CN110465163B - Ceramic membrane-based flue gas water capturing device and ceramic membrane cleaning process - Google Patents

Ceramic membrane-based flue gas water capturing device and ceramic membrane cleaning process Download PDF

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Publication number
CN110465163B
CN110465163B CN201910773579.8A CN201910773579A CN110465163B CN 110465163 B CN110465163 B CN 110465163B CN 201910773579 A CN201910773579 A CN 201910773579A CN 110465163 B CN110465163 B CN 110465163B
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ceramic membrane
water
flushing
flue gas
cleaning
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CN110465163A (en
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肖海平
袁宗海
李建
高丹
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North China Electric Power University
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North China Electric Power University
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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
    • B01D46/54—Particle separators, e.g. dust precipitators, using ultra-fine filter sheets or diaphragms
    • B01D46/543—Particle separators, e.g. dust precipitators, using ultra-fine filter sheets or diaphragms using membranes
    • 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
    • B01D53/22—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 diffusion
    • 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
    • B01D53/268—Drying gases or vapours by diffusion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
    • 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
    • B01D53/22—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 diffusion
    • B01D2053/221—Devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/80—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/04—Backflushing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/16—Use of chemical agents
    • B01D2321/168—Use of other chemical agents

Abstract

The invention belongs to the technical field of flue gas water capture, and particularly relates to a flue gas water capture device based on a ceramic membrane and a ceramic membrane cleaning process. The flue gas water-catching device comprises a ceramic membrane unit, a chemical cleaning unit, a gas-liquid alternative back flushing unit and a low-temperature process spraying unit, solves the problems of large water consumption, unclean cleaning and chemical cleaning agent consumption in mechanical cleaning, solves the problem of pollution to the environment caused by tiny fine particles and acid gas in flue gas, and further improves the capture efficiency of a ceramic membrane component on water vapor.

Description

Ceramic membrane-based flue gas water capturing device and ceramic membrane cleaning process
Technical Field
The invention belongs to the technical field of flue gas water capture, and particularly relates to a flue gas water capture device based on a ceramic membrane and a ceramic membrane cleaning process.
Background
As the flue gas at the FGD outlet is fully sprayed by the desulfurization slurry, the water vapor in the flue gas is in a supersaturated state, and the flue gas is discharged into the atmosphere through a chimney, so that a large amount of water resource waste is caused, and the flue gas contains a large amount of tiny particles, acid gas and the like, so that the flue gas is also greatly harmful to the environment. Therefore, many people now study how to capture the water vapor in the part of the flue gas, wherein the ceramic membrane technology is a method which is more advantageous in the existing water capturing technology, but in the ceramic membrane water capturing technology, membrane holes with tiny pore diameters are easy to be blocked by pollutants, tiny fine particles can be attached to the surface of the membrane, and some of the tiny fine particles can be gathered in the membrane holes, so that the permeability flow rate of the tiny fine particles is obviously reduced, a flushing device is usually used in the ceramic membrane filtration technology, and the pollutants on the surface of the ceramic membrane are removed in time, so that the permeability flow rate is kept stable.
The existing ceramic membrane module flushing method has the following four methods. Mechanical cleaning method: the mechanical cleaning comprises back flushing, negative pressure cleaning, soaking, mechanical scraping and the like, wherein the back flushing is a common cleaning method, and the ceramic membrane is reversely flushed by gas or liquid with certain pressure to separate pollutants on the outer surface of the membrane, so that the flux of the ceramic membrane is recovered; negative pressure cleaning is to form negative pressure on the outer side of the ceramic membrane, and the pollutants on the surface and the pores are separated through pressure difference; the mechanical scraping method is to wipe the film surface repeatedly through soft materials to remove pollutants mechanically. Chemical cleaning method: according to the property of the scale layer on the surface of the ceramic membrane, selecting a proper chemical cleaning agent, dissolving the scale layer and removing the scale layer, wherein the common chemical cleaning agent comprises acid alkali solution, chelating agent, oxidant and surfactant, and the cleaning agents are aimed at different scale layers, such as acid liquor for mainly removing calcium carbonate, calcium phosphate and metal oxide respectively; the alkali liquor mainly removes grease, protein and algae substances; chelating agents are commonly used to remove alkaline earth metal sulfates; the oxidizing agent is used for removing organic matters and microorganisms. Ultrasonic cleaning method: the ceramic membrane which is polluted is put into a special ultrasonic cleaning device for cleaning, and water is used as a flushing medium. Ultrasonic cleaning has a strong penetrability to ceramic membranes, so many students now have conducted intensive studies abroad. Electric field cleaning method: an electric field is applied to the ceramic membrane, charged particles and molecules in the pollutants move directionally along the direction of the electric field, and periodic energization is conducted to repeatedly remove the pollutants.
The permeability of the ceramic membrane component is improved to a certain extent in the prior art, however, the process requirement cannot be met by a cleaning technology at times. Mechanical cleaning method: a large amount of flushing water is required to be repeatedly flushed in the mechanical cleaning process, so that the water consumption is high; and the contaminants having strong adhesion cannot be removed by the washing of the washing water. Chemical cleaning method: in the chemical cleaning process, the corresponding chemical cleaning agent is required to be used for the pollutants of the ceramic membrane, and the single cleaning liquid cannot be removed for the scale layer formed by a plurality of pollutants, and the ceramic membrane is required to be repeatedly cleaned by a plurality of cleaning liquids. In addition, the flow rate of the cleaning liquid and the like are strictly controlled, so that irreversible damage to the ceramic membrane is avoided. Ultrasonic cleaning method: ultrasonic cleaning requires placing the ceramic membrane in a special cleaning device, which is inconvenient in terms of engineering application and also increases the cost of the equipment. Electric field cleaning method: the electric field cleaning method must use a conductive film and install electrodes on the ceramic film, so that the cost and maintenance costs of the entire apparatus are increased.
The invention combines the advantages and disadvantages of various cleaning processes, and can further improve the cleaning effect of the ceramic membrane.
Disclosure of Invention
Technical problem to be solved by the invention
The invention aims to provide a flue gas water-capturing device based on a ceramic membrane and a ceramic membrane cleaning process, which solve the problems of large water consumption, uncleanness in cleaning and dosage of chemical cleaning agents in the prior art. Further improving the water supplementing efficiency.
Method for solving technical problems
In order to solve the above problems, the present invention provides a flue gas water capturing device based on a ceramic membrane, which comprises a ceramic membrane unit, wherein the ceramic membrane unit is provided with a ceramic membrane assembly, and the flue gas water capturing device comprises: the device comprises a chemical cleaning unit, a gas-liquid alternating back flushing unit and a low-temperature process spraying unit, wherein the chemical cleaning unit is used for cleaning a severe scaling area of the front row of the ceramic membrane component; the gas-liquid alternating back flushing unit is arranged on the ceramic membrane tube and is used for back flushing all the ceramic membrane components; the low-temperature process spraying unit is used for reducing the temperature of the flue gas and improving the supersaturation degree of the water vapor.
According to a second aspect of the present invention, there is provided a cleaning device for a flue gas water-catching ceramic membrane, comprising: the device comprises a chemical cleaning unit, a gas-liquid alternating back flushing unit and a low-temperature process spraying unit, wherein the chemical cleaning unit is used for cleaning a severe scaling area of the front row of the ceramic membrane component; the gas-liquid alternating back flushing unit is arranged on the ceramic membrane tubes of the ceramic membrane assemblies and is used for back flushing all the ceramic membrane assemblies; the low-temperature process spraying unit is used for reducing the temperature of the flue gas and improving the supersaturation degree of the water vapor.
In one embodiment, pressure measuring elements are provided before and after the ceramic membrane module.
In one embodiment, the low-temperature process spraying unit comprises a cooling device and an atomization nozzle, wherein the atomization nozzle is arranged in a flue before flue gas flows through the ceramic membrane unit.
According to a third aspect of the invention, there is provided a ceramic membrane-based flue gas water capture process comprising a low temperature process water spraying process, a chemical cleaning process and a gas-liquid alternate backwash process.
In one embodiment, chemical cleaning is adopted for the front-row membrane module tube bundle, and cleaning agent is added into flushing water, wherein the cleaning agent contains a high molecular polymer with a certain concentration.
One embodiment is to control the start and stop of the whole chemical cleaning process flushing by pressure difference, and install pressure measuring elements in front and back of the ceramic membrane component.
In one embodiment, after the chemical cleaning process is completed, a back flushing process is initiated by first back flushing the ceramic membrane module with compressed air and then back flushing.
In one embodiment, the flushing water is first sufficiently cooled by the cooling treatment device.
In one embodiment, in the process of spraying the process water, the process water is sprayed into a flue after being cooled by a supercooling device.
The beneficial effects of the invention are that
Solves the problem of large water consumption for mechanical cleaning: by mechanical cleaning alone, the particles with relatively strong adhesion are only washed for a long time, so that the water consumption is increased.
Solves the problems of uncleanness of mechanical cleaning and dosage of chemical cleaning agents: some scale layers cannot be removed by mechanical cleaning, and a chemical cleaning method is required, so that the chemical cleaning method often causes the problem of large consumption of chemical cleaning liquid.
Solves the pollution problem of tiny fine particles and acid gas in the flue gas to the environment: the ceramic membrane component is similar to a tubular demister, has a certain removal effect on solid particles and acid gases in flue gas, but fine particles with the particle size of 0.1-1 mu m cannot be removed, PM2.5 hazard which aggravates the environment is discharged, and the flue gas contains HCl and H 2 SO 4 The discharge of the acid gas to the atmosphere increases the possibility of acid rain;
further improve ceramic membrane module to the problem of vapor capture efficiency: the flue gas is in a saturated state, but the grain size of the vapor in the flue gas is tiny, and when the vapor passes through the ceramic membrane component, the probability of contacting the ceramic membrane component is small, and the probability of being captured is also small.
Further features of the invention will become apparent from the following description of exemplary embodiments.
Drawings
Fig. 1 is a composition diagram and a process flow diagram of the apparatus of the present application.
Detailed Description
An embodiment of the present disclosure will be specifically described below, but the present disclosure is not limited thereto.
Referring to fig. 1: the flue gas forms steam saturated flue gas after FGD, water vapor is captured by a membrane component, captured water enters a water capturing recovery tank, a part of water can be used for flushing, the water is pumped to a flushing water tank by a water pump, and the rest part of water and the recovered flushing water are directly used as process makeup water of FGD. The flushing device consists of chemical cleaning and gas-liquid alternative back flushing, wherein the chemical cleaning is used for cleaning a severe pollution area of the front row of the ceramic membrane component by adding a special cleaning agent, and the gas-liquid alternative back flushing is used for comprehensively flushing by using pressure-sink air and flushing water with certain pressure and temperature. The low-temperature process spraying device is arranged in front of the ceramic membrane component, low-temperature process water and backwash water pass through the low-temperature treatment device, and pressure measuring elements are arranged in front of and behind the ceramic membrane component and used for controlling the start and stop of chemical cleaning.
The flushing process of the invention mainly comprises three parts:
the first part is a chemical wash. As the particles in the FGD outlet flue gas are mainly S, ca and Mg compounds, the vast majority of the particles are CaSO 4 And MgSO 4 Has strong adhesiveness. Ceramic membrane modules resemble tube-type demisters, with a large number of CaSOs 4 、MgSO 4 The fine particles adhere to the ceramic membrane module, the probability of adhesion of the front row is greatest because the front row is contacted with the fine particles first, and the subsequent scaling is easier and substantially 90% of CaSO is achieved once the front row is adhered with the fine particles 4 And MgSO 4 Will adhere intensively to the front rows of tube bundles of the ceramic membrane module. Simple mechanical cleaning is not capable of preventing the scale layer with relatively high adhesionFor removing the tube bundles of the front-row membrane assembly, a chemical cleaning method is adopted, the outer sides of the front rows of the ceramic membrane assembly are washed, a cleaning agent is added in the washing water, the cleaning agent is a high-molecular polymer with a certain concentration, and the polymer is mainly used for CaSO (carbon dioxide) 4 And MgSO 4 The scale layer, a large number of carboxyl groups, substituted amide groups and sulfonic acid groups in the high molecular polymer contain oxygen atoms, nitrogen atoms and sulfur atoms of lone pair electrons to carry out complex reaction with calcium ions, and in the dissolution balance of calcium sulfate scale, calcium ions and sulfate ions, the concentration of the calcium ions is reduced by a cleaning agent, and the calcium sulfate scale is continuously dissolved, so that the purpose of removing the calcium sulfate scale is achieved. The method is characterized in that the starting and stopping of the whole flushing are controlled by differential pressure, pressure measuring elements are arranged in front of and behind a ceramic membrane module, flushing starting differential pressure is set to be delta P0, the setting range is between 130pa and 150pa according to rated parameters and running conditions of a unit, when the differential pressure of the front and the rear of the ceramic membrane module exceeds delta P0, the outer sides of the front rows of the ceramic membrane module are started to clean the heavy scaling areas, chemical pre-cleaning is carried out, meanwhile, a three-way valve below the ceramic membrane module is opened to a flushing water recovery tank, flushing water with cleaning agents and pollutants is collected to the flushing water recovery tank, and the influence on the water quality of water is prevented. And stopping the chemical cleaning device when the front-rear differential pressure reaches delta P1, wherein the delta P1 is set to be in a range of 80-95 pa according to the actual running condition of the unit. In the chemical cleaning process, not only the pollutant with firm scaling is cleaned, but also the consumption of flushing water in the back flushing process can be reduced.
The second part is gas-liquid alternate back flushing. The back flushing device is arranged on all ceramic membrane tubes, after the chemical cleaning device is stopped, the lower end of the ceramic membrane assembly is subjected to sealing treatment, namely, an automatic lifting piston is arranged at the lower end of the ceramic membrane tube, the back flushing device is started after the chemical cleaning is finished in a control logic, and the back flushing device is started when the sealing is finished. The gas-liquid alternate backwash process is as follows: firstly, introducing compressed air with certain pressure and temperature to reversely purge the ceramic membrane component, wherein the temperature of the compressed air is normal temperature, the temperature of the compressed air can be kept between 25 ℃ and 30 ℃ generally, the pressure can be raised to 0.4MP to 0.5MP, and the purging time is according to the load of a unit and the actual running condition of a desulfurization systemSetting the settable range to 40 s-70 s; after the back purging is finished, flushing water with certain pressure and temperature is introduced to perform comprehensive back flushing, the flushing water is fully cooled by cooling treatment equipment, the cooling temperature is reduced to below 20 ℃, the pressure is raised to 0.3-0.4 MP, the flushing time is consistent with the purging time, the back flushing device is stopped for about 60 seconds, and after the water is captured, the three-way valve is opened to the water capturing tank after the pollutant near the three-way valve is completely flushed. The washing water is cooled, SO that the temperature of the washing water for washing is far lower than the temperature of the flue gas, the flue gas can be cooled locally to a certain extent, and along with the reduction of the temperature, the supersaturation degree of the flue gas is increased, and a large amount of water vapor, HCl and H2SO exist 4 The acid gases are condensed on the surface of the membrane component, so that the water capturing capacity can be increased to a certain extent, and meanwhile, the emission of the acid gases is reduced. In addition, in the gas-liquid alternative back flushing process, the compressed air is firstly used for cleaning, and then the flushing water is used for cleaning, so that the consumption of the flushing water is reduced.
The third part is to set low temperature process water spraying device. Introducing a process water spraying device at the position 3 meters in front of the ceramic membrane component, cooling the process water by using an advanced supercooling device, cooling the temperature to below 20 ℃, spraying the water according to the flue gas amount, wherein the flue gas at the FGD outlet is in a water vapor saturation state, the sprayed cooling water amount is according to the unit load and the flue gas amount, for example, a 60MW unit operates under the load of about 80%, the sprayed flow of low-temperature process water can be 3-3.5 t/h, the effect of the low-temperature process water is to cool the flue gas, and the supersaturation degree of the water vapor in the flue gas is further improved.
The fine particles having a particle size of 0.1 to 1 μm are hardly removed, and the emission into the atmosphere aggravates the PM2.5 pollution. The ceramic membrane component is similar to a tubular demister, and can remove solid particles in flue gas to a certain extent, caSO 4 The fine particles have strong hydrophilicity, in the supersaturated state of water vapor, the fine particles are easily activated by the water vapor to form nucleation centers, liquid drop crystal embryos are formed on the surfaces of the particles, the crystal embryos continue to grow up to form large liquid drops under the supersaturated condition, and the liquid drops containing the particles are condensed to form more particles under the actions of thermophoresis, turbulence, fluid drag force and the likeThe large aggregate increases the particle size of 0.1-1 mu m to more than 2 mu m, increases the probability of interception and capture when encountering a ceramic membrane component, reduces the direct discharge of solid fine particles in the flue gas, and effectively relieves the harm of PM 2.5; the temperature of the flue gas is further reduced, and meanwhile, the condensation of acid gas in the flue gas is also improved, and HCl and H in the flue gas are reduced 2 SO 4 And the emission amount of the acid rain is reduced.
The low-temperature process water spraying device solves the problem of emission of tiny particles and acid gas in the flue gas, and greatly improves the water capturing efficiency of the ceramic membrane component. The low-temperature process water reduces the flue gas temperature, improves the flue gas supersaturation degree, changes the phase of the water vapor, and a large amount of water vapor starts to condense into small liquid drops, and the small liquid drops are continuously combined with the water vapor to grow up in the supersaturation state and are captured on the ceramic membrane component, so that the water capturing efficiency of the ceramic membrane component is further improved. For example, in one embodiment of the low-temperature process water spraying procedure, the temperature of the flue gas at the outlet of the desulfurization system is about 50 ℃, the steam is in a saturated state, the temperature of the flue gas is reduced by 3-6 ℃ by spraying the low-temperature process water, and the supersaturation degree of the steam in the flue gas is further improved by the sprayed steam. The invention reduces the temperature of the flue gas, improves the supersaturation degree of water vapor in the flue gas and promotes CaSO with the grain diameter smaller than 15 mu m by spraying low-temperature process water 4 、MgSO 4 When the particles grow up, then flow around the ceramic membrane component when passing through the ceramic membrane component, under the action of inertia force, the particles with larger particle size have higher probability to contact with the ceramic membrane component, are further captured, and have remarkable effect on removing fog drops with particle size smaller than 15 mu m. The captured particles are adhered on the ceramic membrane component, can be easily removed by the ceramic membrane flushing device, and the ceramic membrane has smooth wall, simple flushing and high flushing efficiency.
Industrial applicability
The mechanical cleaning technology and the chemical cleaning technology are effectively combined, so that the water consumption of mechanical cleaning and the consumption of chemical cleaning agents are reduced, and the cleaning efficiency is improved; the back flushing adopts gas-liquid alternative flushing, further improves flushing efficiency, and simultaneously reduces flushing water consumption.
This application has adopted low temperature to spout and has shone the device, cools down the flue gas, further improves the flue gas supersaturation degree, has following several effects: the growth of fine particles with the particle size of 0.1-1 mu m can be promoted, so that the particles are captured by a membrane component, and the harm of the PM2.5 in the atmosphere is improved; the probability of phase change of the water vapor is increased, the water vapor is condensed into small droplets which are continuously grown and captured on the membrane component, and the water capturing efficiency of the membrane component is improved; the condensation effect of the acid gas is increased, the acid gas and the water vapor are captured together, and the emission amount of the acid gas is reduced.
The present invention is not limited to the preferred embodiments, and any changes or substitutions that would be apparent to one skilled in the art within the scope of the present invention are intended to be included in the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the protection scope of the claims.

Claims (3)

1. The utility model provides a flue gas water trap based on ceramic membrane, includes ceramic membrane unit, and ceramic membrane unit has ceramic membrane subassembly, its characterized in that includes: the device comprises a chemical cleaning unit, a gas-liquid alternating back flushing unit and a low-temperature process spraying unit, wherein the chemical cleaning unit is used for cleaning a severe scaling area of the front row of the ceramic membrane component; the gas-liquid alternating back flushing unit is arranged on the ceramic membrane tube and is used for back flushing all the ceramic membrane components; the low-temperature process spraying unit is used for reducing the temperature of the flue gas and improving the supersaturation degree of the water vapor;
the flue gas water catching process of the flue gas water catching device comprises the following steps: a low-temperature process water spraying procedure, a chemical cleaning procedure and a gas-liquid alternative back flushing procedure:
the chemical cleaning procedure is as follows: the method comprises the steps of controlling the start and stop of the whole flushing through differential pressure, installing a pressure measuring element in front of and behind a ceramic membrane module, setting flushing start differential pressure to be delta P0, setting the range to be 130 pa-150 pa, starting the outer cleaning of a plurality of rows before the starting when the differential pressure of the front and the rear of the ceramic membrane module exceeds delta P0, carrying out chemical pre-cleaning of a severe scaling area, and simultaneously, opening a three-way valve below the ceramic membrane module to a flushing water recovery tank to collect flushing water with cleaning agents and pollutants into the flushing water recovery tank to prevent the flushing water with cleaning agents and pollutants from influencing the water quality of water capture; stopping the chemical cleaning device when the front-rear differential pressure reaches delta P1, wherein the delta P1 is set to be 80-95 pa;
the gas-liquid alternate back flushing procedure comprises the following steps: firstly, introducing compressed air to reversely purge the ceramic membrane component, wherein the temperature of the compressed air is normal temperature, the temperature is kept between 25 ℃ and 30 ℃, the pressure can be raised to 0.4-0.5 MP, and the purging time is set to be 40-70 s; after the back purging is finished, flushing water is introduced to perform comprehensive back flushing, the flushing water is fully cooled by cooling treatment equipment, the cooling temperature is reduced to below 20 ℃, the pressure is raised to 0.3-0.4 MP, the flushing time is consistent with the purging time, the back flushing device is stopped for about 60 seconds, and after the water is captured, the three-way valve is opened to the water capturing water tank after the pollutants near the three-way valve are completely flushed;
the low-temperature process water spraying procedure is as follows: introducing a process water spraying device at the position 3 meters in front of the ceramic membrane component, cooling the process water by using an advanced supercooling device, and cooling the temperature to below 20 ℃.
2. The device of claim 1, wherein pressure measuring elements are provided before and after the ceramic membrane module.
3. The apparatus of claim 1 or 2, wherein the cryogenic process spray unit comprises a cooling device and an atomizer head disposed in the flue gas before the flue gas flows through the ceramic membrane unit.
CN201910773579.8A 2019-08-21 2019-08-21 Ceramic membrane-based flue gas water capturing device and ceramic membrane cleaning process Active CN110465163B (en)

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Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101934199A (en) * 2010-06-13 2011-01-05 北京科泰兴达高新技术有限公司 Offline reverse osmosis membrane cleaning equipment
CN107166367A (en) * 2017-06-21 2017-09-15 华北电力大学 A kind of fume afterheat and moisture recovery system based on ceramic membrane heat exchanger

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101934199A (en) * 2010-06-13 2011-01-05 北京科泰兴达高新技术有限公司 Offline reverse osmosis membrane cleaning equipment
CN107166367A (en) * 2017-06-21 2017-09-15 华北电力大学 A kind of fume afterheat and moisture recovery system based on ceramic membrane heat exchanger

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