CN108067091A - A kind of ultra-clean discharge flue gas desulfurization technique - Google Patents
A kind of ultra-clean discharge flue gas desulfurization technique Download PDFInfo
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- CN108067091A CN108067091A CN201611002677.4A CN201611002677A CN108067091A CN 108067091 A CN108067091 A CN 108067091A CN 201611002677 A CN201611002677 A CN 201611002677A CN 108067091 A CN108067091 A CN 108067091A
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- flue gas
- desulfurization
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- ammonium sulfate
- absorbing liquid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
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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
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
- B01D53/502—Sulfur 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
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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
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/24—Sulfates of ammonium
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- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
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Abstract
The invention discloses SO in a kind of removing flue gas2The ultra-clean discharge technology of producing ammonium sulfate byproduct chemical fertilizer belongs to field of environment protection air contaminant treatment desulfurization removing nitric technology.It uses ammonia as desulfurizing agent, and high-temperature flue gas enters absorption tower absorber portion after absorption tower enriching section is cooled to 50~70 DEG C, absorbing liquid and the SO in flue gas in absorber portion2Sweetening process is completed in reaction, absorbing liquid after reaction flow to absorption cycle slot certainly, absorbing liquid and ammonia reaction generation ammonium sulfite in absorption cycle slot, part ammonium sulfite returns to absorber portion as absorbing liquid, and part ammonium sulfite is oxidized to ammonium sulfate, and ammonium sulfate is sent to enriching section and flue gas heat exchange, ammonia sulfate crystal is precipitated, suspension containing ammonia sulfate crystal becomes finished product by eddy flow, filtering, solid through dry, and liquid returns again to enriching section.Flue gas after desulfurization deep purifying section of the flue gas into absorption tower top after chevron mist eliminator after desulfurization is handled, and reaches ultra-clean discharge standard.
Description
Technical field：
The present invention relates to field of environment protection air contaminant treatment desulfurization removing nitric technology more particularly to a kind of ultra-clean discharges
Flue gas desulfurization technique.
Background technology：
Existing similar technique and existing deficiency are as follows：
The ultra-clean draining technology of current wet ammonia process desulfurizing mainly have the ammonia process of desulfurization+wet type electrostatic precipitator method, the ammonia process of desulfurization+
Bundled tube demister method, the ammonia process of desulfurization+multistage WATER-WASHING METHOD.
1st, the ammonia process of desulfurization+wet type electrostatic precipitator method
Using ammonium hydroxide as desulfurizing agent, big cycle volume makes ammonia and ammonium sulfite solution and the SO in flue gas in desulfurizing tower2
Reaction removing SO2, by-product ammonium sulfate and ammonium sulfite are generated, in desulfurization tower bottom using the method for air aeration by sub- sour ammonium
Ammonium sulfate is oxidized to, ammonia sulfate crystal packaging and storage is produced after eddy flow, centrifugation, drying after ammonium sulfate discharge, completes
Desulfurization and the removal process of ammonium sulfate product.Flue gas after desulfurization is by washing and chevron mist eliminator, using wet type electricity demisting
Device is discharged into air after removing dust and drop in flue gas after desulfurization.
There are following defects for this method：
1) ammonia process of desulfurization+wet type electrostatic precipitator method is to increase a set of wet type electrostatic precipitator device, equipment newly after the ammonia process of desulfurization
Investment is big, and electric quantity consumption is big in wet type electrostatic precipitator use, and operating cost is high.
2) wet type electrostatic precipitator is increased, desulfurizer flow increases, and floor space increases, and desulphurization system pressure drop increases, behaviour
Make expense increase.
2nd, the ammonia process of desulfurization+bundled tube demister method
Using ammonium hydroxide as desulfurizing agent, big cycle volume makes ammonia and ammonium sulfite solution and the SO in flue gas in desulfurizing tower2
Reaction removing SO2, by-product ammonium sulfate and ammonium sulfite are generated, in desulfurization tower bottom using the method for air aeration by sub- sour ammonium
Ammonium sulfate is oxidized to, ammonia sulfate crystal packaging and storage is produced after eddy flow, centrifugation, drying after ammonium sulfate discharge, completes
Desulfurization and the removal process of ammonium sulfate product.Flue gas after desulfurization is discharged into air after washing and bundled tube demister.
There are following defects for this method：
1) ammonia process of desulfurization+bundled tube demister method is to be changed to the chevron mist eliminator used in former ammonia desulfurizing process
Bundled tube demister, bundled tube demister pressure drop is big, and system operatio is costly.
2) bundled tube demister operation principle be flue gas after desulfurization by bundled tube demister when, in bundled tube demister
Guide vane changes gas flow direction, high tangential velocity is formed, so as to separate the dust and drop in flue gas after desulfurization.
Operation principle requirement gas flow operating mode stabilization can ensure preferable removal efficiency, so in actual motion, operation difficulty is big,
Neat stress quality it is difficult to ensure that.
3rd, the ammonia process of desulfurization+multistage WATER-WASHING METHOD
Using ammonium hydroxide as desulfurizing agent, big cycle volume makes ammonia and ammonium sulfite solution and the SO in flue gas in desulfurizing tower2
Reaction removing SO2, by-product ammonium sulfate and ammonium sulfite are generated, in desulfurization tower bottom using the method for air aeration by sub- sour ammonium
Ammonium sulfate is oxidized to, ammonia sulfate crystal packaging and storage is produced after eddy flow, centrifugation, drying after ammonium sulfate discharge, completes
Desulfurization and the removal process of ammonium sulfate product.Flue gas after desulfurization is discharged into air after multistage washing and chevron mist eliminator.
There are following defects for this method：
1) ammonia process of desulfurization+multistage WATER-WASHING METHOD is to increase by one section of washing in former ammonia desulfurizing process for two sections and two sections or more
Water washing cycles layer, 3 meters or so of absorption tower tower height, and corresponding increase water washing cycles slot and washing must be increased by often increasing by one section of washing layer
Circulating pump, equipment cost increase are higher.
2) purpose of washing section is using flue gas after clear water washing desulphurization, makes dust remaining in flue gas after desulfurization and desulfurization
Agent liquid further reduces, but because the reason for gas is carried secretly, neat stress carries the desulfurization into washing section secretly when entering washing section
Agent amount of liquid is larger, causes desulfurization agent concentration in final washing section Xun Huan clear water higher, it is impossible to flue gas after good washing desulphurization,
Even if being washed by multistage, neat stress quality cannot be ensured well, more in addition because the reason for desulphurization system water balance
After Duan Shuixi, desulfurization agent concentration remains difficult to control in final stage washing section Xun Huan clear water.
The content of the invention：
For problems of the prior art, the present invention proposes a kind of flue gas desulfurization technique of ultra-clean discharge, with solution
Certainly prior art high energy consumption, the problem of investment is big, neat stress cannot reach minimum discharge, this technical flow design is reasonable, energy consumption
Low, neat stress reaches ultra-clean discharge standard.
The present invention adopts the following technical scheme that realize：
A kind of flue gas desulfurization technique of ultra-clean discharge, including the following steps：
1) prepared by ammonium hydroxide
2) desulphurization reaction
3) sulfite oxidation
4) ammonium sulfate concentrates
5) ammonium sulfate separation, purification, recycling
6) flue gas after desulfurization deep purifying
Ammonium hydroxide will configure in ammonium hydroxide batch tank in the above-mentioned technical solutions, and the concentration of ammonium hydroxide is 8~20%, has been configured
Ammonium hydroxide is by being pumped into absorption cycle slot.
Flue gas is evenly distributed in tower, flow velocity drops to below 3m/s from the enriching section entrance positioned at absorption tower lower part.Cigarette
From bottom to top, ammonium sulfate slurries spray gas from top to bottom, and liquid phase inversely comes into full contact with, the moisture evaporation in slurries, flue gas temperature
Degree reduces, and is reduced to flue gas saturation balance stabilization；Ammonium sulfate concentration of slurry increases, and reaches ammonium sulfate saturated concentration, ammonium sulfate exists
Crystallization inside tower is precipitated.
Flue gas after saturation enters absorber portion by a liter gas cap, is subject to the spray washing of absorbing liquid, and liquid phase is inversely abundant
Contact.During spray, the ammonia and ammonium sulfite absorbing and removing in sulfur dioxide absorbed liquid in flue gas, in flue gas
Pollutant is purified.Generation main chemical reactions are as follows：
2NH3+H2O+SO2=(NH4)2SO3 (1)
(NH4)2SO3+SO2+H2O=2NH4HSO3 (2)
It is continued up by the flue gas of absorber portion by chevron mist eliminator, removes the dust carried secretly in flue gas and absorbing liquid
Drop, flue gas complete sweetening process, become flue gas after desulfurization.Flue gas after desulfurization continues to enter flue gas after desulfurization depth along tower uplink
Spend clean-up stage.Flue gas after desulfurization deep purifying section is made of washing layer and mesh mist eliminator, and flue gas after desulfurization is advanced rashly by liter gas
Enter to wash layer, be washed using weak solution of the equilibrium concentration below 1%, remove the dust carried secretly after desulfurization sulfur in flue gas and
Absorbent droplet finally removes free water by tower top mesh mist eliminator and is discharged by chimney.Whole system pressure drop≤1.5kPa.
The ammonium bisulfite of absorber portion generation reacts generation ammonium sulfite, part in absorption cycle slot with the ammonium hydroxide of addition
Ammonium sulfite is back to absorber portion as absorbent；Part ammonium sulfite is aoxidized in absorption cycle slot by excessive oxidation air
Ammonium sulfate is formed, ammonium sulfate is admitted to enriching section by pump.Generation main chemical reactions are as follows：
2NH4HSO3+2NH3=2 (NH4)2SO3 (3)
(NH4)2SO3+1/2O2=(NH4)2SO4 (4)
Slurries in enriching section come into full contact with flue gas, and moisture evaporation therein enters flue gas, and concentration constantly raises, finally
Reach saturated solution (about 55 DEG C, 46%) at such a temperature, operation lasting afterwards causes ammonium sulfate crystallization to be precipitated, Zhi Daonong
In contracting section slurries during ammonium sulfate crystallization containing 5-15%, ammonium sulfate system production ammonium sulfate is emitted by excavationg pump.
Ammonium sulfate excavationg pump conveying slurries enter cyclone, and the ammonium sulfate slurries with crystallization continue to concentrate in cyclone
Reach 45% to solid content, the slurries of overflow return to enriching section stock tank.The ammonium sulfate slurries of solid content 45% by centrifuge into
One step thickening obtains the wet ammonium sulfate of moisture content≤5%.Wet ammonium sulfate enters drying machine through screw(-type) feeder, through overheat
Air-dry it is dry after, obtain the ammonium sulfate product of moisture content≤0.3%, most afterwards after automatic packaging machine is packed store or sell.
In absorption tower, process water is supplemented by being located at the mist eliminator flushing above washing layer.Wash the water of layer
By being pumped into absorber portion, the absorbing liquid of absorber portion enters enriching section also by pump, so that realizes water balance in absorption tower.
Ammonium hydroxide addition is controlled by absorber portion pH value.According to the exhaust gas volumn of the entrance on absorption tower, SO2Concentration, absorber portion
The parameters such as pH value determine specific ammonium hydroxide injection rate.
The present invention will play following good effect：
1) this technology desulfurization degree is high, desulfurization degree ＞ 96%, while has the effect of denitrogenation, and denitrification percent is up to more than 35%.
2) this technology operating cost is low, and a whole set of desulfurizer pressure drop is less than 1500Pa, less than other ultra-clean discharge desulfurization skills
Art.
3) neat stress discharge index reaches SO2Concentration is less than 35mg/Nm3, solid particulate matter concentration is less than 10mg/Nm3。
Description of the drawings：
Fig. 1 show a kind of flue gas desulfurization process figure of ultra-clean discharge of the present invention.
Specific embodiment：
Liquefied ammonia as absorbent, is changed into 8~20% ammonium hydroxide by this technology using ammonium hydroxide.
This technology absorption tower is divided into enriching section, absorber portion, demister, four part of flue gas after desulfurization deep purifying section.
The heat smoke that boiler comes is into absorption tower enriching section after electricity or bag-type dust, and ammonium sulfate slurries are from enriching section bottom
Concentration cycles slot pumped out with concentrated circulating pump, sprayed by spraying layer from enriching section top and under, and heat smoke counter current contacting,
Flue gas be cooled to 50-70 DEG C after into absorption tower absorber portion, moisture in ammonium sulfate slurries by high-temperature flue gas be concentrated by evaporation to
After saturation state, ammonia sulfate crystal is precipitated in concentration cycles slot, when solid content reaches 5-15% in ammonium sulfate slurries, by sulfuric acid
Ammonium slurry discharge pump is sent into cyclone separator and carries out separation of solid and liquid.
Flue gas after saturation enters absorber portion by the liter gas cap of absorber portion liquid header, and absorbing liquid is from absorption cycle slot
It is pumped out with absorbent recirculation pump, by absorbing spraying layer from absorber portion top spray and under, liquid phase inversely comes into full contact with, in flue gas
Sulfur dioxide absorbed liquid in ammonia and sulfurous acid ammonia absorbing and removing, the pollutant in flue gas be purified.Complete desulfurization work(
The absorbing liquid of energy flow to absorption cycle slot certainly after being collected by absorber portion liquid header.
It is continued up by the flue gas of absorber portion by chevron mist eliminator, removes the dust carried secretly in flue gas and absorbing liquid
Drop, flue gas complete sweetening process, become flue gas after desulfurization.
Flue gas after desulfurization continues to enter flue gas after desulfurization deep purifying section along tower uplink.Flue gas after desulfurization deep purifying section
It is made of washing layer and mesh mist eliminator, flue gas after desulfurization is emitted by washing the liter gas of layer liquid header into washing layer, water
It washes circulation fluid circulating pump is washed with water from water washing cycles slot and pump out, by washing spraying layer from washing layer top spray and under, gas-liquid
It is mutually inversely come into full contact in layer filler is washed, the dust and absorbent liquid concentration carried secretly in flue gas after desulfurization further drop
It is low.The water washing cycles liquid for completing water scrub function flow to water washing cycles slot certainly by washing after the collection of layer liquid header.By water
The flue gas after desulfurization after layer is washed finally to be discharged by tower top chimney after tower top mesh mist eliminator removes free water.Whole system pressure
Drop≤1.5kPa.
Generation to be reacted with the ammonium hydroxide of addition sub- from absorber portion from the absorbing liquid for flowing to absorption cycle slot in absorption cycle slot
Ammonium sulfate, part ammonium sulfite are pumped into absorber portion by absorbent recirculation pump and are used as absorbent；Part ammonium sulfite is followed in absorption
It aoxidizes to form ammonium sulfate by the oxidation air that oxidation fan inputs in annular groove, ammonium sulfate is admitted to by ammonium sulfate delivery pump
Enriching section.
Slurries in enriching section come into full contact with flue gas, and moisture evaporation therein enters flue gas, and concentration constantly raises, finally
Reach saturated solution (about 55 DEG C, 46%) at such a temperature, operation lasting afterwards causes ammonium sulfate crystallization to be precipitated, Zhi Daonong
In contracting section slurries during ammonium sulfate crystallization containing 5-15%, ammonium sulfate system production ammonium sulfate is emitted by slurry discharge pump.
Slurry discharge pump conveying slurries enter cyclone, and the ammonium sulfate slurries with crystallization continue to be concentrated in cyclone
Solid content reaches 45%, and the slurries of overflow return to enriching section stock tank.The ammonium sulfate slurries of solid content 45% pass through centrifuge into one
Thickening is walked, obtains the wet ammonium sulfate of moisture content≤5%.Wet ammonium sulfate enters drying machine through screw(-type) feeder, by hot wind
After drying, the ammonium sulfate product of moisture content≤0.3% is obtained, most stores or sells after automatic packaging machine is packed afterwards.
In absorption tower, process water is supplemented by being located at the mist eliminator flushing above washing layer.Wash the water of layer
By being pumped into absorber portion, the absorbing liquid of absorber portion enters enriching section also by pump, so that realizes water balance in absorption tower.
Ammonium hydroxide addition is controlled by absorber portion pH value.According to the exhaust gas volumn of the entrance on absorption tower, SO2 concentration, absorber portion
The parameters such as pH value determine specific ammonium hydroxide injection rate.
Claims (6)
1. a kind of flue gas desulfurization technique of ultra-clean discharge, it is characterised in that using ammonia as desulfurizing agent, high-temperature flue gas is through absorption tower
Enriching section enters absorption tower absorber portion after being cooled to 50~70 DEG C, absorbing liquid and the SO in flue gas in absorber portion2Reaction is completed
Sweetening process, the absorbing liquid after reaction is from absorption cycle slot is flow to, and absorbing liquid generates sulfurous with ammonia reaction in absorption cycle slot
Sour ammonium, part ammonium sulfite return to absorber portion as absorbing liquid, and part ammonium sulfite is oxidized to ammonium sulfate, ammonium sulfate quilt
It send to enriching section and flue gas heat exchange, ammonia sulfate crystal is precipitated, and the suspension containing ammonia sulfate crystal is by eddy flow, filtering, solid
Become finished product through dry, liquid returns again to enriching section, and the flue gas after desulfurization is after chevron mist eliminator into absorption tower top
The processing of flue gas after desulfurization deep purifying section, reaches ultra-clean discharge standard.
2. according to the flue gas desulfurization technique described in right 1, it is characterised in that high-temperature flue gas initially enters ammonium sulfate concentration section, makes height
Warm flue-gas temperature is reduced to 50~70 DEG C, and then the flue gas after saturation enters back into absorber portion and reacted with absorbing liquid, avoids
Ammonium sulfite in absorbing liquid is decomposed into gaseous ammonia and gaseous sulfur dioxide, thoroughly solves gaseous ammonia and gaseous sulfur dioxide
The problem of solid particle ammonium sulfite and ammonium sulfate are generated under the conditions of water vapour, forms aerosol is the ultra-clean row of flue gas desulfurization
It puts and creates good condition.
3. according to the flue gas desulfurization technique described in right 1, it is characterised in that flue gas is after absorber portion carries out desulfurization, using folding
Plate demister carries out removing dust and droplet processing, ensures that dust and droplet content are less than 75mg/Nm3 (grains in flue gas after desulfurization
Footpath is more than 20um dust and droplet).
4. according to the flue gas desulfurization technique described in right 1, it is characterised in that from chevron mist eliminator come out flue gas after desulfurization into
Enter the flue gas after desulfurization deep purifying section at the top of absorption tower, further remove dust and absorbent mist in flue gas after desulfurization
Drop.
5. according to the flue gas desulfurization technique described in right 1, it is characterised in that flue gas after desulfurization deep purifying section be divided into washing layer and
Mesh mist eliminator, washing layer set a water washing cycles slot, two water washing cycles pump (the using and the reserved), one layer of washing spraying layer,
One section of washing layer filler, a set of washing layer liquid header, the dust carried secretly by flue gas after desulfurization after folded plate demister and
Droplet is seldom, and after washing layer washing, water washing cycles liquid equilibrium concentration is very low, and salinity is about 1%.
6. the flue gas after desulfurization deep purifying section according to right 5, it is characterised in that mesh mist eliminator is woven wire demisting
Device, material S316, mesh mist eliminator two layers of flushing water setting up and down, mesh mist eliminator can capture dust more than grain size 5um
And droplet, catch rate 99.98%, but because in droplet salinity be about 1%, therefore when neat stress is discharged into air, solid particulate matter
Content is less than 10mg/Nm3, ensures the ultra-clean discharge of neat stress.
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| CN201611002677.4A CN108067091A (en) | 2016-11-15 | 2016-11-15 | A kind of ultra-clean discharge flue gas desulfurization technique |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109200783A (en) * | 2018-09-28 | 2019-01-15 | 北京国电龙源环保工程有限公司 | Process of desulfurization for boiler flue gas device and its process flow |
| CN109764351A (en) * | 2018-12-12 | 2019-05-17 | 河南心连心化肥有限公司 | A kind of coal-fired boiler tail gas minimum discharge device and discharge technology |
| CN109939541A (en) * | 2019-04-19 | 2019-06-28 | 安徽金森源环保工程有限公司 | A kind of coking industry dry coke quenching tail gas by ammonia method desulfurizer |
| CN110115919A (en) * | 2019-04-19 | 2019-08-13 | 陕西陕化煤化工集团有限公司 | It is a kind of for sulfur recovery when acid tail gas in sulphur recovery process |
| CN111111413A (en) * | 2020-01-13 | 2020-05-08 | 江苏远东环保工程有限公司 | Desulfurization system and process for ultralow emission of waste gas in carbon black industry |
| CN111330442A (en) * | 2020-04-08 | 2020-06-26 | 西安热工研究院有限公司 | Ammonia process catalysis combined desulfurization and denitrification method |
| CN112047359A (en) * | 2020-09-17 | 2020-12-08 | 嘉施利（宜城）化肥有限公司 | Comprehensive utilization process for acid-making tail gas and sulfur-based compound fertilizer production |
| CN113996150A (en) * | 2021-11-03 | 2022-02-01 | 福建三宝钢铁有限公司 | Efficient desulfurization and denitrification method and system |
| WO2022095148A1 (en) * | 2020-11-03 | 2022-05-12 | 江南环保集团股份有限公司 | Method for applying membrane separation apparatus to ammonia desulfurization |
| CN114956421A (en) * | 2022-03-25 | 2022-08-30 | 同兴环保科技股份有限公司 | Zero-emission method for preparing acid from desulfurization waste liquid and sulfur foam |
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109200783A (en) * | 2018-09-28 | 2019-01-15 | 北京国电龙源环保工程有限公司 | Process of desulfurization for boiler flue gas device and its process flow |
| CN109764351A (en) * | 2018-12-12 | 2019-05-17 | 河南心连心化肥有限公司 | A kind of coal-fired boiler tail gas minimum discharge device and discharge technology |
| CN109939541A (en) * | 2019-04-19 | 2019-06-28 | 安徽金森源环保工程有限公司 | A kind of coking industry dry coke quenching tail gas by ammonia method desulfurizer |
| CN110115919A (en) * | 2019-04-19 | 2019-08-13 | 陕西陕化煤化工集团有限公司 | It is a kind of for sulfur recovery when acid tail gas in sulphur recovery process |
| CN111111413B (en) * | 2020-01-13 | 2022-04-29 | 江苏远东环保工程有限公司 | Desulfurization system and process for ultralow emission of waste gas in carbon black industry |
| CN111111413A (en) * | 2020-01-13 | 2020-05-08 | 江苏远东环保工程有限公司 | Desulfurization system and process for ultralow emission of waste gas in carbon black industry |
| CN111330442A (en) * | 2020-04-08 | 2020-06-26 | 西安热工研究院有限公司 | Ammonia process catalysis combined desulfurization and denitrification method |
| CN111330442B (en) * | 2020-04-08 | 2022-03-08 | 西安热工研究院有限公司 | Ammonia process catalysis combined desulfurization and denitrification method |
| CN112047359A (en) * | 2020-09-17 | 2020-12-08 | 嘉施利（宜城）化肥有限公司 | Comprehensive utilization process for acid-making tail gas and sulfur-based compound fertilizer production |
| WO2022095148A1 (en) * | 2020-11-03 | 2022-05-12 | 江南环保集团股份有限公司 | Method for applying membrane separation apparatus to ammonia desulfurization |
| CN113996150A (en) * | 2021-11-03 | 2022-02-01 | 福建三宝钢铁有限公司 | Efficient desulfurization and denitrification method and system |
| CN113996150B (en) * | 2021-11-03 | 2022-07-15 | 福建三宝钢铁有限公司 | Efficient desulfurization and denitrification method and system |
| CN114956421A (en) * | 2022-03-25 | 2022-08-30 | 同兴环保科技股份有限公司 | Zero-emission method for preparing acid from desulfurization waste liquid and sulfur foam |
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