蒸发，从而在烟气的吹动下，将脱硫废水干燥后残留的晶体吹入除尘器14，进行除尘。
本实施方式中，可以利用除尘器对脱硫废水结晶后的晶体进行收集，避免脱硫废水结晶后的晶体排放至外界而造成环境污染。
另外，脱硫废水干燥后残留的晶体通过除尘器的除尘后进入粉煤灰内，该晶体的质量较小，而锅炉排放的烟气的粉尘的质量较大，因此脱硫废水晶体不会影响粉煤灰的综合利用，不会产生晶体处置的问题，从而便于粉煤灰的循环利用。
可选的，浓缩塔22的入水口221和出风口224均设置于浓缩塔22的顶部，浓缩塔22的出水口223和入风口222均设置于浓缩塔22的下部。
其中，如图2所示，浓缩塔22的入风口222设置于浓缩塔22的下部，且位于浓缩塔内的液位之上。
另外，如图2所示，浓缩塔22内的上部设置有与入水口221连通的洒水装置225，用于增加脱硫废水与烟气之间的接触面积，以增加脱硫废水的浓缩效率。
这样，可以在脱硫废水和烟气之间进行逆向换热(即，脱硫废水和烟气在热量交换时沿相反的方向移动)，提升脱硫废水和烟气之间相对移动的速度，从而提升脱硫废水的浓缩效率。
另外，可以在浓缩塔22的入风口222处设置增压风机28，对进入浓缩塔22内的烟气进行增压，以增加烟气的流速，从而提升脱硫废水的浓缩效率。
可选的，蒸发器23的入风口232和入水口231均设置于蒸发器23的顶部，蒸发器23的出风口233设置于蒸发器23的底部。
这样，可以使蒸发器中的烟气与脱硫废水沿同一方向移动，使烟气将脱硫废水干燥并结晶之后，将获得的晶体从蒸发器的出风口吹出，使得烟气和晶体并一同进入除尘器中进行除尘，以防止脱硫废水的结晶后的晶体排放至大气中，从而便于收集脱硫废水的结晶后的晶体，提升所述脱硫废水处理系统的环保性能。
可选的，浓缩塔22的出水口223与蒸发器23的入水口231之间连通有混凝沉淀装置24，用于使浓缩后的脱硫废水经过混凝沉淀装置24的澄清作用而分离出澄清液体和沉淀物，以将所述澄清液体排入蒸发器23内。
这样，可以减少进入蒸发器内的脱硫废水中的杂质，减轻杂质回收的工作负担，并减少排放至外界的烟气中的杂质含量，提升脱硫废水处理系统的环保性能。
如图2所示，本实施方式中，利用了三联箱241、与三联箱241的出水口连通的浓缩澄清池242和与澄清池242的出水口连通的出水箱243作为混凝沉淀装置24，且出水箱243与蒸发器23的入水口231连通。
本实施方式中，利用燃煤电厂本身具有的三联箱对浓缩后的脱硫废水进行絮凝反应，并利用浓缩澄清池进行澄清，以分离出澄清液体和沉淀杂质。并将澄清液体排放至出水箱中，以供其流入蒸发器，从而去除进入蒸发器内的脱硫废水中的大颗粒悬浮物，便于对脱硫废水进行雾化时，不会因杂质过多或者杂质颗粒过大而堵塞喷雾出口。
另外，在浓缩澄清池中的沉淀杂质在沉淀至一定量之后，可以进行统一收集，从而便于收集脱硫废水中的杂质。
可选的，混凝沉淀装置24的出水口241与蒸发器23的入水口231之间还设置有雾化器25，用于将混凝沉淀装置24排出的所述澄清液体经过雾化后排入蒸发器23内。
这样，可以增加蒸发器内的脱硫废水与烟气之间的接触面积，大大提升增发脱硫废水的效率，从而提升了脱硫废水处理系统的整体工作效率。
可选的，雾化器25为双流体雾化喷枪，所述双流体雾化喷枪包括空气压缩器251(也可以称之为：压缩空气储罐)和喷雾水泵252，空气压缩器251将喷雾水泵252喷出的所述澄清液体雾化成粒径为20μm～200μm的水雾，其 中，所述喷雾水泵252连通混凝沉淀装置25的出水口253和蒸发器23的入水口231，所述双流体雾化喷枪的出水口253设置于蒸发器23的入水口231处。
其中，空气压缩器251内压缩空气的压力为0.2～0.7Mpa之间。
空气压缩器251内压缩的空气可以是第二侧管道112中的烟气。
这样，可以利用空气压缩器雾化脱硫废水，以大大增加脱硫废水与烟气的接触面积，从而提升烟气对脱硫废水的干燥效率。
可选的，如图2所示，预沉池21的入水口与湿法脱硫吸收塔15的出水口之间通过旋流器26连接。
这样，可以利用旋流器对脱硫废水进行离心沉降后，排入所述预沉池中，以使脱硫废水中的杂质与液体在预沉池中快速的分离。
可选的，在浓缩塔22的入水口221、入风口222以及蒸发器23的入风口232处设置阀门27，以控制进入浓缩塔22内的烟气量和水量，以及进入蒸发器23内的烟气量。
这样，可以根据烟气温度、脱硫废水量等的改变，调节各个阀门，以确保烟气能够将脱硫废水完全蒸发成水蒸气和晶体，避免蒸发不完全而达不到废水零排放，或者避免烟气通入量过多而增加了脱硫废水处理系统对高温烟气的消耗而影响锅炉的热效率，从而提升了脱硫废水处理系统的可靠性。
可选的，还可以在预沉池21的出水口处以及浓缩塔22的出水口223处设置污水泵29，以驱动脱硫废水流动。
这样，可以驱使脱硫废水流动，且可以驱动脱硫废水从低的位置向高的位置流动，减小对所述脱硫废水处理系统中各个装置的地势位置的限制，从而增加了所述脱硫废水处理系统的适用性。
在本发明实施例中，利用燃煤电厂排放的烟气在浓缩塔中对脱硫废水进行浓缩，在蒸发器中对浓缩后的脱硫废水进行蒸发，以实现脱硫废水的零排放。省略了对脱硫废水进行的化学预处理，因此节省了化学预处理的药剂成本，且利用燃煤电厂排放的能量对脱硫废水进行两次干燥处理，无需为脱硫废水的干燥提供额外的能源，从而降低了处理脱硫废水的能耗，因此本发明实施例提供的脱硫废水处理系统能够降低处理脱硫废水的成本。
请参阅图3，是本发明实施例提供的一种脱硫废水处理方法的流程图。该 方法应用于燃煤电厂，所述燃煤电厂产生的烟气通过烟气主管道依次通入脱硝装置、空气预热器、除尘器以及湿法脱硫吸收塔，然后被排放至外界，所述烟气主管道包括位于所述空气预热器的靠近所述脱硝装置一侧的第一侧管道和位于所述空气预热器的另一侧的第二侧管道，所述第一侧管道内的烟气温度大于所述第二侧管道内的烟气温度，所述方法包括：
步骤301、收集所述湿法脱硫吸收塔内的脱硫废水。
步骤302、利用所述第二侧管道内的烟气对所述脱硫废水进行浓缩。
步骤303、利用所述第一侧管道内的烟气对浓缩后的所述脱硫废水进行干燥，以使干燥后的所述脱硫废水干燥成晶体。
可选的，如图4所示，所述方法还包括：
步骤304、将浓缩所述脱硫废水后的烟气排入所述湿法脱硫吸收塔内进行脱硫。
步骤305、将蒸发所述脱硫废水后的烟气依次排入所述除尘器和所述湿法脱硫吸收塔，以进行除尘和脱硫。
本发明实施例提供的方法能够应用于如图1和图2提供的脱硫废水处理系统，且能够取得相同的有益效果，为避免重复，在此不再赘述。
以上，仅为本发明的具体实施方式，但本发明的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本发明揭露的技术范围内，可轻易想到变化或替换，都应涵盖在本发明的保护范围之内。因此，本发明的保护范围应以权利要求的保护范围为准。

Claims (10)

  1. 一种脱硫废水处理系统，所述脱硫废水处理系统应用于燃煤电厂，所述燃煤电厂产生的烟气通过烟气主管道依次通入脱硝装置、空气预热器、除尘器以及湿法脱硫吸收塔，然后被排放至外界，其特征在于，所述烟气主管道包括位于所述空气预热器的靠近所述脱硝装置一侧的第一侧管道和位于所述空气预热器的另一侧的第二侧管道，所述第一侧管道内的烟气温度大于所述第二侧管道内的烟气温度，所述脱硫废水处理系统包括：
    与所述湿法脱硫吸收塔的出水口连通的预沉池，用于收集所述湿法脱硫吸收塔中的脱硫废水；
    浓缩塔，所述浓缩塔的入水口与所述预沉池的出水口连通，所述浓缩塔的入风口与所述第二侧管道连通，用于利用所述第二侧管道内的烟气浓缩所述脱硫废水；
    蒸发器，所述蒸发器的入水口与所述浓缩塔的出水口连通，所述蒸发器的入风口与所述第一侧管道连通，用于利用所述第一侧管道内的烟气蒸发干燥浓缩后的脱硫废水。
  2. 根据权利要求1所述的系统，其特征在于，所述浓缩塔的出风口和所述蒸发器的出风口均与所述第二侧管道的位于所述空气预热器和所述湿法脱硫吸收塔之间的部分连通。
  3. 根据权利要求1所述的系统，其特征在于，所述浓缩塔的入水口和出风口均设置于所述浓缩塔的顶部，所述浓缩塔的出水口和入风口均设置于所述浓缩塔的下部。
  4. 根据权利要求1所述的系统，其特征在于，所述蒸发器的入风口和入水口均设置于所述蒸发器的顶部，所述蒸发器的出风口设置于所述蒸发器的底部。
  5. 根据权利要求1所述的系统，其特征在于，所述浓缩塔的出水口与所述蒸发器的入水口之间连通有混凝沉淀装置，用于使浓缩后的脱硫废水经过所述混凝沉淀装置的澄清作用而分离出澄清液体和沉淀物，以将所述澄清液体排入所述蒸发器内。
  6. 根据权利要求5所述的系统，其特征在于，所述混凝沉淀装置的出水口与所述蒸发器的入水口之间还设置有雾化器，用于将所述混凝沉淀装置排出的所述澄清液体经过雾化后排入所述蒸发器内。
  7. 根据权利要求6所述的系统，其特征在于，所述雾化器为双流体雾化喷枪，所述双流体雾化喷枪包括空气压缩器和喷雾水泵，所述空气压缩器将所述喷雾水泵喷出的所述澄清液体雾化成粒径为20μm～200μm的水雾，其中，所述喷雾水泵连通所述混凝沉淀装置的出水口和所述蒸发器的入水口，所述双流体雾化喷枪的出水口设置于所述蒸发器的入水口处。
  8. 根据权利要求1所述的系统，其特征在于，所述浓缩塔的入风口与所述第二侧管道之间设置有增压风机，所述第二侧管道内的烟气经过所述增压风机增压后进入所述浓缩塔内。
  9. 一种脱硫废水处理方法，应用于燃煤电厂，所述燃煤电厂产生的烟气通过烟气主管道依次通入脱硝装置、空气预热器、除尘器以及湿法脱硫吸收塔，然后被排放至外界，其特征在于，所述烟气主管道包括位于所述空气预热器的靠近所述脱硝装置一侧的第一侧管道和位于所述空气预热器的另一侧的第二侧管道，所述第一侧管道内的烟气温度大于所述第二侧管道内的烟气温度，所述方法包括：
    收集所述湿法脱硫吸收塔内的脱硫废水；
    利用所述第二侧管道内的烟气对所述脱硫废水进行浓缩；
    利用所述第一侧管道内的烟气对浓缩后的所述脱硫废水进行干燥，以使干燥后的所述脱硫废水干燥成晶体。
  10. 根据权利要求9所述的方法，其特征在于，所述方法还包括：
    将浓缩所述脱硫废水后的烟气排入所述湿法脱硫吸收塔内进行脱硫；
    将蒸发所述脱硫废水后的烟气依次排入所述除尘器和所述湿法脱硫吸收塔，以进行除尘和脱硫。
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