CN208990559U - Realize NO in ultralow temperature flue gasxThe process system of efficient removal and its resource utilization - Google Patents
Realize NO in ultralow temperature flue gasxThe process system of efficient removal and its resource utilization Download PDFInfo
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- CN208990559U CN208990559U CN201821554358.9U CN201821554358U CN208990559U CN 208990559 U CN208990559 U CN 208990559U CN 201821554358 U CN201821554358 U CN 201821554358U CN 208990559 U CN208990559 U CN 208990559U
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
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- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/73—After-treatment of removed components
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- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/20—Nitrogen oxides; Oxyacids of nitrogen; Salts thereof
- C01B21/38—Nitric acid
- C01B21/40—Preparation by absorption of oxides of nitrogen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/10—Oxidants
- B01D2251/102—Oxygen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
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- B01D2258/0283—Flue gases
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
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- Y02P20/00—Technologies relating to chemical industry
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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Abstract
The utility model, which discloses, realizes NO in ultralow temperature flue gasxThe process system of efficient removal and its resource utilization, including the smoke inlet pipe for conveying upstream workshop section flue gas, smoke inlet pipe has the heat exchanger that waste heat recycling is carried out for the flue gas to upstream workshop section by piping connection, the outlet of heat exchanger has by piping connection for carrying out denitration to flue gas and the denitration material for being used for denitration being carried out regenerated adsorption-regeneration system, adsorption-regeneration system is connect by air-introduced machine with chimney, and air-introduced machine is used to the flue gas after denitration in adsorption-regeneration system being discharged into chimney；Adsorption-regeneration system is also connected with the NO for storing the higher concentration obtained after regeneration in adsorption-regeneration systemxAir accumulator, the outlet of air accumulator is connected with nitric acid preparation system.By the utility model NO can be realized under conditions of being lower than 100 DEG CxEfficient removal, and be able to achieve its resource utilization, compared with prior art, there is apparent advanced and economy.
Description
Technical field
The utility model relates to atmosphere pollution Treatment process fields, and in particular to realize NO in ultralow temperature flue gasxEfficiently
The process system of removing and its resource utilization.
Background technique
Nitrogen oxides (NOx) it is a kind of typical atmosphere pollution, it is mainly derived from fossil energy conversion and nature
Organic matter decomposes two processes in boundary.NOxThe environmental pollutions such as acid rain and photochemical fog are not only resulted in, while to the mankind and being moved
The ecological environment that plant depends on for existence causes persistent threat.For example, the mist that China's most area persistently occurs in recent years
Haze phenomenon and NOxDischarge beyond standards it is closely related.NOxIt is extensive discharge seriously violate sustainable development objective, to China's economy
Social development proposes stern challenge.State Council in 2013 has printed and distributed " prevention and control of air pollution action plan ", is NOxIt is anti-
It controls work and specifies direction.
Gas denitrifying technology is one of important R&D direction of atmosphere pollution Treatment process.After decades of development,
High temperature gas denitrifying technology has been realized in industrial applications, wherein most representative technology is SNCR and SCR denitration skill
Art.In recent years, with the continuous reinforcement of environmental protection standard, low-temperature flue gas improvement is gradually received significant attention.Due to SNCR denitration skill
Efficiency is lower in actual application for art, and the escaping of ammonia is serious, it is difficult to reach increasingly strict discharge standard.Traditional SCR is de-
Nitre technology is suitable for high temperature fume treatment, for low-temperature flue gas and is not suitable for.The active temperature one of low-temperature SCR catalyst
As can be down to 200 DEG C or less.The low-temperature SCR catalyst of Dutch Shell company and the exploitation of Ceram company, Austria is real
Industrial applications are showed.The country also obtains a series of progress in low-temperature SCR catalyst technology of preparing.Although low temperature SCR denitration
Technology has been realized in industrial applications, but there are still some problems, how to improve the low-temperature reactivity of catalyst and resist
Sulphur still needs to further break through.Oxidative absorption denitration technology is that one kind can be with efficient process NOxTechnology.Due to NOxMain component
For the NO for being insoluble in water, how NO is efficiently oxidized to the pass that high-valence state nitrogen oxides soluble easily in water is oxidative absorption technology
Key.German Linde company develops with O3Aoxidize the LoTO that NO is technological corexTechnology, and in Effect of Catalysis In Petrochemistry cracking unit etc.
Application is achieved in fume treatment.The defect of oxidative absorption denitration technology is to need to consume a large amount of expensive oxidants, with oxygen
For changing 1 ton of NO, theoretically need to consume 1.6 tons of O3, due to O under the prior art3Production cost is very high, and then causes to take off
Nitre cost is excessively high, and technology is difficult to large-scale promotion.
So far, it there is no economically feasible both at home and abroad, and be generally applicable to the denitration technology of every profession and trade fume treatment.If
NO in flue gas can be even realized at room temperature in ultra low temperature (< 100 DEG C)xEfficient removal, then denitrification apparatus can be arranged in cigarette
After the recycling of gas waste heat, dedusting, desulfurizer, denitration is carried out under the operating condition of relative clean, to solve existing denitration technology
Without general applicability, and the technical problem that operating condition is severe.In conclusion for existing in existing flue gas treating process
Deficiency, develop novel ultralow temperature gas denitrifying technology with urgent need.
Utility model content
To solve problems of the prior art, the purpose of this utility model is that open realize in ultralow temperature flue gas
NOxThe process system of efficient removal and its resource utilization can make the NO in flue gas by the utility modelxIn flue gas
O2And H2The intrinsic component such as O is in ultralow temperature Benitration reactor under the catalytic action of denitration material, in-situ preparation acidic materials, and
It is adsorbed in the hole of denitration material.NO by a series of chemical reaction and adsorption process, in flue gasxIt is removed, only
Flue gas after change passes through smoke stack emission.Regeneration circulation utilization, the height generated in the process are carried out to the denitration material after absorption
Concentration NOxNitric acid product is generated by certain chemical reaction and concentration.The utility model provides one kind can be low
NO in flue gas is realized under conditions of 100 DEG CxEfficient removal, and be able to achieve the technical solution of its resource utilization, and it is existing
Technology is compared, and the utility model technology has apparent advanced and economy.
The purpose of this utility model is achieved through the following technical solutions:
Realize NO in ultralow temperature flue gasxThe process system of efficient removal and its resource utilization, including for conveying upstream
The smoke inlet pipe of workshop section's flue gas, smoke inlet pipe has by piping connection carries out waste heat recycling for the flue gas to upstream workshop section
Heat exchanger, the outlet of heat exchanger by piping connection have for flue gas progress denitration and will be used for the denitration material of denitration into
The regenerated adsorption-regeneration system of row, adsorption-regeneration system are connect by air-introduced machine with chimney, and air-introduced machine is used for adsorption-regeneration
Flue gas in system after denitration is discharged into chimney；Adsorption-regeneration system is also connected with for storing in adsorption-regeneration system after regeneration
The NO of obtained higher concentrationxAir accumulator, the outlet of air accumulator is connected with nitric acid preparation system.
Adsorption-regeneration system includes ADSORPTION IN A FIXED BED tower A and ADSORPTION IN A FIXED BED tower B, and the outlet of heat exchanger is divided into two-way simultaneously
The entrance with ADSORPTION IN A FIXED BED tower A and ADSORPTION IN A FIXED BED tower B passes through piping connection respectively；ADSORPTION IN A FIXED BED tower A and fixed bed are inhaled
The outlet of attached tower B passes through pipeline and connect with air-introduced machine；The outlet of ADSORPTION IN A FIXED BED tower A and ADSORPTION IN A FIXED BED tower B also lead to respectively
Pipeline is crossed to connect with air accumulator；Smoke inlet pipe is connect by pipeline with air-introduced machine；
On the pipeline that smoke inlet pipe is connect with heat exchanger, heat exchanger and ADSORPTION IN A FIXED BED tower A and ADSORPTION IN A FIXED BED tower B connect
On the pipeline connect, on the pipeline that the outlet of ADSORPTION IN A FIXED BED tower A and ADSORPTION IN A FIXED BED tower B are connect with air-introduced machine, ADSORPTION IN A FIXED BED
The outlet of tower A and ADSORPTION IN A FIXED BED tower B on the tank connected pipeline of gas storage and pipeline that smoke inlet pipe is connect with air-introduced machine
On be equipped with control valve.
The outlet of ADSORPTION IN A FIXED BED tower A and ADSORPTION IN A FIXED BED tower B are in parallel, and entirety is connect with air-introduced machine after parallel connection, simultaneously
Pipeline after connection is equipped with control valve；
The outlet of ADSORPTION IN A FIXED BED tower A and the outlet of ADSORPTION IN A FIXED BED tower B are respectively arranged to control ADSORPTION IN A FIXED BED tower A
The control valve of air-introduced machine is passed through with the gas in ADSORPTION IN A FIXED BED tower B.
The outlet of ADSORPTION IN A FIXED BED tower A and ADSORPTION IN A FIXED BED tower B are in parallel, and entirety is connect with air accumulator after parallel connection；
The outlet of ADSORPTION IN A FIXED BED tower A and the outlet of ADSORPTION IN A FIXED BED tower B are respectively arranged to control ADSORPTION IN A FIXED BED tower A
The control valve of air accumulator is passed through with the gas in ADSORPTION IN A FIXED BED tower B.
Adsorption-regeneration system includes moving bed adsorption tower and moving bed regenerator, and the outlet of heat exchanger and moving bed adsorb
The gas access of tower passes through piping connection；The gas vent of moving bed adsorption tower is connect by pipeline with air-introduced machine；Moving bed is inhaled
The denitration material outlet of attached tower is connect with the feed bin of moving bed regenerator；The denitration material of moving bed regenerator exports and moving bed
The feed bin of adsorption tower connects, and the gas vent and air accumulator of moving bed regenerator pass through piping connection；Smoke inlet pipe passes through pipe
Road is connect with air-introduced machine；
On the pipeline that smoke inlet pipe is connect with heat exchanger, the outlet of heat exchanger and the gas access of moving bed adsorption tower connect
On the pipeline connect, on the pipeline that the gas vent of moving bed adsorption tower is connect with air-introduced machine, the gas vent of moving bed regenerator
Control valve is equipped with on the tank connected pipeline of gas storage and on pipeline that smoke inlet pipe is connect with air-introduced machine.
The denitration material outlet of moving bed adsorption tower is connect by conveyer belt with the feed bin of moving bed regenerator；Moving bed is again
The denitration material outlet of raw tower is connect by conveyer belt with the feed bin of moving bed adsorption tower.
Nitric acid preparation system includes nitric acid reaction device and nitric acid storage tank, and the entrance of nitric acid reaction device passes through pipeline and air accumulator
Connection, outlet are connect by pipeline with nitric acid storage tank；The connecting line of nitric acid reaction device and air accumulator and company with nitric acid storage tank
Adapter tube road is equipped with control valve.
Compared with prior art, the utility model at least has following benefit:
By the process system of the utility model can (1) denitration activity temperature is down to 100 DEG C hereinafter, having widened denitration
Denitrification apparatus can be set to after dedusting and desulfurizer since reaction temperature is low, avoid the powder in flue gas by temperature window
Dirt and SO2Etc. influence of the harmful substances to denitration material；(2) oxidant for not consuming reducing agent or valuableness, merely in flue gas
O2And H2Denitration in situ can be realized in the intrinsic component such as O, greatlys save operating cost；(3) by the NO in flue gasxIt recycles and turns
The nitric acid product with economic value is turned to, the resource utilization of waste is realized.
It can make the NO in flue gas by the utility modelxWith the O in flue gas2And H2The intrinsic component such as O is in ultralow temperature denitration
In reactor under the catalytic action of denitration material, in-situ preparation acidic materials, and be adsorbed in the hole of denitration material.Pass through
A series of chemical reaction and adsorption process, the NO in flue gasxIt is removed, purified flue gas passes through smoke stack emission.To absorption
Denitration material afterwards carries out regeneration circulation utilization, the higher concentration NO generated in the processxBy certain chemical reaction and dense
Contracting processing generates nitric acid product.The utility model can realize NO in flue gas under conditions of being lower than 100 DEG CxEfficient removal,
And it is able to achieve the technical solution of its resource utilization, compared with prior art, there is apparent advanced and economy.
Detailed description of the invention
Fig. 1 is NO in the realization ultralow temperature flue gas of the utility modelxThe technology path of efficient removal and its resource utilization；
Fig. 2 is process system schematic diagram when the utility model uses ADSORPTION IN A FIXED BED technique；
Fig. 3 is process system schematic diagram when the utility model uses moving bed absorbing process.
In figure, 1- smoke inlet pipe, 2- heat exchanger, 3- ADSORPTION IN A FIXED BED tower A, 4- air-introduced machine, 5- chimney, 6- fixed bed
Adsorption tower B, 7- air accumulator, 8- nitric acid reaction device, 9- nitric acid storage tank, 10- moving bed adsorption tower, 11- moving bed regenerator, 12-
Control valve, 13- feed bin, 14- discharge valve.
Specific embodiment
The utility model is described further with reference to the accompanying drawings and examples.
As shown in Figures 2 and 3, NO in the realization ultralow temperature flue gas of the utility modelxEfficient removal and its resource utilization
Process system, including the smoke inlet pipe 1 for conveying upstream workshop section flue gas, smoke inlet pipe 1 by piping connection it is useful
The heat exchanger 2 of waste heat recycling is carried out in the flue gas to upstream workshop section, the outlet of heat exchanger 2 has by piping connection for flue gas
It carries out denitration and the denitration material for being used for denitration is subjected to regenerated adsorption-regeneration system, adsorption-regeneration system passes through air-introduced machine
4 connect with chimney 5, and air-introduced machine 4 is used to the flue gas after denitration in absorption-regenerative system being discharged into chimney；Adsorption-regeneration system
It is also connected with the NO for storing the higher concentration obtained after regeneration in adsorption-regeneration systemxAir accumulator 7, air accumulator 7 go out
Mouth is connected with nitric acid preparation system.
The composite material that denitration material is made of organic or inorganic zwitterion active component and carrier, shape are
The random geometries such as spherical, column or plate；Active component forms liquid film in carrier surface, under the catalytic action of liquid film,
NOxWith the O in flue gas2And H2The intrinsic component such as O can in-situ preparation acidic materials.
Such as Fig. 2, when the utility model uses ADSORPTION IN A FIXED BED technique, adsorption-regeneration system includes ADSORPTION IN A FIXED BED tower A
3 and ADSORPTION IN A FIXED BED tower B 6, the outlet of heat exchanger 2 be divided into two-way and respectively with ADSORPTION IN A FIXED BED tower A 3 and ADSORPTION IN A FIXED BED
Tower B 6 passes through piping connection；The outlet of ADSORPTION IN A FIXED BED tower A 3 and ADSORPTION IN A FIXED BED tower B 6 pass through pipeline and air-introduced machine 4
Connection；The outlet of ADSORPTION IN A FIXED BED tower A 3 and ADSORPTION IN A FIXED BED tower B 6 are also connect by pipeline with air accumulator 7 respectively；Flue gas into
Tracheae 1 is connect by pipeline with air-introduced machine 4；
On the pipeline that smoke inlet pipe 1 is connect with heat exchanger 2, heat exchanger 2 and ADSORPTION IN A FIXED BED tower A 3 and ADSORPTION IN A FIXED BED
On the pipeline of the connection of tower B 6, pipeline that the outlet of ADSORPTION IN A FIXED BED tower A 3 and ADSORPTION IN A FIXED BED tower B 6 are connect with air-introduced machine 4
On, on the pipeline that the outlet of ADSORPTION IN A FIXED BED tower A 3 and ADSORPTION IN A FIXED BED tower B 6 are connect with air accumulator 7 and smoke inlet pipe
Control valve is equipped on 1 pipeline connecting with air-introduced machine 4.
Such as Fig. 3, when the utility model uses moving bed absorbing process, adsorption-regeneration system includes moving bed adsorption tower
10 and moving bed regenerator 11, the outlet of heat exchanger 2 and the gas access of moving bed adsorption tower 10 pass through piping connection；Moving bed
The gas vent of adsorption tower 10 is connect by pipeline with air-introduced machine 4；The denitration material outlet of moving bed adsorption tower 10 passes through transmission
Band is connect with the feed bin of moving bed regenerator 11；The denitration material outlet of moving bed regenerator 11 passes through conveyer belt and moving bed
The feed bin of adsorption tower 10 connects, and the gas vent and air accumulator 7 of moving bed regenerator 11 pass through piping connection；Smoke inlet pipe 1
It is connect by pipeline with air-introduced machine 4；
On the pipeline that smoke inlet pipe 1 is connect with heat exchanger 2, the outlet of heat exchanger 2 and the gas of moving bed adsorption tower 10
On the pipeline of entrance connection, on the pipeline that the gas vent of moving bed adsorption tower 10 is connect with air-introduced machine 4, moving bed regenerator 11
The pipeline that is connect with air accumulator 7 of gas vent on and the pipeline that is connect with air-introduced machine 4 of smoke inlet pipe 1 on be equipped with control
Valve.
In conjunction with Fig. 2 and Fig. 3, nitric acid preparation system includes nitric acid reaction device 8 and nitric acid storage tank 9, the entrance of nitric acid reaction device 8
It is connect by pipeline with air accumulator 7, outlet is connect by pipeline with nitric acid storage tank 9；The connection of nitric acid reaction device 8 and air accumulator 7
Pipeline and be equipped with control valve on the connecting line of nitric acid storage tank 9.
The utility model proposes under the catalysis of ultralow temperature denitration material and absorption multiple action, NO is utilizedxWith flue gas
In intrinsic O2And H2The components such as O occur in-situ chemical reaction and realize NOxEfficient removal, regenerated using denitration material
Higher concentration NOxNitric acid product is prepared, while reaching NO in flue gasxEfficient removal and its resource utilization purpose.
As shown in Figure 1, the process system by the utility model realizes NO in ultralow temperature flue gasxEfficient removal and its resource
Change the method utilized, includes the following steps:
Step 1, the flue gas from upstream workshop section makes the temperature of flue gas be down to 25~75 DEG C, institute after residual neat recovering system
The flue gas stated includes power-plant flue gas, coking flue gas, industrial furnace smoke and contains NOxTail gas；
Step 2, the flue gas after cooling is handled, process are as follows: denitration is carried out to flue gas first, makes NO in flue gasx
It is up to standard and by flue gas emission up to standard；The denitration material for being used for denitration is regenerated again, obtains the NO of higher concentrationx, and will
Denitration material after regeneration is recycled and reused for denitrating flue gas；
Step 3, the NO of the higher concentration obtained by step 2xNitric acid product is prepared, realizes the recycling benefit of waste
With when preparing nitric acid product, with air, O2And O3One of or it is a variety of be oxidant, with H2O、 H2O2And HNO3One of
Or a variety of is solvent, reaction temperature is set as 25~75 DEG C, and the reaction time is set as 1~30min, and reaction pressure is set as 0.02
~0.9MPa, the NO for the higher concentration that step 2 is obtainedxConvert and be concentrated the nitric acid for mass percentage not less than 60%
Product.
The step 2 of the utility model can be carried out by the following two kinds mode:
First way, in conjunction with Fig. 2, in the step 2, by the flue gas after cooling by ADSORPTION IN A FIXED BED technique at
When being handled by ADSORPTION IN A FIXED BED technique, at least 2 groups of adsorption towers are arranged in reason, are denoted as ADSORPTION IN A FIXED BED tower A 3 respectively and consolidate
Fixed bed adsorption tower B 6；
Treatment process specifically comprises the following steps:
Step 2.1.1, flue gas initially enter in ADSORPTION IN A FIXED BED tower A 3；
Flue gas is switched to ADSORPTION IN A FIXED BED tower B when ADSORPTION IN A FIXED BED tower A 3 is close to when adsorption saturation by step 2.1.2
6, while ADSORPTION IN A FIXED BED tower A 3 is regenerated；
Flue gas is switched to ADSORPTION IN A FIXED BED when ADSORPTION IN A FIXED BED tower B 6 is close to when adsorption saturation by step 2.1.3 again
Tower A 3, while ADSORPTION IN A FIXED BED tower B 6 is regenerated；
Step 2.1.4 repeats step 2.1.1 to step 2.1.3, so recycles, can be realized NO in flue gasxEfficient place
Reason and qualified discharge.Wherein, in ADSORPTION IN A FIXED BED tower A 3 and ADSORPTION IN A FIXED BED tower B 6, in the catalytic action of denitration material
Under, the NO in flue gasxWith the O in flue gas2And H2In-situ chemical reaction occurs for O, and the product of generation is adsorbed to the hole of denitration material
In gap, reaction temperature is 20~80 DEG C；When being regenerated to ADSORPTION IN A FIXED BED tower A 3 and ADSORPTION IN A FIXED BED tower B 6, added with electricity
Hot or steam-heated mode desorbs the denitration material after absorption, and heating temperature is 105~155 DEG C.
The second way, in conjunction with Fig. 3, in the step 2, by the flue gas after cooling by moving bed absorbing process at
When being handled by moving bed absorbing process, at least 1 group of moving bed adsorption tower 10 and 1 group moving bed regenerator is arranged in reason
11；
Treatment process specifically comprises the following steps:
Flue gas is passed through moving bed adsorption tower 10 by step 2.2.1, and the denitration material in flue gas and moving bed adsorption tower 10 exists
It is inversely contacted in moving bed adsorption tower 10 and realizes NOxEfficient removal, the flue gas being purified；
Purified flue gas is entered smoke stack emission, and will adsorb NO in moving bed adsorption tower 10 by step 2.2.2x's
Denitration material, which is passed through in moving bed regenerator 11, to be regenerated；
Denitration material after regeneration is again returned in moving bed adsorption tower 10 and is used for denitrating flue gas by step 2.2.3；
Step 2.2.4 repeats step 2.2.1 to 2.2.3, so recycles, and realizes NO in flue gasxEfficient process and up to standard
Discharge.
Wherein, the NO in moving bed adsorption tower 10, under the catalytic action of denitration material, in flue gasxWith the O in flue gas2
And H2In-situ chemical reaction occurs for O, and the product of generation is adsorbed in the hole of denitration material, and reaction temperature is 25~75 DEG C；
When being regenerated to moving bed regenerator 11, by electric heating or it is steam-heated in a manner of the denitration material after absorption is solved
It inhales, heating temperature is 105~155 DEG C.
Embodiment 1
Power-plant flue gas is handled, flue gas is after waste heat recycles, and exhaust gas temperature is 55 DEG C, NOxContent is 600mg/
m3.Denitration process is carried out to flue gas using ADSORPTION IN A FIXED BED technique, denitration temperature is set as 55 DEG C, and regeneration temperature is set as 135
℃.After treatment, NO in flue gasxContent is down to 43mg/m3, reach " fossil-fuel power plant atmospheric pollutant emission standard " (GB
The requirement of special emission limit in 13223-2011).Higher concentration NO obtained in denitration material regenerative processxIt is prepared into nitric acid
In system, with O2For oxidant, H2O is solvent, and reaction temperature is set as 25 DEG C, and the reaction time is set as 1min, and reaction pressure is set
It is set to 0.02MPa, the nitric acid product that mass percentage is not less than 60% is obtained after after chemical reaction and concentration.
Embodiment 2
Power-plant flue gas is handled, flue gas is after waste heat recycles, and exhaust gas temperature is 55 DEG C, NOxContent is 600mg/
m3.Denitration process is carried out to flue gas using moving bed absorbing process, denitration temperature is set as 55 DEG C, and regeneration temperature is set as 135
℃.After treatment, NO in flue gasxContent is down to 48mg/m3, reach " fossil-fuel power plant atmospheric pollutant emission standard " (GB
The requirement of special emission limit in 13223-2011).Higher concentration NO obtained in denitration material regenerative processxIt is prepared into nitric acid
In system, with O2For oxidant, H2O is solvent, and reaction temperature is set as 25 DEG C, and the reaction time is set as 1min, and reaction pressure is set
It is set to 0.02MPa, the nitric acid product that mass percentage is not less than 60% is obtained after after chemical reaction and concentration.
Embodiment 3
Coking flue gas is handled, flue gas is after waste heat recycles, and exhaust gas temperature is 25 DEG C, NOxContent is
1500mg/m3.Denitration process is carried out to flue gas using ADSORPTION IN A FIXED BED technique, denitration temperature is set as 25 DEG C, and regeneration temperature is set
It is set to 105 DEG C.After treatment, NO in flue gasxContent is down to 120mg/m3, reach " coking chemistry emission of industrial pollutants mark
It is quasi- " the especially requirement of emission limit in (GB 16171-2012).Higher concentration NO obtained in denitration material regenerative processxInto
In nitric acid preparation system, using air as oxidant, H2O2For solvent, reaction temperature is set as 55 DEG C, and the reaction time is set as
15min, reaction pressure are set as 0.9MPa, the nitre that mass percentage is not less than 60% are obtained after after chemical reaction and concentration
Acid product.
Embodiment 4
Coking flue gas is handled, flue gas is after waste heat recycles, and exhaust gas temperature is 25 DEG C, NOxContent is
1500mg/m3.Denitration process is carried out to flue gas using moving bed absorbing process, denitration temperature is set as 25 DEG C, and regeneration temperature is set
It is set to 105 DEG C.After treatment, NO in flue gasxContent is down to 108mg/m3, reach " coking chemistry emission of industrial pollutants mark
It is quasi- " the especially requirement of emission limit in (GB 16171-2012).Higher concentration NO obtained in denitration material regenerative processxInto
In nitric acid preparation system, using air as oxidant, H2O2For solvent, reaction temperature is set as 55 DEG C, and the reaction time is set as
15min, reaction pressure are set as 0.9MPa, the nitre that mass percentage is not less than 60% are obtained after after chemical reaction and concentration
Acid product.
Embodiment 5
Industrial Boiler flue gas is handled, flue gas is after waste heat recycles, and exhaust gas temperature is 75 DEG C, NOxContent is
750mg/m3.Denitration process is carried out to flue gas using ADSORPTION IN A FIXED BED technique, denitration temperature is set as 75 DEG C, and regeneration temperature is set
It is set to 155 DEG C.After treatment, NO in flue gasxContent is down to 65mg/m3, reach " emission standard of air pollutants for boilers "
(GB13271-2014) requirement of special emission limit in.Higher concentration NO obtained in denitration material regenerative processxInto nitric acid
In preparation system, with O3For oxidant, HNO3For solvent, reaction temperature is set as 75 DEG C, and the reaction time is set as 30min, reaction
Pressure is set as 0.5MPa, and the nitric acid product that mass percentage is not less than 60% is obtained after after chemical reaction and concentration.
Embodiment 6
Industrial Boiler flue gas is handled, flue gas is after waste heat recycles, and exhaust gas temperature is 75 DEG C, NOxContent is
750mg/m3.Denitration process is carried out to flue gas using moving bed absorbing process, denitration temperature is set as 75 DEG C, regeneration temperature setting
It is 155 DEG C.After treatment, NO in flue gasxContent is down to 73mg/m3, reach " emission standard of air pollutants for boilers "
(GB13271-2014) requirement of special emission limit in.Higher concentration NO obtained in denitration material regenerative processxInto nitric acid
In preparation system, with O3For oxidant, HNO3For solvent, reaction temperature is set as 75 DEG C, and the reaction time is set as 30min, reaction
Pressure is set as 0.5MPa, and the nitric acid product that mass percentage is not less than 60% is obtained after after chemical reaction and concentration.
Claims (7)
1. realizing NO in ultralow temperature flue gasxThe process system of efficient removal and its resource utilization, which is characterized in that including being used for
The smoke inlet pipe (1) of upstream workshop section flue gas is conveyed, smoke inlet pipe (1) has by piping connection for the cigarette to upstream workshop section
Gas carries out the heat exchanger (2) of waste heat recycling, and the outlet of heat exchanger (2) has by piping connection for carrying out denitration to flue gas and inciting somebody to action
Denitration material for denitration carries out regenerated adsorption-regeneration system, and adsorption-regeneration system passes through air-introduced machine (4) and chimney (5)
Connection；Adsorption-regeneration system is also connected with the NO for storing the higher concentration obtained after regeneration in adsorption-regeneration systemx's
The outlet of air accumulator (7), air accumulator (7) is connected with nitric acid preparation system.
2. NO in realization ultralow temperature flue gas according to claim 1xThe process system of efficient removal and its resource utilization,
It is characterized in that, adsorption-regeneration system includes ADSORPTION IN A FIXED BED tower A (3) and ADSORPTION IN A FIXED BED tower B (6), heat exchanger (2) goes out
Mouth is divided into two-way and the entrance with ADSORPTION IN A FIXED BED tower A (3) and ADSORPTION IN A FIXED BED tower B (6) passes through piping connection respectively；Fixed bed
The outlet of adsorption tower A (3) and ADSORPTION IN A FIXED BED tower B (6) pass through pipeline and connect with air-introduced machine (4)；ADSORPTION IN A FIXED BED tower A (3)
Outlet with ADSORPTION IN A FIXED BED tower B (6) is also connect by pipeline with air accumulator (7) respectively；Smoke inlet pipe (1) by pipeline with
Air-introduced machine (4) connection；
On the pipeline that smoke inlet pipe (1) is connect with heat exchanger (2), heat exchanger (2) and ADSORPTION IN A FIXED BED tower A (3) and fixed bed
On the pipeline of adsorption tower B (6) connection, the outlet and air-introduced machine (4) of ADSORPTION IN A FIXED BED tower A (3) and ADSORPTION IN A FIXED BED tower B (6) are even
On the pipeline connect, on the pipeline that the outlet of ADSORPTION IN A FIXED BED tower A (3) and ADSORPTION IN A FIXED BED tower B (6) are connect with air accumulator (7) with
And control valve is equipped on the pipeline that connect with air-introduced machine (4) of smoke inlet pipe (1).
3. NO in realization ultralow temperature flue gas according to claim 2xThe process system of efficient removal and its resource utilization,
It is characterized in that, the outlet of ADSORPTION IN A FIXED BED tower A (3) and ADSORPTION IN A FIXED BED tower B (6) are in parallel, and entirety and air-introduced machine after parallel connection
(4) it connects, control valve is equipped on the pipeline after parallel connection；
The outlet of ADSORPTION IN A FIXED BED tower A (3) and the outlet of ADSORPTION IN A FIXED BED tower B (6) are respectively arranged to control ADSORPTION IN A FIXED BED
Gas in tower A (3) and ADSORPTION IN A FIXED BED tower B (6) is passed through the control valve of air-introduced machine (4).
4. NO in realization ultralow temperature flue gas according to claim 2xThe process system of efficient removal and its resource utilization,
It is characterized in that, the outlet of ADSORPTION IN A FIXED BED tower A (3) and ADSORPTION IN A FIXED BED tower B (6) are in parallel, and entirety and air accumulator after parallel connection
(7) it connects；
The outlet of ADSORPTION IN A FIXED BED tower A (3) and the outlet of ADSORPTION IN A FIXED BED tower B (6) are respectively arranged to control ADSORPTION IN A FIXED BED
Gas in tower A (3) and ADSORPTION IN A FIXED BED tower B (6) is passed through the control valve of air accumulator (7).
5. NO in realization ultralow temperature flue gas according to claim 1xThe process system of efficient removal and its resource utilization,
It is characterized in that, adsorption-regeneration system includes moving bed adsorption tower (10) and moving bed regenerator (11), heat exchanger (2) goes out
The gas access of mouth and moving bed adsorption tower (10) passes through piping connection；The gas vent of moving bed adsorption tower (10) passes through pipeline
It is connect with air-introduced machine (4)；The denitration material outlet of moving bed adsorption tower (10) is connect with the feed bin of moving bed regenerator (11)；It moves
The denitration material outlet of dynamic bed regenerator (11) is connect with the feed bin of moving bed adsorption tower (10), the gas of moving bed regenerator (11)
Body outlet passes through piping connection with air accumulator (7)；Smoke inlet pipe (1) is connect by pipeline with air-introduced machine (4)；
On the pipeline that smoke inlet pipe (1) is connect with heat exchanger (2), outlet and moving bed adsorption tower (10) of heat exchanger (2)
On the pipeline of gas access connection, on the pipeline that the gas vent of moving bed adsorption tower (10) is connect with air-introduced machine (4), moving bed
On the pipeline that the gas vent of regenerator (11) is connect with air accumulator (7) and smoke inlet pipe (1) connect with air-introduced machine (4)
Control valve is equipped on pipeline.
6. NO in realization ultralow temperature flue gas according to claim 5xThe process system of efficient removal and its resource utilization,
It is characterized in that, the denitration material outlet of moving bed adsorption tower (10) is connected by conveyer belt and the feed bin of moving bed regenerator (11)
It connects；The denitration material outlet of moving bed regenerator (11) is connect by conveyer belt with the feed bin of moving bed adsorption tower (10).
7. NO in realization ultralow temperature flue gas according to claim 1xThe process system of efficient removal and its resource utilization,
It is characterized in that, nitric acid preparation system includes nitric acid reaction device (8) and nitric acid storage tank (9), the entrance of nitric acid reaction device (8) passes through
Pipeline is connect with air accumulator (7), and outlet is connect by pipeline with nitric acid storage tank (9)；Nitric acid reaction device (8) and air accumulator (7)
Connecting line and be equipped with control valve on the connecting line of nitric acid storage tank (9).
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| CN201810108339.1A CN108310968A (en) | 2018-02-02 | 2018-02-02 | NO in a kind of realization ultralow temperature flue gasxThe method and process system of efficient removal and its recycling |
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| CN201821554358.9U Active CN208990559U (en) | 2018-02-02 | 2018-09-21 | Realize NO in ultralow temperature flue gasxThe process system of efficient removal and its resource utilization |
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| CN111603886A (en) * | 2020-05-29 | 2020-09-01 | 北京科技大学 | NOx recovery method and device in three-tower switching mode |
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| WO2020083167A1 (en) * | 2018-10-22 | 2020-04-30 | 上海必修福企业管理有限公司 | Engine exhaust ozone purification system and method |
| CN109794137B (en) * | 2019-01-15 | 2021-04-16 | 北京科技大学 | Method and system for adsorbing, purifying, enriching and recovering nitrogen oxides in flue gas |
| CN109794135A (en) * | 2019-01-15 | 2019-05-24 | 北京科技大学 | Flue gas multiple pollutant adsorbing and removing and method of resource based on UTILIZATION OF VESIDUAL HEAT IN |
| CN109821416A (en) * | 2019-03-28 | 2019-05-31 | 东北大学 | A kind of method and system of low-temperature flue gas removing nitrogen oxides |
| GB2593593B (en) * | 2019-10-29 | 2024-07-03 | Huaneng Clean Energy Res Inst | Low-temperature adsorption denitration method for flue gas |
| CN110743313A (en) | 2019-10-29 | 2020-02-04 | 中国华能集团有限公司 | Low-temperature flue gas adsorption denitration method |
| GB2595553B (en) * | 2019-10-29 | 2024-02-07 | Huaneng Clean Energy Res Inst | Low-temperature adsorption flue gas denitration system and process |
| CN110743312A (en) * | 2019-10-29 | 2020-02-04 | 中国华能集团有限公司 | Flue gas low-temperature adsorption denitration system and process |
| CN111495113A (en) * | 2020-05-18 | 2020-08-07 | 中国华能集团有限公司 | Fixed bed type low-temperature flue gas adsorption desulfurization system and method |
| CN111841065A (en) * | 2020-08-14 | 2020-10-30 | 中国华能集团清洁能源技术研究院有限公司 | Near-zero emission type integrated removal system and method for multiple pollutants in flue gas |
| CN112191073A (en) * | 2020-10-21 | 2021-01-08 | 西安热工研究院有限公司 | Integrated removing device for smoke pollutants |
| CN113834341A (en) * | 2021-09-28 | 2021-12-24 | 中国华能集团清洁能源技术研究院有限公司 | Low-temperature desulfurization and denitrification method and system for cement plant flue gas |
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| CN111603886A (en) * | 2020-05-29 | 2020-09-01 | 北京科技大学 | NOx recovery method and device in three-tower switching mode |
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