CN106310880A - Device and method for removing NO - Google Patents
Device and method for removing NO Download PDFInfo
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- CN106310880A CN106310880A CN201610936862.4A CN201610936862A CN106310880A CN 106310880 A CN106310880 A CN 106310880A CN 201610936862 A CN201610936862 A CN 201610936862A CN 106310880 A CN106310880 A CN 106310880A
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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
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
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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
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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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
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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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
- B01D53/22—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
- B01D53/228—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 characterised by specific membranes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/404—Nitrogen oxides other than dinitrogen oxide
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- General Chemical & Material Sciences (AREA)
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- Treating Waste Gases (AREA)
Abstract
The invention discloses a device and method for removing NO. A flue gas generated in a boiler enters a wet desulphurization unit after dedusting treatment, and the temperature is lowered to about 50 DEG C after desulphurization; then the flue gas enters a first adsorption/desorption column which performs adsorption removal on NO in the flue gas, then the flue gas enters an NO concentration analyzer which measures the concentration of NO, the flue gas is discharged if the NO concentration reaches a standard, the flue gas is switched into a second adsorption/desorption column which performs adsorption removal on the NO if the NO concentration is out of a limit, meanwhile, part of the high-temperature flue gas after dedusting is introduced into the first adsorption/desorption column to perform desorption on an adsorbent, and the NO after desorption enters a hollow fibrous membrane for chemical absorption; and when the NO concentration at the outlet of the second adsorption/desorption column is out of a limit, the flue gas is switched into the first adsorption/desorption column, and by virtue of alternate operation of the two adsorption/desorption columns and the chemical absorption of the hollow fibrous membrane, high-efficiency removal of the NO in the flue gas is achieved.
Description
Technical field
The present invention relates to tail gas disposal technique field, remove NO device it is more particularly related to a kind of and take off
Except method, espespecially use NO pre-concentration and the device of Hollow Fiber Membrane Absorption removing NO and removing NO method.
Background technology
NOxIt it is the one of the main reasons causing the environmental problem such as acid rain and photochemical fog.Along with China industry continuous
Development, and affected by the energy resource structure based on coal, China's nitrogen oxides pollution situation is serious, prevention and control situation is severe.According to system
Meter, electric power and thermoelectricity industry discharged nitrous oxides account for the 66.7% of Industrial Nitrogen emissions of oxides.Along with day by day carrying of environmental requirement
Height, newly-built coal-burning power plant of China has all installed denitrification apparatus additional, implements stricter NO in " 12 " period simultaneouslyxDischarge
Standard, the NO the most serious to control ChinaxPollute.
Currently for NOxRemoving sulfuldioxide be broadly divided into two classes: one is to remove in burning, i.e. uses low NOxBurning skill
Art, the NO that in minimizing burner hearth, coal combustion generatesxAmount；Another kind is removing after burning, i.e. removes NO from flue gasx, typically have choosing
Selecting property catalytic reduction method and SNCR method.For low NOxCombustion technology, general denitration efficiency is low, and may
Stove internal corrosion, slagging scorification can be caused, even reduce efficiency of combustion.For selective catalytic reduction and SNCR
Method, although have higher removal efficiency, but occupation area of equipment is big, investment and operating cost are high, and secondary the most also can be caused dirty
Dye.
Chinese patent CN102553416 discloses a kind of method of power-plant flue gas denitration and absorbent used thereof.The party
Method be characterized by absorption tower, use by H2O2It is additive with modified Fenton reaction and the EDTA of iron sulfate composition
Aqueous solution, as absorbent, under conditions of control temperature is 30-80 DEG C, makes NO aoxidize in absorption tower and then be absorbed by absorbent
Thus complete denitration.But the method is in advance by H2O2With Fe2(SO4)3Solution mixes, H2O2Consumption is relatively big, relatively costly.
Chinese patent CN103007753 discloses a kind of heterogeneous Fenton reagent and its preparation method and application.The party
Method is characterised by that described heterogeneous Fenton reagent is by H2O2Aqueous solution and Al2O3The PH of load Fe catalyst composition is 5-6's
Mixed solution.Method of denitration is to add heterogeneous Fenton reagent in conventional bubble tower, is oxidized to by the NO in flue gas
HNO3.The method H2O2Consumption is big, cost is high.
Chinese patent CN105561769 discloses denitrification apparatus and the method for a kind of salt strengthening hydrogen peroxide solution oxidation NO.
The method is characterized in that and utilize absorbent to absorb the nitrogen oxides in flue gas in bubbling reactor, absorbent used is H2O2
Mixed solution with salt.But the method can only process a small amount of flue gas, H2O2Consumption is big, cost is high, inefficient.
There is no a kind of efficient, method of denitration of low cost being applicable to medium small boiler flue gas at present, therefore, find one
Plant Low investment and operating cost, efficient denitration technology are still the task of top priority.
Summary of the invention
It is an object of the invention to solve at least the above, and the advantage that at least will be described later is provided.
It is a still further object of the present invention to provide a kind of removing NO device and removal methods thereof, espespecially use NO pre-concentration and
The device of Hollow Fiber Membrane Absorption removing NO and removal methods, it is achieved efficient, the denitration of low cost of medium small boiler flue gas.
In order to realize according to object of the present invention and further advantage, it is provided that a kind of removing NO device, including:
Dust removing units, its import connects with boiler；
Desulfurization unit, its import and described dust removing units outlet；
First adsorption/desorption tower, its import is by the first stop valve and described desulfurization unit outlet；
Oneth NO concentration analyzer, its import by the second stop valve and described first adsorption/desorption tower outlet, described the
One NO concentration analyzer outlet is outwardly open；
Second adsorption/desorption tower, its import is by the 4th stop valve and described desulfurization unit outlet；
2nd NO concentration analyzer, its import by the 9th stop valve and described second adsorption/desorption tower outlet, described the
Two NO concentration analyzer outlets are outwardly open；
Hollow fiber membrane reactor, its gas access is adsorbed with described first adsorption/desorption tower outlet and described second/is solved respectively
Inhaling the connection of tower egress selection, described hollow fiber membrane reactor gas outlet is outwardly open；
Wherein, being provided with the first heating coil in described first adsorption/desorption tower, described first heating coil import passes through the 6th
Stop valve and described dust removing units outlet, described first heating coil outlet is by the 5th stop valve and described desulfurization unit
Inlet communication, is provided with the second heating coil in described second adsorption/desorption tower, described second heating coil import passes through the 7th
Stop valve and described dust removing units outlet, described second heating coil outlet is by the 8th stop valve and described desulfurization unit
Inlet communication.
Preferably, described first adsorption/desorption tower and the second adsorption/desorption tower structure are identical, described first adsorption/desorption
If being provided with the dividing plate that dried layer is evenly arranged in tower, described dividing plate is axially vertical with tower body, and described dividing plate is evenly arranged activated carbon
Adsorbent.
Preferably, described first heating coil spirals and is arranged in described first adsorption/desorption tower, and described first heating
Coil pipe runs through the described dividing plate of each layer and contacts with described acticarbon.
Preferably, the absorption temperature of described first adsorption/desorption tower and the second adsorption/desorption tower is 50 DEG C, desorption temperature
It it is 300 DEG C.
Preferably, if being provided with dry film silk, the gas of described hollow fiber membrane reactor in described hollow fiber membrane reactor
Entrance and gas outlet diagonal angle are opened in hollow fiber membrane reactor shell wall two ends, and gas forward flows through hollow fiber membrane reactor
Shell side, absorbing liquid inversely flows through the tube side of film silk.
Preferably, the operation temperature of described hollow fiber membrane reactor is 50～80 DEG C, and gas-liquid flow-rate ratio is 5:1.
Preferably, described hollow fiber membrane reactor is made up of polypropylene material, and described absorbing liquid is by 0.5wt% H2O2、
The aqueous solution composition of 30wt%NaCl.
Preferably, described hollow fiber membrane reactor gas access is by the 3rd stop valve and described first adsorption/desorption
Tower outlet, by the tenth stop valve and described second adsorption/desorption tower outlet.
A kind of removing NO method, comprises the following steps:
Step one, open first, second stop valve, close the 3rd to the tenth stop valve, through the flue gas removing dust that boiler produces
Enter desulfurization unit desulfurization after unit dedusting, will flue gas lower the temperature after send into the first adsorption/desorption tower removing NO, be subsequently sent to the
Detection NO concentration in one NO concentration analyzer, if to record NO concentration up to standard, then by flue gas from first for a NO concentration analyzer
NO concentration analyzer outlet directly discharge, otherwise enters step 2；
Step 2, close first, second stop valve, open the four, the 9th stop valves, the flue gas after desulfurization is introduced the second suction
Attached/desorber removes NO, is subsequently sent in the 2nd NO concentration analyzer detection NO concentration, and open the three, the 5th and
6th stop valve, draws a road high-temperature flue gas from dust removing units and flows through the first heating coil, by activity in the first adsorption/desorption tower
Being back to desulfurization unit after carbon adsorbent desorbing, the higher concentration NO gas simultaneously desorbed by the first adsorption/desorption tower is through hollow
Fibrous membrane reactor directly discharges after absorbing；If it is up to standard that the 2nd NO concentration analyzer records NO concentration, then by flue gas from second
NO concentration analyzer outlet directly discharge, otherwise enters step 3；
Step 3, closedown the 3rd to the 9th stop valve, open first, second stop valve, the flue gas after desulfurization introduced first
Adsorption/desorption tower removes NO, and sends into detection NO concentration in a NO concentration analyzer, meanwhile, open the seven, the 8th and
Tenth stop valve, draws a road high-temperature flue gas from dust removing units and flows through the second heating coil, by activity in the second adsorption/desorption tower
Being back to desulfurization unit after carbon adsorbent desorbing, the higher concentration NO gas simultaneously desorbed by the second adsorption/desorption tower is through hollow
Fibrous membrane reactor directly discharges after absorbing NO；If it is up to standard that a NO concentration analyzer records NO concentration, then by flue gas from
One NO concentration analyzer outlet directly discharge, otherwise returns to step 2.
Preferably, the higher concentration NO gas that first, second adsorption/desorption tower desorbs is passed through hollow fiber membrane reactor
Shell side inlet, hollow fiber membrane reactor shell side relative to shell side reverse flow oxidative absorption NO, is gone out in tube side by absorbing liquid
Mouth effluent air directly discharges.
The present invention at least includes following beneficial effect:
1, the difficult point using the NO of conventional oxidation method removal flue gas is that the concentration of NO is the lowest, needs substantial amounts of absorbing liquid ability
Realize the efficient removal of NO, cause that equipment investment is big, reagent loss is big, operating cost is high, and the present invention is by two alternately fortune
The adsorption/desorption tower of row carries out concentration to the NO in flue gas, then passes through absorbing liquid in hollow fiber membrane reactor by dense
The NO of contracting efficiently removes, and equipment investment is few, plant area is little, absorbing liquid consumption is greatly decreased, operating cost significantly reduces；
2, present invention is especially suited for the nitrogen oxides of the power-equipment of the enterprises such as middle-size and small-size steam power plant, cement plant, small-sized petrochemical plant
Remove, be suitable to promote on a large scale.
Part is embodied by the further advantage of the present invention, target and feature by description below, and part also will be by this
Invention research and practice and be understood by the person skilled in the art.
Accompanying drawing explanation
Fig. 1 is the structural representation that the present invention removes NO device；
Fig. 2 is the structural representation of described hollow fiber membrane reactor；
Fig. 3 is adsorption/desorption tower structure schematic diagram；
In the figures above: 1: boiler；2: dust removing units；3: desulfurization unit；4: the first adsorption/desorption towers；5: the second adsorption/desorptions
Tower；6: the one NO concentration analyzers；7: the two NO concentration analyzers；8: hollow fiber membrane reactor；9: the first drains；10:
Second drain；11～20: the first cut-off～the tenth stop valves；21: gas feed；22: absorbing liquid import；23: gas goes out
Mouthful；24: absorbing liquid exports；25: the first heating coils；26: the second heating coils；401(501): adsorption/desorption tower import；402
(502): adsorption/desorption tower exports；403(503): heating coil import；404(504): heating coil exports；405(505): live
Property carbon adsorbent；406(506): dividing plate；801: film silk.
Detailed description of the invention
The present invention is described in further detail below in conjunction with the accompanying drawings, to make those skilled in the art with reference to description literary composition
Word can be implemented according to this.
Should be appreciated that used herein such as " have ", " comprising " and " including " term do not allot one or many
Other element individual or the existence of a combination thereof or interpolation.
In a kind of embodiment, as shown in Figures 1 to 3, flue gas is removed NO device and builds as shown in Figure 1, concrete,
Being connected by pipeline with a dust removing units 2 by boiler 1, dust removing units 2 exports a road and is connected with wet desulphurization unit 3, dedusting
Unit 2 second tunnel is connected by pipeline with the first heating coil 25 in the first adsorption/desorption tower 4, and pipeline is provided with the 6th
Stop valve 16, dust removing units 2 the 3rd tunnel is connected by pipeline, on pipeline with the second heating coil 26 in the second adsorption/desorption tower 5
7th stop valve 17 is installed；The first heating coil 25 outlet in first adsorption/desorption tower 4 and wet desulphurization unit 3 import
Being connected by pipeline, pipeline is provided with the 5th stop valve 15, the second heating coil 26 in the second adsorption/desorption tower 5 exports
It is connected by pipeline with wet desulphurization unit 3 import, pipeline is provided with the 8th stop valve 18；Flue gas through desulfurization unit
One road and the first adsorption/desorption tower 4 are connected by pipeline, and pipeline is provided with the first stop valve 11, the flue gas of desulfurization unit
Two roads and the second adsorption/desorption tower 5 are connected by pipeline, and pipeline is provided with the 4th stop valve 14；First adsorption/desorption tower 4
Export a road and a NO concentration analyzer 6 is connected by pipeline, pipeline is provided with the second stop valve 12, the first absorption/solve
The other road that exports inhaling tower 4 is connected by pipeline with the gas access 21 of hollow fiber membrane reactor 8, and pipeline is provided with the
Three stop valves 13；Outlet one road and the 2nd NO concentration analyzer 7 of the second adsorption/desorption tower 5 are connected by pipeline, and pipeline is pacified
Equipped with the 9th stop valve 19, the other road of outlet of the second adsorption/desorption tower 5 and the gas access of hollow fiber membrane reactor 8
21 are connected by pipeline, and pipeline is provided with the tenth stop valve 20；The gas outlet 23 of hollow-fibre membrane 8 and a NO concentration are divided
Analyzer 6 exports and is connected with the first drain 9 respectively；The outlet of the 2nd NO concentration analyzer 7 is connected with the second drain 10.
The flue gas removing dust produced in boiler enters wet desulphurization unit after processing, and after desulfurization, temperature is down to 50 DEG C of left sides
Right；Subsequently into first adsorption/desorption tower, the NO in flue gas being carried out Adsorption, flue gas subsequently enters NO concentration and divides
The concentration of NO is measured by analyzer, if NO concentration is up to standard, discharges, if exceeded standard, flue gas is switched to second absorption/
Desorber carries out adsorbing and removing to NO, is passed through in first adsorption/desorption tower high-temperature flue gas after part dedusting to suction simultaneously
Attached dose carries out desorbing, and the NO desorbed enters hollow-fibre membrane and carries out chemical absorbing；When second adsorption/desorption tower outlet NO is dense
Degree exceeds standard, and flue gas is switched to first adsorption/desorption tower, high-temperature flue gas after part dedusting is passed through second simultaneously
In adsorption/desorption tower, adsorbent being carried out desorbing, the NO desorbed enters hollow-fibre membrane and carries out chemical absorbing；By two suctions
The alternate run of attached/desorber and the chemical absorbing of hollow-fibre membrane realize the efficient removal of flue gas NO.
In another kind of embodiment, the flue gas that boiler produces is 2000Nm3/ hour, the concentration of NO is 300ppm.The first,
Second adsorption/desorption tower structure as it is shown on figure 3, and described first adsorption/desorption tower and the second adsorption/desorption tower structure identical,
Tower body material is rustless steel, and tower internal diameter is 1400mm, tower height 2500mm, is evenly arranged 4 layers of dividing plate dividing plate 406 in tower vertically
(506), the most described dividing plate is axially vertical with tower body, and dividing plate is evenly arranged acticarbon 405(505), inside tower
Being provided with serpentine METAL HEATING PROCESS coil pipe 25,26, coil pipe nominal diameter is 50mm, and heating coil run through the described dividing plate of each layer with
Described acticarbon contacts, the contact area contacted with acticarbon with raising, and then improves acticarbon
Desorption efficiency.The absorption temperature of described first adsorption/desorption tower and the second adsorption/desorption tower is 50 DEG C, desorption temperature is 300
DEG C, the NO in flue gas is efficiently absorbed in described first adsorption/desorption tower and the second adsorption/desorption tower.
Hollow fiber membrane reactor 8 as in figure 2 it is shown, material polypropylene material, hollow fiber membrane reactor a length of
2000mm, reactor inside diameter is 1500mm, and external diameter is 1540mm, and reactor is contained within 12000 film silks 801, and film silk internal diameter is
0.38mm, the external diameter of film silk is 0.5mm, and the effective length of film silk is 2000mm, and film silk porosity is 65%, film silk average pore size
It is 0.21 m.Gas access and the gas outlet diagonal angle of described hollow fiber membrane reactor are opened in hollow fiber membrane reactor shell
Wall two ends, gas forward flows through the shell side of hollow fiber membrane reactor, and absorbing liquid inversely flows into from absorbing liquid import 22, absorbing liquid
Outlet 24 outflow, flows through the tube side of film silk, say, that absorbing liquid is walked inside film silk, and flue is made leave with rage outside film silk, flow direction
Contrary with gas, the operation temperature of described hollow fiber membrane reactor is 50～80 DEG C, and gas-liquid flow-rate ratio is 5:1, described absorption
Liquid is by 0.5wt% H2O2, 30wt%NaCl aqueous solution composition.Described first adsorption/desorption tower and the second adsorption/desorption tower are lived
Property the higher concentration NO gas that parses of carbon adsorbent directly discharge after hollow fiber membrane reactor 8 absorbs, it is achieved that flue gas
The continuous operation of removing NO, in blowdown stack gas, the concentration of NO is consistently lower than 50ppm, and absorbing liquid consumption is greatly decreased and can weigh
Multiple recycling, operating cost significantly reduces.
Removing NO method is as follows:
Step one, open first stop valve the 11, second stop valve 12, close the 3rd stop valve 13 to the tenth stop valve 20, through pot
Desulfurization unit 3 desulfurization is entered after flue gas removing dust unit 2 dedusting that stove 1 produces, and by about flue gas cool-down to 50 DEG C, then
Entering the first adsorption/desorption tower 4, flue gas is tightly held by activated carbon agent in tower and optionally adsorbs NO, and flue gas enters subsequently
Oneth NO concentration analyzer 6, in NO concentration analyzer 6 exhaust pass gas, NO concentration was respectively less than 50ppm in 2 hours, met ring
Guaranteed request, NO concentration analyzer 6 exhaust pass gas is directly vented in air；After running 2 hours, a NO concentration analyzer 6
In exhaust pass gas, NO concentration is more than 50ppm, then enter step 2；
Step 2, close first stop valve the 11, second stop valve 12, open the 4th stop valve 14 and the 9th stop valve 19, will be through
Flue gas after desulfurization unit 3 introduces and carries out NO removing in the second adsorption/desorption tower 5, meanwhile, open the 3rd stop valve 13,
Five stop valve 15 and the 6th stop valves 16, draw the flue gas on 300 DEG C of a road through the first adsorption/desorption tower 4 from dust removing units 2
The first heating coil 25 give acticarbon desorbing after enter desulfurization unit 3, be directly entered desulfurization with removing dust unit 2
Entering in the second adsorption/desorption tower 5 after the flue gas mixing of unit 3, flue gas is tightly held by activated carbon agent optionally in tower
Absorption NO, flue gas enters the 2nd NO concentration analyzer 7 subsequently, and in NO concentration analyzer 7 exhaust pass gas, NO concentration is from dress
Putting and be respectively less than 50ppm in bringing into operation 2-4 hour, meet environmental requirement, NO concentration analyzer 7 exhaust pass gas is directly vented to
In air.The gas containing 99%NO that first adsorption/desorption tower 4 desorbs is passed through the shell side gas of hollow fiber membrane reactor 8
Body entrance 21, absorbing liquid at tube side relative to shell side reverse flow oxidative absorption NO, from hollow fiber membrane reactor 8 shell side gas
Export 23 effluent airs to be directly vented, thus, the adsorption/desorption tower of two alternate runs to NO concentration in flue gas from
300ppm carries out concentration to 99%, is finally parsed by this higher concentration NO gas and is absorbed by hollow fiber membrane reactor 8.Hollow is fine
The operation temperature of dimension membrane reactor 8 is 50-80 DEG C, and gas-liquid flow-rate ratio is 5:1.Absorbing liquid consist of 0.5wt% H2O2、30wt%
The aqueous solution of NaCl.After device brings into operation 4 hours, the 2nd NO concentration analyzer 7 exit NO concentration is more than 50ppm, enters
Step 3；
Step 3, closedown the 3rd to the 9th stop valve, open first stop valve the 11, second stop valve 12, will be after desulfurization unit 3
Flue gas introduce in the first adsorption/desorption tower 4 and carry out NO removing.Meanwhile, open the 7th stop valve the 17, the 8th stop valve 18,
Tenth stop valve 20, draws the flue gas on 300 DEG C of a road the second heating coil through the second adsorption/desorption tower 5 from dust removing units 2
26 give entrance desulfurization unit 3 after acticarbon desorbing, in the flue gas being directly entered desulfurization unit 3 with removing dust unit 2
Entering in the first adsorption/desorption tower 4 after mixing, flue gas is tightly held by activated carbon agent in tower and optionally adsorbs NO, subsequently cigarette
Road gas enters a NO concentration analyzer 6, and in NO concentration analyzer 6 exhaust pass gas, NO concentration is the least in running 4-6 hour
In 50ppm, meet environmental requirement, then the flue gas of NO concentration analyzer 6 outlet is directly vented in air.Inhale second
The highly concentrated NO gas that attached/desorber 5 desorbs is passed through the shell side inlet of hollow fiber membrane reactor 8, and absorbing liquid is relative at tube side
In shell side reverse flow oxidative absorption NO, directly it is vented from hollow fiber membrane reactor 8 shell-side outlet effluent air.Along with holding
Reforwarding row, until when a NO concentration analyzer 6 exit NO concentration is more than 50ppm, returning to step 2, repeats step 2 and step
Rapid three, it is achieved the continuous operation of flue gas removing NO, in blowdown stack gas, the concentration of NO is consistently lower than 50ppm.
From embodiment, the present invention by the adsorption/desorption tower of two alternate runs to NO concentration in flue gas from
300ppm carries out concentration to 99%, is then efficiently removed by the NO of concentration by absorbing liquid in hollow fiber membrane reactor, it is achieved
The continuous operation of flue gas removing NO, in blowdown stack gas, the concentration of NO is consistently lower than 50ppm.The cigarette that this invention is relatively conventional
Gas denitrating technique, equipment is mainly the stainless head tower of two normal pressures and a hollow fiber membrane reactor, and equipment investment is few, device
Take up an area little；The absorbing liquid consumption used is greatly decreased and repeatable recycling, and operating cost significantly reduces.Meanwhile, the present invention
The nitrogen oxides of the power-equipment being particularly suitable for the enterprises such as middle-size and small-size steam power plant, cement plant, small-sized petrochemical plant is removed, and is suitable to big model
Enclose popularization.
Although embodiment of the present invention are disclosed as above, but it is not restricted in description and embodiment listed
Using, it can be applied to various applicable the field of the invention completely, for those skilled in the art, and can be easily
Realizing other amendment, therefore under the general concept limited without departing substantially from claim and equivalency range, the present invention does not limit
In specific details with shown here as the legend with description.
Claims (10)
1. a removing NO device, it is characterised in that including:
Dust removing units, its import connects with boiler；
Desulfurization unit, its import and described dust removing units outlet；
First adsorption/desorption tower, its import is by the first stop valve and described desulfurization unit outlet；
Oneth NO concentration analyzer, its import by the second stop valve and described first adsorption/desorption tower outlet, described the
One NO concentration analyzer outlet is outwardly open；
Second adsorption/desorption tower, its import is by the 4th stop valve and described desulfurization unit outlet；
2nd NO concentration analyzer, its import by the 9th stop valve and described second adsorption/desorption tower outlet, described the
Two NO concentration analyzer outlets are outwardly open；
Hollow fiber membrane reactor, its gas access is adsorbed with described first adsorption/desorption tower outlet and described second/is solved respectively
Inhaling the connection of tower egress selection, described hollow fiber membrane reactor gas outlet is outwardly open；
Wherein, being provided with the first heating coil in described first adsorption/desorption tower, described first heating coil import passes through the 6th
Stop valve and described dust removing units outlet, described first heating coil outlet is by the 5th stop valve and described desulfurization unit
Inlet communication, is provided with the second heating coil in described second adsorption/desorption tower, described second heating coil import passes through the 7th
Stop valve and described dust removing units outlet, described second heating coil outlet is by the 8th stop valve and described desulfurization unit
Inlet communication.
2. removing NO device as claimed in claim 1, it is characterised in that described first adsorption/desorption tower and the second absorption/solution
Suction tower structure is identical, if being provided with, in described first adsorption/desorption tower, the dividing plate that dried layer is evenly arranged, described dividing plate is axial with tower body
Vertically, described dividing plate is evenly arranged acticarbon.
3. removing NO device as claimed in claim 2, it is characterised in that described first heating coil spirals and is arranged on described the
In one adsorption/desorption tower, and described first heating coil runs through the described dividing plate of each layer and contacts with described acticarbon.
4. removing NO device as claimed in claim 1, it is characterised in that described first adsorption/desorption tower and the second absorption/solution
The absorption temperature inhaling tower is 50 DEG C, desorption temperature is 300 DEG C.
5. removing NO device as claimed in claim 1, it is characterised in that if being provided with dry film in described hollow fiber membrane reactor
Silk, gas access and the gas outlet diagonal angle of described hollow fiber membrane reactor are opened in hollow fiber membrane reactor shell wall two
End, gas forward flows through the shell side of hollow fiber membrane reactor, and absorbing liquid inversely flows through the tube side of film silk.
6. removing NO device as claimed in claim 5, it is characterised in that the operation temperature of described hollow fiber membrane reactor is
50～80 DEG C, gas-liquid flow-rate ratio is 5:1.
7. removing NO device as claimed in claim 6, it is characterised in that described hollow fiber membrane reactor is by polypropylene material
Making, described absorbing liquid is by 0.5wt%H2O2, 30wt%NaCl aqueous solution composition.
8. removing NO device as claimed in claim 7, it is characterised in that described hollow fiber membrane reactor gas access is passed through
3rd stop valve and described first adsorption/desorption tower outlet, gone out with described second adsorption/desorption tower by the tenth stop valve
Mouth connection.
9. the removing NO method of a removing NO device as claimed in claim 8, it is characterised in that comprise the following steps:
Step one, open first, second stop valve, close the 3rd to the tenth stop valve, through the flue gas removing dust that boiler produces
Enter desulfurization unit desulfurization after unit dedusting, will flue gas lower the temperature after send into the first adsorption/desorption tower removing NO, be subsequently sent to the
Detection NO concentration in one NO concentration analyzer, if to record NO concentration up to standard, then by flue gas from first for a NO concentration analyzer
NO concentration analyzer outlet directly discharge, otherwise enters step 2；
Step 2, close first, second stop valve, open the four, the 9th stop valves, the flue gas after desulfurization is introduced the second suction
Attached/desorber removes NO, is subsequently sent in the 2nd NO concentration analyzer detection NO concentration, and open the three, the 5th and
6th stop valve, draws a road high-temperature flue gas from dust removing units and flows through the first heating coil, by activity in the first adsorption/desorption tower
Being back to desulfurization unit after carbon adsorbent desorbing, the higher concentration NO gas simultaneously desorbed by the first adsorption/desorption tower is through hollow
Fibrous membrane reactor directly discharges after absorbing；If it is up to standard that the 2nd NO concentration analyzer records NO concentration, then by flue gas from second
NO concentration analyzer outlet directly discharge, otherwise enters step 3；
Step 3, closedown the 3rd to the 9th stop valve, open first, second stop valve, the flue gas after desulfurization introduced first
Adsorption/desorption tower removes NO, and sends into detection NO concentration in a NO concentration analyzer, meanwhile, open the seven, the 8th and
Tenth stop valve, draws a road high-temperature flue gas from dust removing units and flows through the second heating coil, by activity in the second adsorption/desorption tower
Being back to desulfurization unit after carbon adsorbent desorbing, the higher concentration NO gas simultaneously desorbed by the second adsorption/desorption tower is through hollow
Fibrous membrane reactor directly discharges after absorbing NO；If it is up to standard that a NO concentration analyzer records NO concentration, then by flue gas from
One NO concentration analyzer outlet directly discharge, otherwise returns to step 2.
10. removing NO method as claimed in claim 9, it is characterised in that the height that first, second adsorption/desorption tower desorbs
Concentration NO gas is passed through the shell side inlet of hollow fiber membrane reactor, and absorbing liquid aoxidizes relative to shell side reverse flow in tube side
Absorb NO, hollow fiber membrane reactor shell-side outlet effluent air is directly discharged.
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| US5118328A (en) * | 1990-02-14 | 1992-06-02 | Fraunhofer Gesellschaft | Process for regenerating adsorbers |
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