CN109513341A - Pelletizing flue gas low-temperature desulfurization denitration method - Google Patents

Pelletizing flue gas low-temperature desulfurization denitration method Download PDF

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CN109513341A
CN109513341A CN201811493988.4A CN201811493988A CN109513341A CN 109513341 A CN109513341 A CN 109513341A CN 201811493988 A CN201811493988 A CN 201811493988A CN 109513341 A CN109513341 A CN 109513341A
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flue gas
zsm
temperature
zeolite
molecular sieve
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梁军
张燎原
杜军
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Shandong Zhoulan Environmental Protection Technology Co Ltd
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Shandong Zhoulan Environmental Protection Technology Co Ltd
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
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    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86Catalytic processes
    • B01D53/8621Removing nitrogen compounds
    • B01D53/8625Nitrogen oxides
    • B01D53/8628Processes characterised by a specific catalyst
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    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • 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
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    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
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    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/48Sulfur compounds
    • B01D53/50Sulfur oxides
    • B01D53/501Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B01D53/502Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
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    • 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
    • B01D53/78Liquid phase processes with gas-liquid contact
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23JREMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00Arrangements of devices for treating smoke or fumes
    • F23J15/02Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/04Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material using washing fluids
    • FMECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23JREMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00Arrangements of devices for treating smoke or fumes
    • F23J15/06Arrangements of devices for treating smoke or fumes of coolers
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    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D2253/00Adsorbents used in seperation treatment of gases and vapours
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    • B01D2253/106Silica or silicates
    • B01D2253/108Zeolites
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
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    • B01D2255/504ZSM 5 zeolites
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2257/00Components to be removed
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01DSEPARATION
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    • B01D2258/0283Flue gases
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2259/00Type of treatment
    • B01D2259/40Further details for adsorption processes and devices
    • B01D2259/40083Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
    • B01D2259/40088Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
    • B01D2259/4009Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas

Abstract

The present invention relates to a kind of method of pelletizing flue gas desulfurization and denitrification, mainly solves the problem of that existing pelletizing flue gas desulfurization and denitrification operating cost is high and generate secondary pollution.The present invention is by using the nitrogen oxides and sulfide in the method removing pelletizing flue gas of absorption, nitrogen oxides in effluent and sulfide after regeneration carry out the technical solution of salt manufacturing processing, preferably solves the above problem, this method can be used in the industrial production of steel plant's flue gas desulfurization and denitrification.

Description

Pelletizing flue gas low-temperature desulfurization denitration method
Technical field
The invention belongs to desulphurization denitration technical fields, and in particular to a kind of pelletizing flue gas desulfurization and denitration method.
Background technique
SO2And NOXIt is the important atmosphere pollution in China, excessive discharge will cause haze, acid rain and photochemical fog Deng serious harm ecological environment and human health.The burning of fossil fuel is SO2And NOXMain source.Coal be China most Important natural energy source, as the second largest coal field in China, carbonization of coal is one of industrial coal field primary pollution source, ball Group's flue gas is the important pollution sources of atmosphere.
Current pelletizing flue gas desulfurization field is using more for ammonia process, lime/lime stone method, Dual alkali, magnesium oxide method etc. For the Wet Flue Gas Desulfurization Technique and semi-dry desulphurization technology of representative.Wet desulphurization absorption rate is high, but such as lime/lime Stone-gypsum, Dual alkali contain small hydrophilic ionic in magnesium oxide method slurries, are taken out of by flue gas, and are emitted into big In gas, while these particle surfaces are easily absorbing sulfur dioxide, sulfur trioxide, hydrogen chloride, hydrogen fluoride, nitrogen oxides, nocuousness Organic matter and bacterium etc. cause atmosphere suspended particles (usually said PM100, PM10, PM2.5 etc.) content to dramatically increase, And cause haze and atmospheric photochemical reaction phenomenon, cause serious environmental pollution.Sodium sulfite (potassium) method sulfur removal technology, Wei Er Man-Luo Defa Desulfovibrio technique, organic acid-acylate buffer-solution method sulfur removal technology, regeneration steam energy consumption is big and regenerates Rate is low, therefore it is big to industrialize difficulty.Ammonia corrosion is big in the ammonia process of desulfurization, the production process of equipment burn into and ammonia is caused to be high energy Consumption, high pollution process.Semi-dry desulphurization equipment corrosion compared with wet desulphurization is small, spreads without obvious temperature drop, conducive to chimney exhaust, But desulfuration efficiency is relatively low, reaction speed is slow.
The mainstream technology in pelletizing denitrating flue gas field is NH3SCR denitration, SCR technology use catalyst, and catalytic action makes Reaction activity reduces.In steel plant, since flue gas self-temperature is very low (200 DEG C ~ 300 DEG C), it need to be urged using low-temperature denitration Agent carries out denitration reaction in this temperature range, and need to spray into ammonia into flue gas and make reducing agent.
Individual desulphurization and denitration technique not only takes up a large area, but also invests, operating cost height.Simultaneous SO_2 and NO removal skill Art, which has, reduces device configuration, saves space, material source is wide, and price is low, renewable the advantages that recycling.Wherein, with work Property charcoal (coke) technology be representative dry desulfurization denitrification integral technology be the technology most to the heat energy utilization in flue gas.
Chinese patent 201410119747.9 recycles stack gases waste heat using stack gases waste-heat recovery device, reduces The temperature of stack gases, the activated adoption ability having using coke and low-temperature denitration catalytic capability realize the de- of stack gases Sulphur, denitration integration.The concrete operation step of the invention is that 1) stack gases first pass through waste gas residual heat recovery unit, and flue is useless The waste heat of gas is recovered, and temperature is reduced to 100 DEG C ~ 150 DEG C, is subsequently entered in low-temperature SCR desulphurization denitration unit, in flue gas SO2It by coke adsorbing and removing, is mixed by the flue gas of desulfurization with ammonia, take coke as the catalyst of SCR method, denitration reduction occurs NO is completed in reactionXRemoving;2) coke in low-temperature SCR desulphurization denitration unit is supplied from by elevator and grader leveling blade The coke feed unit of conveyer composition, the coke after denitration reduction reaction is expelled in coke main tank, periodically by outlet vehicle It sends outside;3) flue gas of low-temperature SCR desulphurization denitration unit discharge is sent after gas cleaning unit dust separation to chimney, realizes flue The qualified discharge of exhaust gas.The waste heat recycled in the waste gas residual heat recovery unit is sent in ammonia steaming device, is generated to coke-oven plant Remained ammonia carries out ammonia still process processing, provides necessary ammonia for the denitration reduction reaction in low-temperature SCR desulphurization denitration unit.
Chinese patent 201810438291.0 discloses a kind of low-sulfur flue gas desulfurization and denitrification device.The device includes adsorption tower And vibrating screen, adsorption tower are successively arranged the firstth area, the secondth area and third area along flue gas circulating direction, the firstth area is equipped with flue gas air inlet Mouthful and positioned at smoke air inlet ammonia-spraying grid, third area is equipped with the gas outlet of flue gas, the active carbon flowed is equipped in the secondth area Layer, active carbon layer are flowed into from the top entry of adsorption tower, outlet at bottom outflow;The connection of the outlet at bottom of vibrating screen and adsorption tower, And it is connected by the top entry of conveying mechanism and adsorption tower.
Chinese patent CN201611269710.X discloses a kind of sintering flue gas ammonia charcoal combined desulfurization and denitration method, sintering Flue gas is after the desulfurization of absorbing liquid containing ammonia again through activated carbon adsorption;Carbonaceous raw material, the gold that the active carbon is 2:1 ~ 5:1 by mass ratio Belong to oxide source to roast to obtain in 850 ~ 1100 DEG C of countrysidies;The carbonaceous raw material is semicoke, or is the mixed of coal and biomass Close material.In the present invention, the active carbon as made from by ammonia and the method for the invention is combined, can effective desulphurization denitration, also Help reduce secondary pollution, reduction technique.
Document above is active carbon (coke) simultaneous SO_2 and NO removal, but can not all be detached from ammonia as this step of reducing agent denitration Suddenly.Since pelletizing flue flow field is uneven, temperature field is uneven, catalyst failure degree is uneven, the volume fraction of escape ammonia is difficult low In design discipline.Escape ammonia is exceeded to will cause secondary pollution, and corrosion pipeline material, and there is danger in the use process of ammonia Property, it is very important to the body harm of people.
In view of the above problems, not using ammonia, simultaneously the invention proposes the technology of molecular sieve adsorption simultaneous SO_2 and NO removal Adsorb the SO in pelletizing flue gas2And NOx, and be worth with certain recycling.
Summary of the invention
The technical problem to be solved by the present invention is to during existing steel plant's pelletizing smoke gas treatment, operating cost height is produced The technical issues of raw secondary pollution, a kind of method of pelletizing flue gas low-temperature desulphurization denitration is provided, which has process Short, low equipment investment, regeneration is simple, and low energy consumption, advantage without secondary pollution.
In order to solve the above technical problems, a kind of method that the present invention uses pelletizing flue gas low-temperature desulphurization denitration, including it is following Step:
A) the pelletizing flue gas of pelletizing flue is drawn sulfur compound and nitrogen oxides, is denoted as material flow A, the temperature of the material flow A It is 120 ~ 320 DEG C;
B) material flow A enters the denitrating tower comprising denitrating catalyst, after catalysis reduction, forms flow B;
C) flow B enters cooling tower, after supercooling, forms flow C, the temperature of the flow C is 30 ~ 100 DEG C, spray liquid Into waste water treatment system or salt extraction system;
D) flow C enters the adsorption tower comprising crystallite adsorbent, after adsorbing sulfide and nitrogen oxides, forms logistics D;
E) logistics D enters smoke stack emission;
F) adsorption tower after adsorbing sulfide and nitrogen oxides saturation in step d), with 100 ~ 10000m3The material flow A or heat of/h Air regenesis, regenerated flue gas form logistics E, wherein the temperature of the logistics E is 120 ~ 350 DEG C;
G) logistics E enters the oxidizing tower comprising oxidation catalyst, after catalysis oxidation, forms logistics F;
H) logistics F enters step the cooling tower in c);Spray liquid enters waste water treatment system or salt extraction system.
In the above-mentioned technical solutions, preferred technical solution is that the temperature of the material flow A is 140 ~ 280 DEG C;Nitrogen oxidation Object content is 100 ~ 1000mg/m3, sulfide content is 30 ~ 3000 mg/m3
In the above-mentioned technical solutions, preferred technical solution is that the denitrating catalyst includes being selected from SSZ-13 molecule Sieve, TS-1, Ti-MWW, Ti-MOR, ZSM type molecular sieve, modenite, beta molecular sieve, SAPO type molecular sieve, MCM-22, MCM- 49, MCM-56, ZSM-5/ modenite, ZSM-5/ β zeolite, ZSM-5/Y, MCM-22/ modenite, ZSM-5/Magadiite, ZSM-5/ β zeolite/modenite, ZSM-5/ β zeolite/at least one of Y zeolite or ZSM-5/Y zeolite/modenite.
In the above-mentioned technical solutions, preferred technical solution is that also containing in the denitrating catalyst includes element week At least one of Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race's element element in phase table.
In above-mentioned technical proposal, preferred technical solution is UTILIZATION OF VESIDUAL HEAT IN to be carried out before the step c), using steam Pelletizing, the vapor (steam) temperature of production are 140 ~ 180 DEG C;The flue gas that waste heat pelletizing comes out enters back into heat exchanger, and the heat exchanger is Shell and tube or finned heat exchanger;Cooling tower in the step c) is spray column or heat exchanger types;The temperature of logistics D Degree is 30 ~ 100 DEG C.
In above-mentioned technical proposal, preferred technical solution is that the temperature of the logistics D is 30 ~ 100 DEG C;Nitrogen oxides Content is 1 ~ 200mg/m3, sulfide content is 0.1 ~ 100 mg/m3
In above-mentioned technical proposal, preferred technical solution is that the logistics D and material flow A exchange heat after heating up, temperature 80 ~ 200 DEG C, then it is discharged into chimney.
In above-mentioned technical proposal, preferred technical solution is, the quantity of adsorption tower is at least more than two, adsorbent bed operation Temperature is 30 ~ 100 DEG C, and operating pressure is 0.1 ~ 20KPa.
The quantity of adsorption tower at least more than three, adsorbent bed operation temperature be 30 ~ 100 DEG C, operating pressure be 0.1 ~ 20KPa。
In above-mentioned technical proposal, preferred technical solution is that the temperature of the material flow A is 200 ~ 300 DEG C;Nitrogen oxides Content is 100-1000mg/m3, sulfide content is 40 ~ 3000 mg/m3
In the above-mentioned technical solutions, preferred technical solution is that in step c), adsorbent bed operation temperature is 30 ~ 80 DEG C, behaviour Making pressure gauge pressure is 0.5 ~ 5Kpa.
In the above-mentioned technical solutions, preferred technical solution is that it includes X-type molecular sieve, Y that the crystallite adsorbent, which is selected from, Type molecular sieve, A type molecular sieve, SSZ-13 molecular sieve, TS-1, Ti-MWW, Ti-MOR, ZSM type molecular sieve, modenite, β type point Sub- sieve, SAPO type molecular sieve, MCM-22, MCM-49, MCM-56, ZSM-5/ modenite, ZSM-5/ β zeolite, ZSM-5/Y, MCM-22/ modenite, ZSM-5/Magadiite, ZSM-5/ β zeolite/modenite, ZSM-5/ β zeolite/Y zeolite or ZSM- At least one of 5/Y zeolite/modenite.
In the above-mentioned technical solutions, preferred technical solution is that also containing in the crystallite adsorbent includes element week At least one of Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race's element element in phase table.
In the above-mentioned technical solutions, preferred technical solution is that containing in the oxidation catalyst includes period of element At least one of Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race's element element in table.
In the above-mentioned technical solutions, preferred technical solution is that the lye is sodium hydroxide solution, ammonium hydroxide, residue At least one of ammonium hydroxide, sodium carbonate liquor, calcium hydroxide solution.
In the above-mentioned technical solutions, preferred technical solution, it includes SSZ-13, TS- that the adsorbent of molecular sieve, which is selected from, 1, Ti-MWW, Ti-MOR, ZSM type molecular sieve, modenite, beta molecular sieve, SAPO type molecular sieve, MCM-22, ZSM-5/ mercerising Zeolite, ZSM-5/ β zeolite, ZSM-5/Y, MCM-22/ modenite, ZSM-5/ β zeolite/modenite, ZSM-5/ β zeolite/Y boiling At least one of stone or ZSM-5/Y zeolite/modenite.
In the above-mentioned technical solutions, the silica alumina ratio of preferred technical solution, the molecular sieve is greater than 2.
In the above-mentioned technical solutions, preferred technical solution, the IIth element A is selected from magnesium and calcium in the periodic table of elements At least one of;Ith B race element is selected from least one of copper, silver;IIIth B race element in lanthanum, cerium, yttrium at least It is a kind of.
In the above-mentioned technical solutions, preferred technical solution, ZSM type molecular sieve is selected from packet in the adsorbent of molecular sieve At least one of ZSM-5, ZSM-23, ZSM-11, ZSM-48 are included, wherein the silica alumina ratio of the molecular sieve is greater than 20.
In the above-mentioned technical solutions, preferred technical solution, adsorbent bed operation temperature be 30 ~ 50 DEG C, operating pressure be 1 ~ 3Kpa, gauge pressure.
In the above-mentioned technical solutions, preferred technical solution is passed through air, ozone, double water oxygen water in regeneration gas oxidizing tower At least one of.
In the above-mentioned technical solutions, preferred technical solution, after the adsorbent of molecular sieve adsorption saturation, heat first Water rinses, then with 100-300 DEG C of nitrogen regeneration.
By adopting the above technical scheme, using crystallite adsorbent desulphurization denitration, crystallite adsorbent to gas cleaning handle just like Lower advantage: the sulfur dioxide and nitrogen oxides in flue gas can be effectively adsorbed, discharge standard is made up to;High temperature resistant, structure are steady It is fixed, iterative regenerable;It is high to adsorb precision, other than adsorb sulfur dioxide, can also dedusting simultaneously remove the harmful substances such as dioxin, Make up to discharge standard;Crystallite adsorbent long service life, does not generate dangerous waste.By setting up adsorption tower in exhanst gas outlet, benefit Sulfur dioxide, the nitrogen oxides in flue gas are adsorbed with System of Silica/Aluminum Microparticle hydrochlorate crystallite adsorbent, System of Silica/Aluminum Microparticle in adsorption tower After hydrochlorate crystallite adsorbent adsorption saturation, crystallite adsorbent is regenerated by high-temperature flue gas, the nitrogen oxides and sulphur of desorption Compound enters oxidizing tower, is oxidized to sulfur trioxide and nitrogen dioxide, and regenerated flue gas is absorbed with water spray, after effluent part neutralizes, It is discharged into biochemical system or goes to salt extraction workshop, tail gas enters flue gas spray column circulation.Entire treatment process process is short, equipment investment It saves, regenerative operation is simple and reliable, and low energy consumption, flue gas emission nitrogen oxides≤50mg/m3, sulfur dioxide≤30mg/m3, dust content Less than 5 mg/m3, achieve preferable technical effect.
Detailed description of the invention
Fig. 1 is the flow diagram of pelletizing flue gas desulfurization and denitration method of the invention.
1 is pelletizing flue gas in Fig. 1, and 2 be denitrating tower, and 3 be cooling tower, and 4 be adsorption tower, and 5 be blower, and 6 be oxidizing tower, and 7 are Sedimentation basin, 8 be biochemistry pool, and 9 be chimney.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
[embodiment 1]
The flue gas of 160 240 DEG C of ten thousand steres, amount of nitrogen oxides 500mg/m3, sulfide content is 200 mg/m3, flue gas Into denitrating tower, at 240 DEG C, under ZSM-5 molecular sieve catalyst action, nitrogen oxides is reduced into nitrogen, the flue gas after reaction Into cooling tower, by spraying cooling to 50 DEG C, shower water after effluent part neutralizes, removes biochemical system by being recycled;Drop After flue gas after temperature passes through defogging equipment, into adsorption tower;Using 3 200m3Adsorption tower, two open standby, each adsorption tower Interior filling 120m3Micro crystal material amounts to 360 m3Micro crystal material modenite;Adsorption tower specification is 4.8 meters of diameter, 12.0 meters high; After flue gas removes sulfide and nitrogen oxides, into smoke stack emission, nitrogen oxides in effluent content is 50mg/m3, sulfide contains Amount is 20 mg/m3.Desulphurization and denitration, dedusting crystallite adsorbent are loaded in adsorption tower, automatically switch circular regeneration after adsorption saturation; Automatically switch within every 7 days a tower regeneration, the adsorption tower 3000m of saturation3The hot fume of/h is regenerated, the nitrogen oxides of desorption Enter oxidizing tower with sulfide, is oxidized to sulfur trioxide and nitrogen dioxide;It into cooling tower, is absorbed with water spray, effluent part After neutralization, being discharged into produces salt extraction workshop salt extraction.
[embodiment 2]
Specific embodiment device process as shown in Fig. 1, the flue gas of 150 260 DEG C of ten thousand steres, amount of nitrogen oxides are 400mg/m3, sulfide content is 100 mg/m3, flue gas enters denitrating tower, at 240 DEG C, in ZSM-5 molecular sieve catalyst action Under, nitrogen oxides is reduced into nitrogen, and the flue gas after reaction enters cooling tower, and to 40 DEG C, shower water is made spraying cooling by circulation After being neutralized with, effluent part, biochemical system is removed;After flue gas after cooling passes through defogging equipment, into adsorption tower;Using 3 200m3Adsorption tower, two open one standby, and 120m is loaded in each adsorption tower3Micro crystal material amounts to 360 m3Micro crystal material ZSM-5 points Son sieve;Adsorption tower specification is 4.8 meters of diameter, 12.0 meters high;After flue gas removes sulfide and nitrogen oxides, into from heat exchanger, After hot fume heat exchange, reach 100 DEG C or more, into smoke stack emission, nitrogen oxides in effluent content is 50mg/m3, sulfide contains Amount is 20 mg/m3.Desulphurization and denitration, dedusting crystallite adsorbent are loaded in adsorption tower, automatically switch circular regeneration after adsorption saturation; Automatically switch within every 7 days a tower regeneration, the adsorption tower 3000m of saturation3The hot fume of/h is regenerated, the nitrogen oxides of desorption Enter oxidizing tower with sulfide, is oxidized to sulfur trioxide and nitrogen dioxide;After mixed gas enters cooling tower cooling, effluent part After neutralization, it is discharged into biochemical system or goes to salt extraction workshop.
[embodiment 3]
Specific embodiment device process as shown in Fig. 1, the flue gas of 140 300 DEG C of ten thousand steres, amount of nitrogen oxides are 450mg/m3, sulfide content is 200 mg/m3, flue gas enters denitrating tower, at 300 DEG C, urges in the ZSM-5 molecular sieve of copper load Under agent effect, nitrogen oxides is reduced into nitrogen, and the flue gas after reaction enters waste heat pelletizing, generates 160 DEG C of steam, flue gas again into Enter from heat exchanger, and enter the cold flue gas heat exchange of chimney, temperature is reduced to 110 DEG C or so;110 DEG C of flue gas passes through flue-gas temperature It is reduced to 110 DEG C or so;110 DEG C of flue gas is by spraying cooling to 50 DEG C, and by being recycled, effluent part neutralizes shower water Afterwards, biochemical system is removed;After flue gas after cooling passes through defogging equipment, into adsorption tower;Using 3 200m3Adsorption tower, two open One is standby, and 120m is loaded in each adsorption tower3Micro crystal material amounts to 360 m3Micro crystal material ZSM-5 molecular sieve;Adsorption tower specification is It is 4.8 meters of diameter, 12.0 meters high;After flue gas removes sulfide and nitrogen oxides, into from after heat exchanger and hot fume heat exchange, reach To 110 DEG C or more, into smoke stack emission, nitrogen oxides in effluent content is 40mg/m3, sulfide content is 10 mg/m3.Adsorption tower Interior filling desulphurization and denitration, dedusting crystallite adsorbent after adsorption saturation, automatically switch circular regeneration with high-temperature flue gas;Every 7 days certainly One tower regeneration of dynamic switching, the adsorption tower 3000m of saturation3240 DEG C of flue gases of/h are regenerated, the nitrogen oxides and sulphur of desorption Compound enters the oxidizing tower containing vanadium series catalyst, is oxidized to sulfur trioxide and nitrogen dioxide;After mixed gas cooling, sprayed with water Leaching absorbs, and after effluent part neutralizes, is discharged into biochemical system or goes to salt extraction workshop, tail gas enters flue gas spray column.
[embodiment 4]
Specific embodiment device process as shown in Fig. 1, the flue gas of 200 180 DEG C of ten thousand steres, amount of nitrogen oxides are 1000mg/m3, sulfide content is 500 mg/m3, flue gas enters denitrating tower, at 180 DEG C, under mordenite catalyst effect, Nitrogen oxides is reduced into nitrogen, and the flue gas after reaction enters waste heat pelletizing, generates 10 tons of 165 DEG C of steam, flue-gas temperature per hour It is reduced to 120 DEG C or so;120 DEG C of flue gas is by spraying cooling to 40 DEG C, and by being recycled, effluent part neutralizes shower water Afterwards, the salt extraction system that going produces;After flue gas after cooling passes through defogging equipment, into adsorption tower;Using 4 200m3Absorption Tower, three open standby, a filling 120m in each adsorption tower3Micro crystal material amounts to 360 m3Micro crystal material SSZ-13 molecular sieve;Absorption Tower specification is 4.8 meters of diameter, 12.0 meters high;After flue gas removes sulfide and nitrogen oxides, changed into from heat exchanger and hot fume After heat, reach 100 DEG C or more, into smoke stack emission, nitrogen oxides in effluent content is 50mg/m3, sulfide content is 20 mg/ m3.Desulphurization and denitration, dedusting crystallite adsorbent are loaded in adsorption tower, automatically switch circular regeneration after adsorption saturation;Every 7 days automatic Switch a tower regeneration, the adsorption tower 2000m of saturation3The hot fume of/h is regenerated, the nitrogen oxides and sulfide of desorption Into the oxidizing tower containing Cu-series catalyst, it is oxidized to sulfur trioxide and nitrogen dioxide;After mixed gas cooling, inhaled with water spray It receives, after effluent part neutralizes, being discharged into produces salt extraction workshop, and tail gas enters flue gas spray column.
[embodiment 5]
Specific embodiment device process as shown in Figure 1, the flue gas of 200 180 DEG C of ten thousand stere rice, amount of nitrogen oxides are 1000mg/m3, sulfide content is 500 mg/m3, flue gas enters denitrating tower, at 180 DEG C, in the ZSM-5 molecular sieve of copper zinc load Under catalyst action, nitrogen oxides is reduced into nitrogen, and the flue gas after reaction enters waste heat pelletizing, generates 150 DEG C of steam, flue gas drop Temperature is to 170 DEG C, and then flue gas enters from heat exchanger, and enters the cold flue gas heat exchange of chimney, and temperature is reduced to 130 DEG C or so;Cigarette Gas enters spray column, and by spraying cooling to 40 DEG C, shower water is by being recycled, and after effluent part neutralizes, what going produced is mentioned Salt system;After flue gas after cooling passes through defogging equipment, into adsorption tower;Using 4 200m3Adsorption tower, three open it is one standby, often 120m is loaded in a adsorption tower3Y zeolite crystallite material, amount to 360 m3Micro crystal material copper ZSM-5 molecular sieve;Adsorption tower specification It is 4.8 meters of diameter, it is 12.0 meters high;After flue gas removes sulfide and nitrogen oxides, into after exchanging heat from heat exchanger and hot fume, Reach 100 DEG C or more, into smoke stack emission, nitrogen oxides in effluent content is 40mg/m3, sulfide content is 10 mg/m3.Absorption Desulphurization and denitration, dedusting crystallite adsorbent are loaded in tower, automatically switch circular regeneration after adsorption saturation;Automatically switch one within every 7 days Tower regeneration, the adsorption tower 3000m of saturation3180 DEG C of flue gases of/h are regenerated, and the nitrogen oxides and sulfide of desorption, which enter, to be contained There is the oxidizing tower of Cu-series catalyst, is oxidized to sulfur trioxide and nitrogen dioxide;After mixed gas cooling, absorbed with water spray, portion After dividing waste water to neutralize, being discharged into produces salt extraction workshop, and tail gas enters flue gas spray column.
[embodiment 6]
Specific embodiment device process as shown in Figure 1, the flue gas of 260 DEG C of 2,000,000 sides rice, amount of nitrogen oxides are 400mg/m3, sulfide content is 100 mg/m3, flue gas enters denitrating tower, at 250 DEG C or so, in rare earth mordenite catalyst Under effect, nitrogen oxides is reduced into nitrogen, and the flue gas after reaction enters waste heat pelletizing, generates 170 DEG C of steam, and flue gas cool-down arrives 175 DEG C, then flue gas enters from heat exchanger, and enters the cold flue gas heat exchange of chimney, and temperature is reduced to 130 DEG C or so;Into spray Leaching cools to 50 DEG C, and shower water after effluent part neutralizes, removes biochemical system by being recycled;Flue gas after cooling is by removing After mist equipment, into adsorption tower;Using 3 200m3Adsorption tower, two open one standby, and 120m is loaded in each adsorption tower3Crystallite material Material amounts to 360 m3Micro crystal material, micro crystal material include the ZSM-5 molecular sieve of lanthanum and zinc modification;Adsorption tower specification is diameter 4.8 Rice is 12.0 meters high;After flue gas removes sulfide and nitrogen oxides, into smoke stack emission, nitrogen oxides in effluent content is 30mg/ m3, sulfide content 5mg/m3.Desulphurization and denitration, dedusting crystallite adsorbent are loaded in adsorption tower, are automatically switched after adsorption saturation Circular regeneration;Automatically switch within every 7 days a tower regeneration, the adsorption tower 4000m of saturation3180 DEG C of the flue gas of/h is regenerated, The nitrogen oxides and sulfide of desorption enter oxidizing tower, are oxidized to sulfur trioxide and nitrogen dioxide at 250 DEG C;Mixed gas cooling Afterwards, it is absorbed with water spray, after effluent part neutralizes, is discharged into biochemical system or goes to salt extraction workshop, tail gas enters flue gas spray column.
[embodiment 7]
Specific embodiment device process as shown in Fig. 1, the flue gas of 180 240 DEG C of ten thousand stere rice, amount of nitrogen oxides For 400mg/m3, sulfide content is 100 mg/m3, flue gas enters denitrating tower, at 240 DEG C, makees in rare-earth Y molecular sieve catalyst Under, nitrogen oxides is reduced into nitrogen, and the flue gas after reaction enters afterheat steam pelletizing, generates 145 DEG C of steam, and flue gas cool-down arrives 160 DEG C, by spraying cooling to 40 DEG C, shower water after effluent part neutralizes, removes biochemical system by being recycled;After cooling Flue gas by after defogging equipment, into adsorption tower;Using 3 200m3Adsorption tower, two open one standby, and each adsorption tower is built-in Fill out 120m3Micro crystal material amounts to 360 m3Micro crystal material ZSM-5 molecular sieve;Adsorption tower specification is 4.8 meters of diameter, 12.0 meters high; After flue gas removes sulfide and nitrogen oxides, into from after heat exchanger and hot fume heat exchange, reaches 100 DEG C or more, arranged into chimney It puts, nitrogen oxides in effluent content is 50mg/m3, sulfide content is 20 mg/m3.Desulphurization and denitration, dedusting are loaded in adsorption tower Crystallite adsorbent automatically switches circular regeneration after adsorption saturation;Automatically switch within every 7 days a tower regeneration, the adsorption tower of saturation is used 3000m3The hot fume of/h is regenerated, and the nitrogen oxides and sulfide of desorption enter oxidizing tower, is oxidized to sulfur trioxide and two Nitrogen oxide;It after mixed gas cooling, is absorbed with water spray, after effluent part neutralizes, is discharged into biochemical system or goes to salt extraction workshop, Tail gas enters flue gas spray column.
[embodiment 8]
Specific embodiment device process as shown in Fig. 1, the flue gas of 180 210 DEG C of ten thousand stere rice, amount of nitrogen oxides For 400mg/m3, sulfide content is 100 mg/m3, flue gas enters denitrating tower, at 210 DEG C, at the ZSM-5 of copper and tungsten load points Under sub- sieve catalyst effect, nitrogen oxides is reduced into nitrogen, and the flue gas after reaction enters waste heat pelletizing, generates 160 DEG C of steam, cigarette Gas cools to 185 DEG C, and then flue gas enters from heat exchanger, and enters the cold flue gas heat exchange of chimney, and temperature is reduced to 130 DEG C of left sides It is right;By spraying cooling to 50 DEG C, shower water after effluent part neutralizes, goes to the salt extraction workshop of coking by being recycled;Cooling After flue gas afterwards passes through defogging equipment, into adsorption tower;Using 4 200m3Adsorption tower, three open it is one standby, in each adsorption tower Load 150m3Micro crystal material amounts to 450 m3Micro crystal material containing modenite and ZSM-5 molecular sieve;Adsorption tower specification is straight It is 4.8 meters of diameter, 12.0 meters high;After flue gas removes sulfide and nitrogen oxides, into from after heat exchanger and hot fume heat exchange, reach 100 DEG C or more, into smoke stack emission, nitrogen oxides in effluent content is 50mg/m3, sulfide content is 20 mg/m3.In adsorption tower Desulphurization and denitration, dedusting crystallite adsorbent are loaded, automatically switches circular regeneration after adsorption saturation;One tower of automatic switchover in every 7 days is again It is raw, the adsorption tower 4000m of saturation3240 DEG C of the flue gas of/h is regenerated, and the nitrogen oxides and sulfide of desorption enter oxidation Tower is oxidized to sulfur trioxide and nitrogen dioxide;It after mixed gas cooling, is absorbed with water spray, after effluent part neutralizes, is discharged into life Change system goes to salt extraction workshop, and tail gas enters flue gas spray column.

Claims (10)

1. a kind of method of pelletizing flue gas low-temperature desulphurization denitration, comprising the following steps:
The pelletizing flue gas of sulfur compound and nitrogen oxides that pelletizing flue is drawn, is denoted as material flow A, the temperature of the material flow A is 120~320℃;
Material flow A enters the denitrating tower comprising denitrating catalyst, after catalysis reduction, forms flow B;
Flow B enters cooling tower, after supercooling, forms flow C, and the temperature of the flow C is 30 ~ 100 DEG C, spray liquid into Enter waste water treatment system or salt extraction system;
Flow C enters the adsorption tower comprising crystallite adsorbent, after adsorbing sulfide and nitrogen oxides, forms logistics D;
Logistics D enters smoke stack emission;
Adsorption tower after adsorbing sulfide and nitrogen oxides saturation in step d), with 100 ~ 10000m3The material flow A or heat of/h is empty Gas regeneration, regenerated flue gas form logistics E, wherein the temperature of the logistics E is 120 ~ 350 DEG C;
Logistics E enters the oxidizing tower comprising oxidation catalyst, after catalysis oxidation, forms logistics F;
Logistics F enters step the cooling tower in c);Spray liquid enters waste water treatment system or salt extraction system.
2. the method for pelletizing flue gas desulfurization and denitrification according to claim 1, it is characterised in that the temperature of the material flow A is 140~280℃;Amount of nitrogen oxides is 100 ~ 1000mg/m3, sulfide content is 30 ~ 3000 mg/m3
3. the method for pelletizing flue gas low-temperature desulphurization denitration according to claim 1, it is characterised in that the denitration catalyst Agent includes being selected from SSZ-13 molecular sieve, TS-1, Ti-MWW, Ti-MOR, ZSM type molecular sieve, modenite, beta molecular sieve, SAPO Type molecular sieve, MCM-22, MCM-49, MCM-56, ZSM-5/ modenite, ZSM-5/ β zeolite, ZSM-5/Y, MCM-22/ mercerising Zeolite, ZSM-5/Magadiite, ZSM-5/ β zeolite/modenite, ZSM-5/ β zeolite/Y zeolite or ZSM-5/Y zeolite/mercerising At least one of zeolite.
4. according to the method for the pelletizing flue gas low-temperature desulphurization denitration that claim 3 is stated, it is characterised in that the denitrating catalyst In also containing including in the periodic table of elements in the Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race's element At least one element.
5. the method for pelletizing flue gas desulfurization and denitrification according to claim 1, it is characterised in that cold in the step b) But tower is spray column or heat exchanger types, and spray liquid is cooling using cold water;The temperature of flow C is 30 ~ 100 DEG C;The object The temperature for flowing D is 30 ~ 100 DEG C;Amount of nitrogen oxides is 1 ~ 200mg/m3, sulfide content is 0.1 ~ 100 mg/m3
6. the method for pelletizing flue gas low-temperature desulphurization denitration according to claim 1, it is characterised in that the liter of the logistics D Warm mode is using heated by gas heating mode or logistics D and material flow A heat exchange heating mode, and after heating up, temperature is logistics D 80~200℃;In step d), the quantity of adsorption tower is at least more than two, and adsorbent bed operation temperature is 30 ~ 100 DEG C, operating pressure For 0.1 ~ 20KPa.
7. the method for pelletizing flue gas low-temperature desulphurization denitration according to claim 1, it is characterised in that described in step e) It includes X-type molecular sieve, Y type molecular sieve, A type molecular sieve, SSZ-13 molecular sieve, TS-1, Ti-MWW, Ti- that crystallite adsorbent, which is selected from, MOR, ZSM type molecular sieve, modenite, beta molecular sieve, SAPO type molecular sieve, MCM-22, MCM-49, MCM-56, ZSM-5/ Geolyte, ZSM-5/ β zeolite, ZSM-5/Y, MCM-22/ modenite, ZSM-5/Magadiite, ZSM-5/ β zeolite/mercerising boiling Stone, ZSM-5/ β zeolite/at least one of Y zeolite or ZSM-5/Y zeolite/modenite.
8. the method for pelletizing flue gas low-temperature desulphurization denitration according to claim 7, it is characterised in that the crystallite absorption Also containing including the Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race's element in the periodic table of elements in agent At least one of element.
9. the method for pelletizing flue gas low-temperature desulphurization denitration according to claim 1, it is characterised in that the oxidation catalysis Containing including in the Ith A, II A, V A, I B, II B, III B, IV B, V B, VI B, VII B or the VIIIth race's element in the periodic table of elements in agent At least one element.
10. according to the method for the pelletizing flue gas low-temperature desulphurization denitration that claim 7 is stated, it is characterised in that alkali described in step h) Liquid is at least one of sodium hydroxide solution, ammonium hydroxide, remained ammonia, sodium carbonate liquor, calcium hydroxide solution.
CN201811493988.4A 2018-12-07 2018-12-07 Pelletizing flue gas low-temperature desulfurization denitration method Pending CN109513341A (en)

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CN101816886A (en) * 2010-04-29 2010-09-01 昆明理工大学 Method for simultaneously desulfurating, denitrating and decarbonizing coal-fired flue gas
KR20110001738A (en) * 2009-06-30 2011-01-06 한국전력공사 System for separrating acid gas in the power plant equipment
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CN103877856A (en) * 2014-03-27 2014-06-25 中冶焦耐工程技术有限公司 Coke oven flue gas waste heat utilization and purification method
CN104492424A (en) * 2014-11-19 2015-04-08 浙江大学 Method for producing sulfuric acid by catalytic oxidation of sulfur dioxide in flue gas via ozone coupling with manganese dioxide/aluminum oxide

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20110001738A (en) * 2009-06-30 2011-01-06 한국전력공사 System for separrating acid gas in the power plant equipment
CN101816886A (en) * 2010-04-29 2010-09-01 昆明理工大学 Method for simultaneously desulfurating, denitrating and decarbonizing coal-fired flue gas
CN103785290A (en) * 2014-03-03 2014-05-14 中钢集团天澄环保科技股份有限公司 Sintering and pelletizing flue gas desulfurization and denitrification coordinating management system and process
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