CN112246437B - Wet electrostatic dust collector and dust collection process with hydrothermal recovery and pollutant removal - Google Patents
Wet electrostatic dust collector and dust collection process with hydrothermal recovery and pollutant removal Download PDFInfo
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- CN112246437B CN112246437B CN202011043445.XA CN202011043445A CN112246437B CN 112246437 B CN112246437 B CN 112246437B CN 202011043445 A CN202011043445 A CN 202011043445A CN 112246437 B CN112246437 B CN 112246437B
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- 239000000428 dust Substances 0.000 title claims abstract description 61
- 238000000034 method Methods 0.000 title claims abstract description 47
- 238000011084 recovery Methods 0.000 title claims abstract description 27
- 239000003344 environmental pollutant Substances 0.000 title claims abstract description 20
- 231100000719 pollutant Toxicity 0.000 title claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 82
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 81
- 239000003546 flue gas Substances 0.000 claims abstract description 81
- 238000007791 dehumidification Methods 0.000 claims abstract description 34
- 238000010521 absorption reaction Methods 0.000 claims abstract description 9
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 5
- 230000023556 desulfurization Effects 0.000 claims abstract description 5
- 239000007788 liquid Substances 0.000 claims description 33
- 229920006395 saturated elastomer Polymers 0.000 claims description 30
- 239000007789 gas Substances 0.000 claims description 14
- 239000012719 wet electrostatic precipitator Substances 0.000 claims description 10
- 238000004064 recycling Methods 0.000 claims description 7
- 238000005406 washing Methods 0.000 claims description 6
- 239000002699 waste material Substances 0.000 claims description 6
- 230000002195 synergetic effect Effects 0.000 claims 4
- 230000008929 regeneration Effects 0.000 abstract description 7
- 238000011069 regeneration method Methods 0.000 abstract description 7
- 238000006243 chemical reaction Methods 0.000 abstract description 3
- 230000010354 integration Effects 0.000 abstract description 3
- 238000011010 flushing procedure Methods 0.000 description 10
- 239000000779 smoke Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 230000001172 regenerating effect Effects 0.000 description 4
- 239000002253 acid Substances 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 2
- KWGKDLIKAYFUFQ-UHFFFAOYSA-M lithium chloride Chemical compound [Li+].[Cl-] KWGKDLIKAYFUFQ-UHFFFAOYSA-M 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005684 electric field Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000000844 transformation Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
- B03C3/02—Plant or installations having external electricity supply
- B03C3/16—Plant or installations having external electricity supply wet type
-
- 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
- B01D53/1425—Regeneration of liquid 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
- 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
- B01D53/26—Drying gases or vapours
- B01D53/263—Drying gases or vapours by absorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
- B03C3/017—Combinations of electrostatic separation with other processes, not otherwise provided for
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
- B03C3/34—Constructional details or accessories or operation thereof
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
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Abstract
The invention discloses a wet electrostatic dust collector and a dust collection process which take hydrothermal recovery into consideration and remove pollutants, and belongs to the technical field of flue gas dust removal and dehumidification. The dust remover comprises a wet-electric dehumidification cooperative pollutant removal system, a moisture absorption working medium regeneration system and a moisture absorption working medium circulation system. The process method provided by the invention recovers moisture, dust and heat in flue gas after desulfurization by distributing a film on a wet electric anode plate by using a dehumidifying working medium; the exhaust steam of the steam turbine firstly heats a dilute working medium, then heats process water, and finally enters a wet electric dust collector to perform dehumidification reaction with the flue gas; the low-temperature process water sequentially cools the flue gas, the regenerated working medium, the dead steam and the regenerated steam to recover heat. The dehumidifying working medium designed by the invention washes the dust of the anode plate and simultaneously carries out hydrothermal recovery on the flue gas, so that the pollutants in the treated flue gas are deeply removed, and the water and the heat are effectively recycled. The equipment has high water heat recovery efficiency, high function integration level and less occupied area, can effectively improve the heat efficiency of the boiler, and solves the problem of compact layout of a power plant.
Description
Technical Field
The invention relates to an electrostatic dust removal device, belongs to the technical field of flue gas dust removal, and particularly relates to a wet electrostatic dust collector and a dust removal process which take hydrothermal recovery into consideration and remove pollutants.
Background
As industrial water consumers, most coal-fired power plants use a wet desulfurization process to remove SO from flue gas 2 In the process, the desulfurization slurry is heated and evaporated, and a large amount of moisture exists in the desulfurized flue gas in the form of water vapor, so that an important component of the water consumption of a power plant is formed.
Saturated wet flue gas after wet desulphurization enters a wet electric dust collector for deep dedusting and demisting, but the saturation state of the flue gas cannot be changed, and a small amount of gas pollutants still exist in the flue gas to be deeply removed. The saturated wet flue gas with the temperature of about 50 ℃ and the relative humidity of 100 percent is discharged after passing through the wet electric dust collector, because the temperature difference exists between the wet flue gas and the atmosphere, the water vapor in the saturated wet flue gas is condensed to form a white smoke phenomenon, and simultaneously, a small amount of SO exists in the saturated wet flue gas after wet desulphurization 3 The gas is condensed into acidic liquid when meeting the condensation, and the acidic liquid can corrode the internal structure of the chimney.
The method for carrying out hydrothermal recovery on the desulfurized flue gas is different from the traditional flue gas condensation by using the partial pressure difference of water vapor between the dehumidifying working medium and the flue gas as the mass transfer driving force, can reduce the superheat degree of the flue gas and change the flue gas from a saturated state to an unsaturated state, so that the limitation of the acid dew point of the flue gas can be avoided, and the deep dehumidification is realized. The treated smoke has improved superheat degree, enhanced diffusion capacity and capability of avoiding white smoke to a certain extent. Meanwhile, the dehumidifying working medium can react with a small amount of residual acid gas in the flue gas, so that the flue gas is subjected to hydrothermal recovery, the energy conservation of a power plant is facilitated, the flue gas can be deeply purified, the generation of 'white smoke' is avoided, and the method has important significance.
Most of the existing methods for treating desulfurized flue gas by adopting a dehumidifying solution need an absorption tower to provide a reaction site, and for the coal-fired flue gas with huge amount, the specification of the absorption tower is also huge, so that the method not only occupies large-area industrial land, but also has low equipment integration level, thereby greatly improving the process investment.
Disclosure of Invention
In order to solve the technical problems, the invention provides a wet electrostatic dust collector and a dust removal process which take account of hydrothermal recovery and removal of pollutants, and particularly adopts a dehumidifying working medium to directly contact with saturated wet flue gas after desulfurization to complete a heat and mass transfer process, so that most of water vapor in the flue gas is condensed to release heat and is transferred into a dehumidifying solution while pollutants in the flue gas are deeply removed and purified, and the recycling of the dehumidifying solution can be realized on the basis of fully reducing moisture, temperature and dust of the saturated wet flue gas.
In order to achieve the aim, the invention discloses a wet electrostatic dust collector with hydrothermal recovery and removal of pollutants, which comprises a wet electrostatic dust collector shell, a flue gas heat exchanger and a dehumidification area which are arranged in the shell in sequence from bottom to top, and a working medium circulation recovery device arranged outside the shell;
one end of the flue gas heat exchanger is connected with low-temperature process water, the other end of the flue gas heat exchanger is connected with a working medium circulation recovery device, the working medium circulation recovery device comprises a separator, a regenerator, a liquid-water heat exchanger, a steam-water heat exchanger and a condenser, one end of the separator is connected with a waste liquid discharge port positioned at the bottom end of the shell, the other end of the separator is connected with the regenerator, the regenerator is provided with an exhaust steam air inlet, a first exhaust port and a second exhaust port, the first exhaust port is connected with a second mass inlet of the liquid-water heat exchanger, and a second mass discharge port arranged on the liquid-water heat exchanger is connected with a working medium inlet of a dehumidification area through a pipeline; the first exhaust port is connected with one end of the steam-water heat exchanger through a first gas path, and the other end of the steam-water heat exchanger is connected with the wet electrostatic dust collector through a second gas path;
the low-temperature process water and saturated wet flue gas entering a wet electrostatic dust collector undergo preliminary heat exchange, then pass through a liquid-water heat exchanger and a steam-water heat exchanger, and finally are collected into a condenser;
and a second exhaust port of the regenerator is also connected with a condenser.
Furthermore, the dehumidification area comprises anode plates and cathode wires which are distributed in a staggered mode in sequence, and a liquid distributor located above the anode plates, and the liquid distributor is connected with the working medium inlet through a mass conveying pipe. Wherein, because the liquid distributor evenly distributes the membrane to dehumidification district anode plate surface for dehumidification working medium and saturated wet flue gas can better realize heat transfer, pass wet process. The liquid distributor is a conventional liquid distributor.
Furthermore, the working medium circulating and recycling device further comprises a concentrated working medium pool, and the working medium inlet is connected with the concentrated working medium pool.
Further, the concentrated working medium pool is connected with a second mass discharge port of the liquid-water heat exchanger.
Furthermore, the working medium circulation recovery device also comprises a dilute working medium pool positioned between the separator and the regenerator.
Furthermore, a steam exhaust inlet of the regenerator is connected with a steam turbine.
Furthermore, a washing area is arranged above the dehumidification area and comprises a nozzle, a washing pipe and a demister. The flushing zone is used for regular flushing of the apparatus. The demister is preferably a wire mesh demister or a ridge demister, the nozzle is preferably made of stainless steel or anticorrosive materials, and the inner surface of the nozzle is subjected to anticorrosive treatment.
In addition, the invention also discloses a dust removal process adopting the wet electrostatic dust collector, saturated wet flue gas after wet desulphurization is sent into the wet electrostatic dust collector and is subjected to primary heat exchange with low-temperature process water in a flue gas heat exchanger, and the cooled saturated wet flue gas is discharged out of the wet electrostatic dust collector after the processes of dust removal, moisture absorption and further heat exchange are completed in a dehumidification region;
the heated low-temperature process water sequentially flows through the liquid-water heat exchanger and the steam-water heat exchanger from front to back and is finally collected into the condenser;
and after moisture absorption of the saturated wet flue gas is finished, the working medium is recycled by the working medium recycling device and then is sent into the wet electrostatic dust collector again.
Furthermore, the temperature of the dehumidifying working medium is 40-50 ℃, the mass percentage concentration is 40-50%, the temperature of the saturated wet flue gas is 50 ℃, and the relative humidity is 100%.
Further, the dehumidifying working medium comprises an aqueous solution of at least one of calcium chloride, lithium chloride or lithium bromide.
The beneficial effects of the invention are mainly embodied in the following aspects:
1. the invention designs and adopts the dehumidifying working medium to directly contact with the desulfurized saturated wet flue gas to complete the heat and mass transfer process, and most of water vapor in the flue gas is condensed to release heat and is transferred into the dehumidifying solution while deeply removing and purifying the pollutants in the flue gas, so that the concentration of the dehumidified flue gas pollutants is reduced, the temperature is raised, the superheat degree is improved, and the diffusion capacity is enhanced, thereby fundamentally avoiding the phenomena of 'white smoke' and 'chimney rain' at the outlet of a chimney;
2. the dehumidifying working medium designed by the invention realizes cyclic utilization in the working medium circulating and regenerating device, meanwhile, the low-temperature process water in the flue gas heat exchanger for primary heat exchange can also realize heat and moisture recovery in the working medium circulating and regenerating device, and in addition, the system has stable operation, low energy consumption and no pollution;
3. the dehumidification system designed by the invention has high energy utilization rate, and the recovered hot water can be used for supplying water for families and heat supply networks;
4. the dehumidifying working medium designed by the invention can carry out deep dehumidifying and emission-reducing reaction with flue gas while washing dust on the anode dust collecting polar plate, the device has high function integration level, the device occupies less land, and the problem of compact layout of a power plant is effectively solved.
Drawings
FIG. 1 is a schematic structural diagram of a wet electrostatic precipitator in accordance with the present invention;
wherein, each part in fig. 1 is numbered as follows:
a shell 1 (wherein, a flue gas inlet 1.1, a waste liquid outlet 1.2 and a flue gas outlet 1.3);
a flue gas heat exchanger 2;
a dehumidification area 3 (wherein, an anode plate 3.1, a cathode wire 3.2, a liquid distributor 3.3 and a mass transfer tube 3.4);
a flushing zone 4 (wherein nozzles 4.1, flushing pipes 4.2, demisters 4.3);
the system comprises a working medium circulating regeneration device 5 (wherein, a separator 5.1, a regenerator 5.2 (wherein, a steam exhaust inlet 5.2a, a first exhaust port 5.2b, a first exhaust port 5.2c and a second exhaust port 5.2d), a liquid-water heat exchanger 5.3 (wherein, a second inlet 5.3a and a second exhaust port 5.3b), a steam-water heat exchanger 5.4, a condenser 5.5, a first gas circuit 5.6 and a second gas circuit 5.7).
Detailed Description
In order to better explain the invention, the following embodiments further illustrate the main content of the invention, but the invention is not limited to the following embodiments.
Example 1
The embodiment discloses a wet electrostatic precipitator considering hydrothermal recovery and removal of cooperative pollutants, as shown in fig. 1, the wet electrostatic precipitator includes a wet electrostatic precipitator casing 1, a flue gas inlet 1.1 and a waste liquid discharge port 1.2 which are located at the bottom of the casing 1, and a flue gas outlet 1.3 at the top, a flue gas heat exchanger 2 and a dehumidification region 3 are further respectively arranged in the casing 1 from bottom to top, one end of the flue gas heat exchanger 2 is connected with external low-temperature process water, the temperature of the low-temperature process water is usually lower than the temperature of saturated wet flue gas after wet desulphurization, the saturated wet flue gas can perform primary heat exchange with the low-temperature process water, so that primary temperature drop of the flue gas is realized, the other end of the flue gas heat exchanger 2 is connected with a working medium circulation and regeneration device 5, and the warmed low-temperature process water completes heat recovery in the working medium circulation and regeneration device 5.
As can be seen from fig. 1, the anode plate 3.1 and the cathode wire 3.2 are alternately arranged in the dehumidification region 3, the cathode wire 3.2 is connected to a high voltage power supply, and meanwhile, a liquid distributor 3.3 is further arranged above the anode plate 3.1, in this embodiment, the liquid distributor is preferably a conventional liquid distributor, each liquid outlet of the liquid distributor 3.3 is located above each anode plate 3.1, a liquid inlet of the liquid distributor 3.3 is connected to a mass transfer pipe 3.4, and the mass transfer pipe 3.4 is further connected to a concentrated working medium pool of the working medium circulation and regeneration device 5. The dehumidifying working medium flowing out of the liquid distributor 3.3 can be evenly coated on the surface of each anode plate 3.1, and the saturated wet flue gas and the dehumidifying working medium can fully exchange heat and transfer mass on the surface of the anode plate 3.1.
Meanwhile, the working medium circulating regeneration device 5 comprises a separator 5.1, a regenerator 5.2, a liquid-water heat exchanger 5.3, a steam-water heat exchanger 5.4 and a condenser 5.5, wherein one end of the separator 5.1 is connected with a waste liquid discharge port 1.2 positioned at the bottom end of the shell 1, and after the dehumidification working medium and the saturated wet flue gas fully exchange heat and transfer mass on the surface of the anode plate 3.1, the temperature and the concentration of the dehumidification working medium are reduced, and dust carried by the dehumidification working medium is discharged from the waste liquid discharge port 1.2 to the separator 5.1, so that primary impurity removal is realized; the other end of the separator 5.1 is connected with a regenerator 5.2, the regenerator 5.2 is provided with an exhaust steam inlet 5.2a, a first exhaust port 5.2b, a first exhaust port 5.2c and a second exhaust port 5.2d, wherein the exhaust steam inlet 5.2a is connected with a steam turbine and used for continuously conveying exhaust steam with a certain temperature to the regenerator 5.2, the first exhaust port 5.2c is connected with a second exhaust port 5.3a of the liquid-water heat exchanger 5.3, and the second exhaust port 5.3b arranged on the liquid-water heat exchanger 5.3 is connected with a working medium inlet of the dehumidification region 2 through a pipeline; the first exhaust port 5.2b is connected with one end of a steam-water heat exchanger 5.4 through a first gas path 5.6, and the other end of the steam-water heat exchanger 5.4 is connected with a wet type electrostatic dust collector through a second gas path 5.7; in addition, the other end of the flue gas heat exchanger 2 is connected with a liquid-water heat exchanger 5.3, the liquid-water heat exchanger 5.3 is connected with a steam-water heat exchanger 5.4, and the steam-water heat exchanger 5.4 is connected with a condenser 5.5.
Specifically, after the primary impurity removal by the separator 5.1, the working medium flows into the regenerator 5.2, the low-pressure environment is continuously realized in the regenerator 5.2 under the action of the vacuum pump, the working medium is heated by the exhaust steam firstly, and then the moisture is evaporated in the low-pressure environment, wherein the low-pressure environment is arranged in the regenerator 5.2, the working medium is heated and concentrated in the regenerator 5.2, and enters the liquid-water heat exchanger 5.3 through the first discharge port 5.2c on the regenerator 5.2 and the second inlet port 5.3a on the liquid-water heat exchanger 5.3 to perform heat exchange with the low-temperature process water flowing out of the flue gas heat exchanger 2, and after the temperature of the working medium is reduced, the working medium flows into a concentrated working medium pool between the liquid-water heat exchanger 5.3 and the wet electrostatic dust collector shell 1 from the second outlet port 5.3b on the liquid-water heat exchanger 5.3. The low-temperature process water after heat exchange in the liquid-water heat exchanger 5.3 flows into the steam-water heat exchanger 5.4, the gas in the steam-water heat exchanger 5.4 comes from a steam turbine connected with the regenerator 5.2 and flows out from a first exhaust port 5.2b of the regenerator 5.2, enters the liquid-water heat exchanger 5.3 through a gas path I5.6, the exhaust steam further performs heat exchange with the low-temperature process water flowing into the liquid-water heat exchanger 5.3, the exhaust steam after heat exchange enters the wet electrostatic dust collector through a gas path II 5.7, the temperature of the low-temperature process water in the liquid-water heat exchanger 5.3 is increased again and is collected into a condenser 5.5, and the recovery of water and heat is realized.
In addition, a dilute working medium pool can be arranged between the separator 5.1 and the regenerator 5.2, and a concentrated working medium pool and a working medium pump can be arranged between the liquid-water heat exchanger 5.3 and the mass transfer pipe 3.4. The mixed liquid discharged from the liquid outlet 1.2 of the shell 1 flows into the liquid distributor 3.3 along the mass conveying pipe 3.4 after being recycled and reused.
Meanwhile, because the dehumidifying working medium has certain corrosiveness, in order to avoid the corroding damage of the dehumidifying working medium to the anode plate 3.1 and the liquid distributor 3.3, in this embodiment, it is further preferable that a flushing area 4 is arranged at the upper part of the dehumidifying area 3, the flushing area 4 is provided with a flushing pipe 4.2, and the flushing pipe 4.2 is provided with a one-way valve. The one-way valve is opened irregularly to wash the surface of the dust collecting pole plate in the electric field area and the inner pipeline of the liquid distributor, which is beneficial to prolonging the service life of each device component. At the same time, the flushing pipe 4.2 is also provided with nozzles 4.1, each nozzle 4.1 opening towards the dehumidification zone 3, the flushing water sprayed from the nozzles 4.1 being drawn from the process water of the power plant. Preferably, the nozzle 4.1 is made of stainless steel or anticorrosive material, and the inner surface is subjected to anticorrosive treatment.
Example 2
The embodiment discloses a dust removal process, which comprises the steps of taking saturated wet flue gas, sending the saturated wet flue gas into the wet electrostatic dust collector, sequentially cooling the saturated wet flue gas by a heat exchanger in the dust collector, removing dust in a dehumidification area, recovering moisture and heat, removing liquid drops by a demister, obtaining flue gas after dust removal and dehumidification, collecting a dehumidification working medium by a liquid collector after moisture absorption, sending the dehumidification working medium into a working medium circulation and regeneration device, and recycling the dehumidification working medium.
In this example, the temperature of the saturated wet flue gas is selected to be about 50 ℃, the relative humidity is 100%, and NO is selected x 、SO 2 The content is 45mg/m respectively 3 And 30mg/m 3 (ii) a The temperature of the flue gas after dust removal and dehumidification is 53 ℃, the relative humidity is 70 percent, and NO is added x 、SO 2 The content is respectively 30mg/m 3 And 18mg/m 3 . The temperature of the inlet low-temperature process water is 25 ℃, and the temperature of the outlet is 53 ℃. The temperature of the dehumidifying working medium is 50 ℃, and the mass percentage concentration is 40%.
Example 3
The embodiment discloses a dust removal process, which comprises the steps of feeding saturated wet flue gas into a wet electrostatic dust collector, sequentially cooling the saturated wet flue gas by a heat exchanger in the dust collector, removing dust in a dehumidification area, recovering moisture and heat, removing liquid drops by a demister, obtaining the flue gas after dust removal and dehumidification, absorbing moisture of a dehumidifying working medium, collecting the dehumidifying working medium by a liquid collector, feeding the dehumidifying working medium into a working medium circulating and regenerating device, and regenerating and recycling the dehumidifying working medium.
In this example, the temperature of the saturated wet flue gas is selected to be about 50 ℃, the relative humidity is 100%, and NO is selected x 、SO 2 The content is 45mg/m respectively 3 And 30mg/m 3 (ii) a The temperature of the flue gas after dust removal and dehumidification is 50 ℃, the relative humidity is 67 percent, and NO is added x 、SO 2 The content is respectively 28mg/m 3 And 16mg/m 3 . The temperature of the inlet low-temperature process water is 25 ℃, and the temperature of the outlet is 54.7 ℃. The temperature of the dehumidifying working medium is 50 ℃, and the mass percentage concentration is 40%. The temperature of the dehumidifying working medium is 40 ℃, and the mass percentage concentration is 40%.
The above examples are merely preferred examples and are not intended to limit the embodiments of the present invention. In addition to the above embodiments, the present invention has other embodiments. All technical solutions formed by adopting equivalent substitutions or equivalent transformations fall within the protection scope of the claims of the present invention.
Claims (9)
1. A wet electrostatic dust collector giving consideration to hydrothermal recovery and removal of pollutants is characterized by comprising a wet electrostatic dust collector shell (1), a flue gas heat exchanger (2) and a dehumidification area (3) which are positioned in the shell (1) and sequentially arranged from bottom to top, and a working medium circulating and recovering device (5) positioned outside the shell (1);
one end of the flue gas heat exchanger (2) is connected with low-temperature process water, the other end is connected with a working medium circulating and recovering device (5), the working medium circulating and recycling device (5) comprises a separator (5.1), a regenerator (5.2), a liquid-water heat exchanger (5.3), a steam-water heat exchanger (5.4) and a condenser (5.5), wherein, one end of the separator (5.1) is connected with a waste liquid outlet (1.2) positioned at the bottom end of the shell (1), the other end is connected with a regenerator (5.2), the regenerator (5.2) is provided with a dead steam inlet (5.2 a), a first exhaust port (5.2 b), a first exhaust port (5.2 c) and a second exhaust port (5.2 d), the first discharge port (5.2 c) is connected with a second inlet port (5.3 a) of the liquid-water heat exchanger (5.3), a second mass discharge port (5.3 b) arranged on the liquid-water heat exchanger (5.3) is connected with a working medium inlet of the dehumidification area (3) through a pipeline; the first exhaust port (5.2 b) is connected with one end of a steam-water heat exchanger (5.4) through a first gas path (5.6), and the other end of the steam-water heat exchanger (5.4) is connected with a wet type electrostatic dust collector through a second gas path (5.7);
the low-temperature process water and saturated wet flue gas entering a wet electrostatic dust collector undergo preliminary heat exchange, then pass through a liquid-water heat exchanger (5.3) and a steam-water heat exchanger (5.4) and finally are collected into a condenser (5.5);
the second exhaust port (5.2 d) of the regenerator (5.2) is also connected with a condenser (5.5);
the low-temperature process water is process water with the temperature of 25 ℃.
2. The wet electrostatic precipitator for removing synergistic pollutants for hydrothermal recovery according to claim 1, wherein the dehumidification section (3) comprises anode plates (3.1) and cathode wires (3.2) which are sequentially distributed in a staggered manner, and a liquid distributor (3.3) which is positioned above the anode plates (3.1), and the liquid distributor (3.3) is connected with a working medium inlet through a mass transfer pipe (3.4).
3. The wet electrostatic precipitator for removing synergistic pollutants for hydrothermal recovery as claimed in claim 1 or 2, wherein the working medium circulation recovery device (5) further comprises a concentrated working medium pool, and the working medium inlet is connected with the concentrated working medium pool.
4. The wet electrostatic precipitator with consideration to hydrothermal recovery and synergistic pollutant removal according to claim 3, wherein the concentrated working medium pool is connected with the second mass discharge port (5.3 b) of the liquid-water heat exchanger (5.3).
5. The wet electrostatic precipitator with consideration of hydrothermal recovery and synergistic pollutant removal according to claim 1, 2 or 4, characterized in that the working medium circulation recovery device (5) further comprises a dilute working medium pool located between the separator (5.1) and the regenerator (5.2).
6. Wet electrostatic precipitator for combined hydrothermal recovery and removal of pollutants as claimed in claim 1, 2 or 4, wherein the steam exhaust inlet (5.2 a) of the regenerator (5.2) is connected to a steam turbine.
7. The wet electrostatic precipitator for combined hydrothermal recovery and co-pollutant removal according to claim 1, 2 or 4, wherein a washing zone (4) is further arranged above the dehumidification zone (3), and the washing zone (4) comprises nozzles (4.1), washing pipes (4.2) and demisters (4.3).
8. A dust removal process of a wet electrostatic dust collector as claimed in claim 1, wherein saturated wet flue gas after wet desulfurization is sent into the wet electrostatic dust collector, and is subjected to primary heat exchange with low-temperature process water in a flue gas heat exchanger (2), and the cooled saturated wet flue gas is discharged out of the wet electrostatic dust collector after dust removal, moisture absorption and further heat exchange in a dehumidification area (3);
the heated low-temperature process water sequentially flows through a liquid-water heat exchanger (5.3), a steam-water heat exchanger (5.4) and a condenser (5.5) from front to back and is finally collected into a hot water pool;
and after moisture absorption of the saturated wet flue gas is finished, the working medium is recycled by the working medium recycling device (5) and then is sent into the wet electrostatic dust collector again.
9. The dust removal process of the wet electrostatic dust collector of claim 8, wherein the temperature of the dehumidifying working medium is 40-50 ℃, the mass percentage concentration is 40-50%, the temperature of the saturated wet flue gas is 50 ℃, and the relative humidity is 100%.
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| CN106766160A (en) * | 2016-12-22 | 2017-05-31 | 张承虎 | A kind of complete hot heat recovery system of wet waste gas of absorption type heat |
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| JPH0435720A (en) * | 1990-05-31 | 1992-02-06 | Mitsubishi Heavy Ind Ltd | Method for recovering heat in apparatus for wet-desulfurizing stack gas |
| US5146755A (en) * | 1991-01-25 | 1992-09-15 | Abdelmalek Fawzy T | Method for reducing flue gas acid vapor emissions and energy recovery |
| CN101245400B (en) * | 2008-03-19 | 2010-07-21 | 中国科学院力学研究所 | Steelmaking converter gas dry recovery and sensible heat power generation system |
| CN203572285U (en) * | 2013-11-28 | 2014-04-30 | 灵宝金源矿业股份有限公司 | Outlet smoke residual heat recovery device of electric dust collector |
| CN106591887B (en) * | 2016-10-27 | 2018-09-11 | 武汉光谷环保科技股份有限公司 | A kind of aluminium cell side wall device for generating power by waste heat based on organic flash distillation cycle |
| CN206771805U (en) * | 2017-04-27 | 2017-12-19 | 昊姆（上海）节能科技有限公司 | A kind of eliminating white smoke type open absorption heat pump system for industrial waste gas waste heat recovery |
| CN107297113B (en) * | 2017-07-06 | 2019-10-11 | 常州大学 | A waste gas waste heat recovery and pollutant comprehensive treatment system |
| CN206950940U (en) * | 2017-07-20 | 2018-02-02 | 江苏民生重工有限公司 | High energy efficiency flue gas desulphurization system |
| CN107777820B (en) * | 2017-11-07 | 2021-08-10 | 西安协力动力科技有限公司 | Process for applying waste heat of exhaust steam of air cooling island to zero discharge treatment of wastewater of thermal power plant |
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