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CN109126431A - The device and method of liquid phase adsorption formula oxidation-reduction method denitrating flue gas - Google Patents

The device and method of liquid phase adsorption formula oxidation-reduction method denitrating flue gas Download PDF

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Publication number
CN109126431A
CN109126431A CN201810877664.4A CN201810877664A CN109126431A CN 109126431 A CN109126431 A CN 109126431A CN 201810877664 A CN201810877664 A CN 201810877664A CN 109126431 A CN109126431 A CN 109126431A
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denitration
flue gas
liquid
mixed liquor
tower
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温正城
陈江星
李源
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Hangzhou Dianzi University
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Hangzhou Dianzi University
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77Liquid phase processes
    • B01D53/79Injecting reactants
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/02Separation 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 adsorption, e.g. preparative gas chromatography
    • B01D53/06Separation 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 adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/10Separation 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 adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents
    • B01D53/12Separation 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 adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents according to the "fluidised technique"
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation 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
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/54Nitrogen compounds
    • B01D53/56Nitrogen oxides
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2251/00Reactants
    • B01D2251/10Oxidants
    • B01D2251/106Peroxides
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2251/00Reactants
    • B01D2251/20Reductants
    • B01D2251/206Ammonium compounds
    • B01D2251/2067Urea
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2253/00Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10Inorganic adsorbents
    • B01D2253/102Carbon
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2258/00Sources of waste gases
    • B01D2258/02Other waste gases
    • B01D2258/0283Flue gases

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Dispersion Chemistry (AREA)
  • Treating Waste Gases (AREA)

Abstract

The present invention discloses the device and method of liquid phase adsorption formula oxidation-reduction method denitrating flue gas.The present invention will be come into full contact in a manner of being bubbled or spraying etc. with denitration mixed liquor, the NO in flue gas through the boiler smoke after wet process of FGD (WFGD)xIt is first adsorbed by the adsorbent in denitration mixed liquor, redox reaction then occurs with reducing agent and oxidant etc., generate N2、CO2And H2O achievees the purpose that denitration.The range of reaction temperature that liquid phase oxidation restores denitration is 20-80 DEG C, is reheated without additional, and hydrogen peroxide/NO moles of accounting is only 30-50%, hydrogen peroxide usage amount is greatly reduced, and operating cost is greatly reduced.The method of the present invention can reach 90% or more denitration efficiency, and cost is more cheap, and equipment is simple, easily operated, be not necessarily to reheating, be not necessarily to catalyst, without secondary pollution.

Description

The device and method of liquid phase adsorption formula oxidation-reduction method denitrating flue gas
Technical field
The present invention relates to fire coal boiler fume processing technology field more particularly to a kind of liquid phase adsorption formula oxidation-reduction method cigarettes The device and method of qi exhaustion nitre.
Background technique
Steadily improved with the rapid development of our country's economy with living standards of the people, the consumption of China's energy and electric power and Demand increases year by year.Due to the energy resources feature of China's few gas rich in coal and poor in oil, the supply of China's electric power is sent out with coal-fired firepower Based on electricity, and in coal-fired process, flue dust, sulfur dioxide (SO are inevitably resulted from2), nitrogen oxides (NOx), oxidation of coal Object (CO/CO2), the pollutants such as toxic heavy metals and volatile organic matter (VOCs) such as mercury (Hg).Coal contaminants are to China Atmospheric environment and ecological environment cause extremely serious pollution and destruction, direct or indirect wound is also brought to human health Evil and influence.Nitrogen oxides is the most important atmosphere pollution after flue dust and sulfur dioxide, is N2O, NO, NO2, NO3, N2O5 Etc. a series of general name of nitrogen oxides.NOxThere is biggish harm to human body and animals and plants, be capable of forming acid rain and acid mist, breaks Bad ecological environment, moreover it is possible to form photochemical fog in conjunction with volatile organic matter, destroy ozone layer, and cause global warming.Closely Over 30 years, the total emission volumn of China's nitrogen oxides sharp increases year by year with the growth of fired power generating unit installed capacity, Far beyond the ability to bear of environment.With getting worse for environmental pollution and being increasingly enhanced for people's environmental consciousness, coal-fired electricity The NO of factoryxEmission request is also increasingly strict.According to Chinese Ministry of Environmental Protection's fossil-fuel power plant atmospheric pollutant emission standard (GB 13223-2011), Either existing coal-burning boiler or newly constructed boiler, NOxEmission limit is 100mg/m3, only small part boiler is implementable 200mg/m3Emission limit.NOxEmission control be very distinct issues in China's socio-economic development, and learn The hot issue of art field common concern.
The control of Ran Ran power plant NOx emission is there are mainly two types of approach, i.e., in combustion process and flue gas post-processing technology.It is burned Processing technique, which refers to through the condition of the design, change burning that improve burner, in journey reduces NOxDischarge amount.Common burning In the process processing technique include low latitude gas excess combustion, Researched of Air Staging Combustion Burning Pulverized Coal, fuel-staged combustion, flue gas recirculation, it is deep or light partially Difference burning etc..Processing technique is generally only capable of reducing the NO of 30-50% or so in these combustion processesxDischarge, it is difficult to meet existing The increasingly strict discharge standard of row.Therefore, in thermal power plant's Practical Project, it is necessary to flue gas post-processing technology be installed, to reach row Put standard.Flue gas post-processing technology mainly selective non-catalytic reduction (SNCR) and selective catalytic reduction (SCR).SNCR skill Art is a kind of without catalyst, within the temperature range of 850~1100 DEG C, by amino-containing reducing agent (such as ammonium hydroxide, urea liquid Deng) spray into furnace, by the NO in flue gasxReduction removing, generates the denitration technology of nitrogen and water.The major defect of SNCR technology exists It is revealed in ammonia, and its denitration efficiency is only 50-70%, it tends to be difficult to meet increasingly strict emission request.
Selective catalytic reduction (SCR) is the denitration technology that the developed countries such as American-European Japan are widely used.SCR technology denitration It is high-efficient, it is stable, the problem is that, inactivation, the reducing substances (such as ammonium hydroxide etc.) of catalyst are secondary caused by revealing The problems such as pollution, higher dust particles easily cause the abrasion of catalyst, blocking in flue gas under high ash deployment scenarios, operation and Investment cost is very expensive.Wet process of FGD WFGD device is the mature desulfurization technology being widely used at present.Through WFGD desulfurization Afterwards, flue-gas temperature is generally 50-70 DEG C, and the operating temperature of selective catalysis SCR is generally 250-350 DEG C.If being filled in WFGD It postpones and arranges that SCR carries out denitration again, then need to reheat flue gas, operating cost is significantly increased in force.Based on this, urgently It needs to develop a kind of liquid phase gas denitrifying technology of low-cost high-efficiency, to be combined with wet process of FGD WFGD device, reaches To the purpose of removing flue gas pollutant.
Summary of the invention
The purpose of the present invention is be difficult to realize low cost and efficient spy simultaneously for current various gas denitrifying technologies Point provides a kind of liquid phase adsorption formula oxidation-reduction method equipment for denitrifying flue gas, and removal efficiency of the present invention is higher, up to 90% or more, and Cost is more cheap, and equipment is simple, easily operated, is not necessarily to reheating, is not necessarily to catalyst, without secondary pollution.It present invention can be suitably applied to Denitration of boiler smoke processing after wet process of FGD (WFGD), Bubbling method and spray subtraction unit can application implementations.
First method: apparatus of the present invention mainly include being bubbled denitrating tower, denitration mixed liquor, demister, denitration liquid buffering Tank;
The bubbling denitrating tower is provided with denitration mixed liquor, and the bottom for being bubbled denitrating tower is equipped with gas inlet, and the mouth is logical Pressurization air-introduced machine cigarette receiving road is crossed, is entered in tower for flue gas;Upper end is equipped with demister in tower;Above in tower and it is located at demister Upper end is equipped with exhanst gas outlet, which connects back-end ductwork, is discharged outside tower for flue gas after handling;It is bubbled denitrating tower side and is provided with denitration Mixed liquor feed inlet, this mouthful are connect by denitration liquid delivery pipe with the discharge port of denitration liquid surge tank;Denitration liquid surge tank is equipped with Material inlet, for making an addition to the materials such as adsorbent, reducing agent, oxidant.
Above-mentioned liquid phase adsorption formula oxidation-reduction method denitration method for flue gas, mainly comprises the steps that
Step (1), boiler smoke are after wet desulphurization (WFGD) is cooled to 50-70 DEG C, by being pressurized air-introduced machine, after pressurization It sprays into from denitration tower bottom gas inlet is bubbled to tower.
The boiler smoke is containing NOx、SO2, the pollutants such as dust flue gas;
Step (2), flue gas are come into full contact in a manner of being bubbled with denitration mixed liquor, the NO in flue gasxFirst mixed by denitration Adsorbent absorption in liquid, then occurs redox reaction with reducing agent and oxidant etc., generates N2、CO2And H2O reaches de- The purpose of nitre, and it is without secondary pollution.
It is bubbled denitration mixed liquor in denitrating tower to be fed by the conveying of denitration liquid surge tank, denitration mixed liquor passes through material inlet in tank The materials such as adsorbent, reducing agent, oxidant are fed, and are thoroughly mixed.
Step (3) removes NO through denitration mixed liquorxAfterwards, it is bubbled the flue gas emerged and enters tail portion cigarette after demister demisting Road discharge.
Second method: apparatus of the present invention mainly include spray denitrating tower, spray equipment, denitration mixed liquor, demister, take off Nitre liquid surge tank.
The bottom for spraying denitrating tower is equipped with gas inlet and denitration mixed liquor discharge port;Gas inlet cigarette receiving road is used for cigarette Gas enters in tower;Denitration mixed liquor discharge port is fed by the conveying of denitration liquid delivery pipe and the denitration mixed liquor of denitration liquid surge tank Mouth connection.It sprays and is equipped with spray equipment in denitrating tower, which is mixed by circulating pump with the denitration of denitration liquid surge tank The connection of liquid discharge port;It sprays top in denitrating tower and arranges demister above spray equipment;Spray denitrating tower in top and Exhanst gas outlet is equipped with above demister, which connects back-end ductwork, is discharged outside tower for flue gas after handling;Denitration liquid surge tank Equipped with material inlet, for making an addition to the materials such as adsorbent, reducing agent and oxidant.
Further, denitration liquid delivery pipe can control denitration liquid conveying capacity, so that gas inlet is located at processing in tower The top of denitration mixed liquor liquid level afterwards.
Above-mentioned liquid phase adsorption formula oxidation-reduction method denitration method for flue gas, mainly comprises the steps that
Step (1), boiler smoke are after wet desulphurization (WFGD) is cooled to 50-70 DEG C, into spray denitrating tower.
The boiler smoke is containing NOx、SO2, the pollutants such as dust flue gas;
The denitration spray liquid that step (2), flue gas are sprayed with spray equipment in spray denitrating tower comes into full contact with, in flue gas NOxIt is first adsorbed by the adsorbent in denitration spray liquid, redox reaction then occurs with reducing agent and oxidant etc., generate N2、 CO2And H2O achievees the purpose that denitration, and without secondary pollution.
Denitration mixed liquor is delivered to denitration liquid surge tank by denitration liquid delivery pipe after step (3), spray, and denitration mixes in tank Liquid suitably feeds the materials such as adsorbent, reducing agent and oxidant by material inlet, and is thoroughly mixed, then defeated by circulating pump It send to spray equipment and carries out circulated sprinkling denitration.
Step (4), flue gas remove NO through spray denitration liquidxAfterwards, then after demister demisting enter back-end ductwork to discharge.
The denitration liquid of denitration liquid surge tank output is the mixed liquor of adsorbent, reducing agent and oxidant, wherein reducing agent matter Amount concentration is 1-20%, and oxidant mass concentration is 0.1-5%, and adsorbent mass concentration is 0.1-10%, remaining is water;
Preferably, reducing agent mass concentration is 5-15%;
Preferably, oxidant mass concentration is 0.2-2%;
Preferably, adsorbent mass concentration is 0.2-2%;
The adsorbent is the carbon-supported catalyst containing a large amount of holes, high-specific surface area such as active carbon, and particle size range is 1-1000 μm, preferably 30-500 μm
The reducing agent is urea, ammonium hydroxide etc. containing-trivalent nitrogen compound;
The oxidant is hydrogen peroxide;
The bubbling denitrating tower and spray denitrating tower interior reaction temperature range is 20-80 DEG C, is advisable with 50-70 DEG C.
The beneficial effects of the present invention are:
(1) the denitration mixed liquor that the present invention uses is mixed in a certain ratio by adsorbent, reducing agent and oxidant forms; In implementation process, the NOx in flue gas is attracted to adsorbent surface, and redox then occurs with reducing agent and oxidant etc. It reacts and is removed, adsorbent plays the role of intermediary during denitration reaction, without lasting addition, substantially saves operation Cost.
(2) general oxidizing process denitration (ozone/NO or hydrogen peroxide/NO moles of accounting are up to 100-120%) is compared, the present invention Depth denitration (the comprehensive denitration efficiency 90% sprayed based on reducing agent (such as urea) and oxidant (such as hydrogen peroxide) mixed liquor More than), oxidant (such as hydrogen peroxide)/NO moles of accounting of redox denitration is only 30-50%, can reduce 60-80%'s Oxidant (such as hydrogen peroxide) usage amount, substantially saves operating cost.
(3) it is 20-80 DEG C that the present invention, which is bubbled denitrating tower and spray denitrating tower interior reaction temperature range, is advisable with 50-70 DEG C, Without additionally reheating, operating cost is greatly reduced.
Liquid phase adsorption formula oxidation-reduction method denitrating flue gas new method provided by the invention, using Bubbling method and spray subtraction unit Application implementation can reach 90% or more denitration efficiency, and cost is more cheap, and equipment is simple, easily operated, no longer need to Heat is not necessarily to catalyst, without secondary pollution.
Detailed description of the invention
Fig. 1 is liquid phase adsorption formula oxidation-reduction method denitrating flue gas Bubbling method apparatus structure schematic diagram;In figure: flue 1, pressurization Air-introduced machine 2, bubbling denitrating tower 3, denitration mixed liquor 4, demister 5, denitration liquid surge tank 6, denitration liquid delivery pipe 7, material inlet 8, Back-end ductwork 9.
Fig. 2 is liquid phase adsorption formula oxidation-reduction method denitrating flue gas spray process apparatus structure schematic diagram;In figure: flue 1, spray Denitrating tower 2, spray equipment 3, denitration mixed liquor 4, demister 5, denitration liquid delivery pipe 6, denitration liquid surge tank 7, material inlet 8 follow Ring pump 9, back-end ductwork 10.
Specific embodiment
The present invention is described in further detail in the following with reference to the drawings and specific embodiments.
The denitration liquid of denitration liquid surge tank output below is the mixed liquor of adsorbent, reducing agent and oxidant, wherein restoring Agent mass concentration is 1-20%, and oxidant mass concentration is 0.1-5%, and adsorbent mass concentration is 0.1-10%, remaining is water;
Preferably, reducing agent mass concentration is 5-15%;
Preferably, oxidant mass concentration is 0.2-2%;
Preferably, adsorbent mass concentration is 0.2-2%;
The adsorbent is the carbon-supported catalyst containing a large amount of holes, high-specific surface area such as active carbon, and particle size range is 1-1000 μm, preferably 30-500 μm
The reducing agent is urea, ammonium hydroxide etc. containing-trivalent nitrogen compound;
The oxidant is hydrogen peroxide;
The bubbling denitrating tower and spray denitrating tower interior reaction temperature range is 20-80 DEG C, is advisable with 50-70 DEG C.
Embodiment 1:
If Fig. 1 shows, a kind of liquid phase adsorption formula oxidation-reduction method denitrating flue gas, which is bubbled subtraction unit and has, is sequentially connected the cigarette connect Road 1, is bubbled denitrating tower 3 and back-end ductwork 9 at pressurization air-introduced machine 2.It is bubbled denitrating tower 3 and is provided with denitration mixed liquor 4, tower inner top Arrange demister 5.Flue gas 1 blasts after being pressurized air-introduced machine 2 is bubbled denitrating tower 3, and NOx is removed by denitration mixed liquor 4 in flue gas, is taken off Flue gas discharges again through 5 demisting of demister finally by back-end ductwork 9 after nitre.Denitration mixed liquor 4 is connected by denitration liquid delivery pipe 7 Denitration liquid surge tank 6 is connect, denitration liquid delivery pipe 7 can control denitration liquid conveying capacity.6 top layout material inlet of denitration liquid surge tank, It is supplied for materials such as adsorbent, reducing agent and oxidants.
Application implementation of the present invention is bubbled subtraction unit (Fig. 1) progress denitration and mainly comprises the steps that
1) boiler smoke 1 is after wet desulphurization (WFGD) is cooled to 50-70 DEG C, by being pressurized air-introduced machine 2, from drum after pressurization It steeps 3 bottom of denitrating tower and sprays into denitration mixed liquor 4.
2) flue gas is come into full contact in a manner of being bubbled with denitration mixed liquor, the NO in flue gasxFirst by denitration mixed liquor Adsorbent absorption, then occurs redox reaction with reducing agent and oxidant etc., generates N2、CO2And H2O reaches the mesh of denitration , and it is without secondary pollution.
3) denitration mixed liquor is fed by denitration liquid surge tank 6 by denitration liquid delivery pipe 7, and denitration mixed liquor is by giving in tank Material mouth 8 feeds the materials such as adsorbent, reducing agent and oxidant, and is thoroughly mixed.
4) NO is removed through denitration mixed liquorxAfterwards, it is bubbled the flue gas emerged and enters 9 row of back-end ductwork after demister demisting It puts.
If Fig. 2 shows, a kind of liquid phase adsorption formula oxidation-reduction method denitrating flue gas spray subtraction unit, which has, is sequentially connected the cigarette connect Road 1, spray denitrating tower 2 and back-end ductwork 9.It sprays and arranges spray equipment 3 in denitrating tower 2, bottom is denitration mixed liquor 4, top Arrange demister 5.Flue gas enters spray denitrating tower through flue 1, comes into full contact with spray denitration liquid, NOx is sprayed by denitration in flue gas 4 adsorbing and removing of liquid is drenched, flue gas discharges again through 5 demisting of demister finally by back-end ductwork 10 after denitration.Denitration mixes after spray Liquid 4 is delivered to denitration liquid surge tank 7 by denitration liquid delivery pipe 6, and denitration liquid delivery pipe 6 can control denitration liquid conveying capacity.Denitration 7 top layout material inlet of liquid surge tank, for the supply of the materials such as adsorbent, reducing agent and oxidant.Denitration mixes in surge tank 7 Liquid is transported to spray equipment 3 by circulating pump 9, to realize circulated sprinkling denitration.
Present invention application spray subtraction unit (Fig. 2) carries out denitration and mainly comprises the steps that
1) boiler smoke 1 is after wet desulphurization (WFGD) is cooled to 50-70 DEG C, and into spray denitrating tower 2, in-position exists Higher than the spray denitrating tower lower part of 4 liquid level of denitration mixed liquor.
2) the denitration spray liquid that flue gas is sprayed with spray equipment comes into full contact with, the NO in flue gasxFirst by denitration mixed liquor Adsorbent absorption, redox reaction then occurs with reducing agent and oxidant etc., generates N2、CO2And H2O reaches denitration Purpose, and it is without secondary pollution.
3) denitration mixed liquor 4 is delivered to denitration liquid surge tank 7 by denitration liquid delivery pipe 6 after spraying, denitration mixed liquor in tank It by materials such as material inlets 8 suitably supply adsorbent, reducing agent and oxidant, and is thoroughly mixed, then defeated by circulating pump It send to spray equipment and carries out circulated sprinkling denitration.
4) NO is removed through spray denitration liquidxAfterwards, flue gas enters back-end ductwork 10 again after 5 demisting of demister and discharges.
It is bis- with 0.3-0.5% using 0.5-1% active carbon as adsorbent using 10% urea as reducing agent according to experimental result Oxygen water is oxidant, Bubbling method and 90% or more spray process denitration efficiency.
The above enumerated are only specific embodiments of the present invention for finally, it should also be noted that.Obviously, the present invention is unlimited In above embodiments, acceptable there are many deformations.
The present invention can be summarized with others without prejudice to the concrete form of spirit or central characteristics of the invention.Therefore, nothing By from the point of view of which point, the embodiment above of the invention can only all be considered the description of the invention and cannot limit this hair Bright, claims indicate the scope of the present invention, and above-mentioned explanation does not point out the scope of the present invention, therefore, with this Any change in the comparable meaning and scope of claims of invention is all considered as including the range in claims It is interior.

Claims (9)

1. the device of liquid phase adsorption formula oxidation-reduction method denitrating flue gas, it is characterised in that main mixed including bubbling denitrating tower, denitration Close liquid, demister, denitration liquid surge tank;
The bubbling denitrating tower is provided with denitration mixed liquor, and the bottom for being bubbled denitrating tower is equipped with gas inlet, which passes through increasing Air-introduced machine cigarette receiving road is pressed, is entered in tower for flue gas;Upper end is equipped with demister in tower;Top and the upper end positioned at demister in tower Equipped with exhanst gas outlet, which connects back-end ductwork, is discharged outside tower for flue gas after handling;Be bubbled denitrating tower be equipped with denitration mixed liquor into Material mouth, this mouthful are connect by denitration liquid delivery pipe with the discharge port of denitration liquid surge tank;Denitration liquid surge tank is equipped with material inlet, uses In making an addition to the materials such as adsorbent, reducing agent and oxidant;
The denitration liquid of denitration liquid surge tank output is the mixed liquor of adsorbent, reducing agent and oxidant, and wherein reducing agent quality is dense Degree is 1-20%, and oxidant mass concentration is 0.1-5%, and adsorbent mass concentration is 0.1-10%, remaining is water;
Being bubbled denitrating tower interior reaction temperature range is 20-80 DEG C.
2. based on device described in claim 1 carry out liquid phase adsorption formula oxidation-reduction method denitration method for flue gas, mainly include with Lower step:
Step (1), boiler smoke are after wet desulphurization (WFGD) is cooled to 50-70 DEG C, by being pressurized air-introduced machine, from drum after pressurization Bubble denitration tower bottom gas inlet is sprayed into tower;
The boiler smoke is containing NOx、SO2, the pollutants such as dust flue gas;
Step (2), flue gas are come into full contact in a manner of being bubbled with denitration mixed liquor, the NO in flue gasxFirst by denitration mixed liquor Adsorbent absorption, then occurs redox reaction with reducing agent and oxidant etc., generates N2、CO2And H2O reaches the mesh of denitration , and it is without secondary pollution;
It is bubbled denitration mixed liquor in denitrating tower to be fed by the conveying of denitration liquid surge tank, denitration mixed liquor passes through material inlet and feeds in tank The materials such as adsorbent, reducing agent and oxidant, and be thoroughly mixed;
Step (3) removes NO through denitration mixed liquorxAfterwards, it is bubbled the flue gas emerged and enters back-end ductwork row after demister demisting It puts.
3. the device of liquid phase adsorption formula oxidation-reduction method denitrating flue gas, it is characterised in that main includes spray denitrating tower, spray dress It sets, denitration mixed liquor, demister, denitration liquid surge tank;
The bottom for spraying denitrating tower is equipped with gas inlet and denitration mixed liquor discharge port;Gas inlet cigarette receiving road, for flue gas into Enter in tower;Denitration mixed liquor discharge port is connected by the conveying of denitration liquid delivery pipe and the denitration mixed liquor feed inlet of denitration liquid surge tank It connects;It sprays and is equipped with spray equipment in denitrating tower, which is gone out by the denitration mixed liquor of circulating pump and denitration liquid surge tank Material mouth connection;It sprays top in denitrating tower and arranges demister above spray equipment;Above in spray denitrating tower and it is located at Exhanst gas outlet is equipped with above demister, which connects back-end ductwork, is discharged outside tower for flue gas after handling;Denitration liquid surge tank is equipped with Material inlet, for making an addition to the materials such as adsorbent, reducing agent and oxidant;
The denitration liquid of denitration liquid surge tank output is the mixed liquor of adsorbent, reducing agent and oxidant, and wherein reducing agent quality is dense Degree is 1-20%, and oxidant mass concentration is 0.1-5%, and adsorbent mass concentration is 0.1-10%, remaining is water;
Spraying denitrating tower interior reaction temperature range is 20-80 DEG C.
4. based on device as claimed in claim 3 carry out liquid phase adsorption formula oxidation-reduction method denitration method for flue gas, mainly include with Lower step:
Step (1), boiler smoke are after wet desulphurization (WFGD) is cooled to 50-70 DEG C, into spray denitrating tower;
The boiler smoke is containing NOx、SO2, the pollutants such as dust flue gas;
The denitration spray liquid that step (2), flue gas are sprayed with spray equipment in spray denitrating tower comes into full contact with, the NO in flue gasxFirst quilt Adsorbent absorption in denitration spray liquid, then occurs redox reaction with reducing agent and oxidant etc., generates N2、CO2And H2O achievees the purpose that denitration, and without secondary pollution;
Denitration mixed liquor is delivered to denitration liquid surge tank by denitration liquid delivery pipe after step (3), spray, and denitration mixed liquor is logical in tank It crosses material inlet and suitably feeds the materials such as adsorbent, reducing agent and oxidant, and be thoroughly mixed, then be delivered to by circulating pump Spray equipment carries out circulated sprinkling denitration;
Step (4), flue gas remove NO through spray denitration liquidxAfterwards, then after demister demisting enter back-end ductwork to discharge.
5. the device of liquid phase adsorption formula oxidation-reduction method denitrating flue gas as claimed in claim 1 or 3, it is characterised in that denitration liquid Reducing agent mass concentration is 5-15% in the denitration liquid of surge tank output;Oxidant mass concentration is 0.2-2%;Adsorbent mass Concentration is 0.2-2%.
6. the device of liquid phase adsorption formula oxidation-reduction method denitrating flue gas as claimed in claim 1 or 3, it is characterised in that denitration liquid Reducing agent described in the denitration liquid of surge tank output is urea, ammonium hydroxide etc. containing-trivalent nitrogen compound.
7. the device of liquid phase adsorption formula oxidation-reduction method denitrating flue gas as claimed in claim 1 or 3, it is characterised in that denitration liquid Oxidant described in the denitration liquid of surge tank output is hydrogen peroxide.
8. the device of liquid phase adsorption formula oxidation-reduction method denitrating flue gas as claimed in claim 1 or 3, it is characterised in that denitration liquid Adsorbent described in the denitration liquid of surge tank output is the charcoal base absorption containing a large amount of holes, high-specific surface area such as active carbon Agent, particle size range are 1-1000 μm.
9. the device of liquid phase adsorption formula oxidation-reduction method denitrating flue gas as claimed in claim 1 or 3, it is characterised in that described Being bubbled denitrating tower and spray denitrating tower interior reaction temperature range is 50-70 DEG C.
CN201810877664.4A 2018-08-03 2018-08-03 The device and method of liquid phase adsorption formula oxidation-reduction method denitrating flue gas Pending CN109126431A (en)

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CN113048467A (en) * 2020-12-10 2021-06-29 哈尔滨博深科技发展有限公司 Coal-fired boiler with reduced nitrogen oxide injection apparatus
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CN111905548A (en) * 2019-05-07 2020-11-10 山东师范大学 Method for low-temperature denitration of flue gas by using aqueous hydrogen peroxide solution
CN113048467A (en) * 2020-12-10 2021-06-29 哈尔滨博深科技发展有限公司 Coal-fired boiler with reduced nitrogen oxide injection apparatus
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