CN206881688U - A kind of system for producing sulfur trioxide and maintaining its gaseous state - Google Patents
A kind of system for producing sulfur trioxide and maintaining its gaseous state Download PDFInfo
- Publication number
- CN206881688U CN206881688U CN201720403372.8U CN201720403372U CN206881688U CN 206881688 U CN206881688 U CN 206881688U CN 201720403372 U CN201720403372 U CN 201720403372U CN 206881688 U CN206881688 U CN 206881688U
- Authority
- CN
- China
- Prior art keywords
- generating means
- sulfur trioxide
- main body
- gas
- gaseous state
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
Abstract
The utility model proposes a kind of system for producing sulfur trioxide and maintaining its gaseous state, including n feeder and the main body generating means being attached thereto, mass flow controller is connected between the caisson and main body generating means, it is characterized in that, even air chamber and oxidizing chamber are separated into dividing plate inside the main body generating means, shell is installed in the main body generating means outer surface, and the main body generating means is connected with the heater with the first temperature sensor, n >=2.Tthe utility model system improves Sulphur Dioxide efficiency and capacity usage ratio, effectively realizes the generation of gaseous sulfur trioxide, reduces Meteorological, beneficial to promoting the use of for device.
Description
Technical field
The generation device of sulfur trioxide is the utility model is related to, more particularly to one kind produces sulfur trioxide and maintains its gas
The system of state.
Background technology
Sulfur trioxide (SO3) gas and unstable and be difficult to keep, therefore, the high sulfur trioxide of purity generally can not pass through
Purchase is obtained, i.e., sulfur trioxide gas should not be sold in the form of gas bomb or gas tank.Because sulfur trioxide can be deposited in water
Sulfuric acid (H is quickly converted under lower temperature conditions in case2SO4), therefore, the acquisition of gaseous sulfur trioxide is a skill
Art problem.
Utility model content
In order to solve the above problems, the utility model proposes it is a kind of generation sulfur trioxide and maintain its gaseous state be
System, including n feeder and the main body generating means that is attached thereto, the gas storage/feeder and main body generating means it
Between be connected with mass flow controller, it is characterised in that even air chamber and oxygen are separated into dividing plate inside the main body generating means
Change room, shell is installed in the main body generating means outer surface, and the main body generating means is connected with the first temperature sensor
Heater, n >=2.
Further, the main body generating means is cylinder.
Further, the shell is made up of heat-barrier material, and outside installation waste-heat recovery device.
Further, it is provided with aft cover plate group in the even air chamber.
Further, catalyst case is set inside the oxidizing chamber.
Further, the main body generating means configuration installation heater.
Further, it is characterised in that also including automatic controller.
Tthe utility model system is improved existing process, optimizes reaction condition, improves Sulphur Dioxide
Efficiency and capacity usage ratio, the generation of gaseous sulfur trioxide is effectively realized, reduces Meteorological, the popularization beneficial to device makes
With.
Brief description of the drawings
Fig. 1 is a kind of generation sulfur trioxide and the schematic diagram for the system for maintaining its gaseous state in the utility model；
Fig. 2 is the utility model embodiment 2 using schematic diagram during air pump；
Fig. 3 is the flow chart of utility model works.
In figure：The air accumulators of 1-1- first, the air accumulators of 1-2- second, 2-1- sulfur dioxide conveyance conduit, 2-2- carrier gas are defeated
Send pipeline, 2-3- hot-air ducts, 2-4- cleaning feed channel, 2-5- gaseous mixtures inlet duct, 2-6- sulfur trioxides outlet conduit,
The pressure-reducing valves of 3-1- first, the pressure-reducing valves of 3-2- second, the stop valves of 4-1- first, the stop valves of 4-2- second, the stop valves of 4-3- the 3rd, 4-
The stop valves of 4- the 4th, the stop valves of 4-5- the 5th, the stop valves of 4-6- the 6th, the mass flow controllers of 5-1- first, the matter of 5-2- second
Measure flow controller, the mass flow controllers of 5-3- the 3rd, the mass flow controllers of 5-4- the 4th, 6- heaters, 7- air
Pump, 8- drying devices, 9- waste-heat recovery devices, 10- main bodys generating means, the even air chambers of 10-1-, 10-2- oxidizing chambers, 10-3- are urged
Agent room, 10-4- shells, the temperature sensors of 11-1- first, 11-2- second temperature sensors, 11-3- three-temperature sensors,
12- automatic controllers, 13- aft cover plate groups.
Embodiment
The system for producing sulfur trioxide and maintaining its gaseous state a kind of to the utility model is specific below in conjunction with the accompanying drawings
Embodiment is described in detail, and the embodiment is merely to illustrate the utility model rather than limitation model of the present utility model
Enclose, modification of the those skilled in the art to the various equivalent form of values of the present utility model falls within the application appended claims and limited
Fixed scope.
Embodiment 1
Such as Fig. 1, a kind of system for producing sulfur trioxide and maintaining its gaseous state, including n gas storage/feeder, master
Body generating means 10 and heater 6, n 2.Main body generating means 10 by integration even air chamber 10-1 and oxidizing chamber 10-2 with
And shell 10-4 compositions, shell 10-4 are 200 × 500mm of φ cylinder, shell 10-4 is made up of heat-barrier material, such as aerosol
Plate, and the surface of main body generating means 10 is wrapped in, so as to the effect of realization device insulation.Even air chamber 10-1, oxidizing chamber 10-2 are equal
It is placed in inside shell 10-4, is separated between even air chamber 10-1 and oxidizing chamber 10-2 with air distribution plate, even air chamber 10-1 and oxidizing chamber 10-
2 size is 100 × 225mm of φ, and adjustable reacting gas flow velocity scope is 0.1-2.0m3/h.Inside even air chamber 10-1
It is final uniform so as to improve the uniformity coefficient of gaseous mixture mixing to change flowing gas state provided with labyrinth type aft cover plate group 13
Into oxidizing chamber 10-2.Oxidizing chamber 10-2 includes catalyst case 10-3 and supporting construction, and catalyst case 10-3 passes through supporting construction
It is fixed on oxidizing chamber 10-2.
Caisson includes the first air accumulator 1-1, the second air accumulator 1-2, the first air accumulator 1-1 and main body generating means 10
First pressure-reducing valve 3-1, the first stop valve 4-1 and the first mass flow are installed successively on connected sulfur dioxide conveyance conduit 2-1
Second is installed successively on controller 5-1, the carrier gas conveyance conduit 2-2 that the second air accumulator 1-2 is connected with main body generating means 10
Pressure-reducing valve 3-2, the second stop valve 4-2 and the second mass flow controller 5-2.First air accumulator 1-1 is to include concentration known two
The cylinder of the admixture of gas of sulfur oxide and air, the first pressure-reducing valve 3-1 control the gas in the first air accumulator 1-1 to be stored up from first
Gas tank 1-1 flows into sulfur dioxide conveyance conduit 2-1, and is controlled by the first stop valve 4-1 and the first mass flow controller 5-1
The gas flowed out from the first air accumulator 1-1 flows into main body generating means 10 with the blended gas inlet duct 2-5 of certain flow rate
Even air chamber 10-1.Gaseous mixture inlet duct 2-5 is provided with qi-emitting hole.Second air accumulator 1-2 is to include air, nitrogen or other dilutions
The cylinder of gas, the gas that the source of the gas provides enter carrier gas conveyance conduit 2-2 by the second pressure-reducing valve 3-2, are passing through second
After stop valve 4-2, gas controls it to enter gaseous mixture inlet duct 2- with certain flow rate by the second mass flow controller 5-2
Eluting gas is mixed and fed into even air chamber 10-1 in 5, with the first air accumulator 1-1.
Heater 6 is used for the control of reaction temperature, and the temperature control of reaction can be promoted in certain temperature range
Conversion of the sulfur dioxide gas to sulfur trioxide gas, and maintain sulfur trioxide to exist with gaseous state.Such as Fig. 1 and Fig. 2, main body
In generating means 10 at catalyst case 10-3 and at sulfur trioxide outlet conduit 2-6, the first temperature sensor 11-1 is respectively provided with
With three-temperature sensor 11-3, to control generating means environment temperature.Pass through gas source control and temperature sensor control temperature
The modes such as degree, reactions of the oxidizing chamber 10-2 for sulfur dioxide and oxygen-containing gas on catalyst case 10-3 surfaces provide relative nothing
Water environment, to generate the sulfur trioxide gas of concentration known.In the present embodiment, heater 6 is electric heater unit, is placed in
Outside even air chamber 10-1 and catalyst case 10-3, for heatable catalyst room 10-3 and including sulfur dioxide and oxygen-containing gas
Unstripped gas to required temperature, in favor of sulfur dioxide in oxidizing chamber 10-2 to sulphur trioxide conversion.Caused sulfur trioxide
Gas exports the sulfur trioxide gas of certain concentration by sulfur trioxide outlet conduit 2-6 to outside main body generating means 10.
In addition, outside the shell 10-4 of main body generating means 10, in sulfur trioxide outlet conduit 2-6 and gaseous mixture entrance
Between pipeline 2-5, provided with pipe type exhaust heat retracting device 9, device outlet sulfur trioxide gas temperature is reduced to appropriate, and collect
Generating means exit heat, to preheat inlet gas, to improve the utilization rate of energy.
In the present embodiment, between oxidizing chamber 10-2 temperature need to maintain 400 degrees Celsius to 500 degrees Celsius, and will
Sulfur trioxide output channel 2-6 is maintained between 200 degrees Celsius to 300 degrees Celsius.Meanwhile the first air accumulator 1-1, the second gas storage
Mass flow controller on tank 1-2 and each pipeline is in room temperature state, is separated with heating environment or outside heating environment
Portion., can be by adjusting the flow velocity and dilution ratio of sulfur dioxide gas, there is provided three oxygen of concentration known in this embodiment
Change sulphur gas.
For providing the second air accumulator 1-2 of carrier gas reverse blow gas is provided for main body generating means 10.During purging, cut
Only valve 4-1,4-3 should be at closed mode, and purge gass are via Cleaning pipes 2-4, the 4th mass flowmenter 5-4 and the 4th stop valve
4-4 enters main body generating means 10, is discharged by floss hole through the 5th stop valve 4-5.
Main body generating means 10 is configured with automatic controller 12, the module by electronic signature capture sulfur dioxide gas and
Diluting gas flow, and the real time data such as catalyst member and sulfur trioxide gas output par, c temperature, are fed back by signal
The state of heater 6 and each gas circuit valve is controlled, temperature needed for sulfur trioxide generating process is controlled with this, and adjust according to demand
Sulfur dioxide gas and diluting gas flow are saved, so as to realize the auto-control of sulfur trioxide gas generating process and more preferable
Realize sulfur dioxide with about 100% conversion ratio Efficient Conversion.
Embodiment 2
Such as Fig. 2, in the present embodiment, air is provided using air pump 7, air is oxidation after the drying of drying device 8
Room 10-2 provides dry carrier gas.Heater 6 heats the gas provided by air pump 7, make gas temperature reach 400 DEG C-
500 DEG C, the 6th stop valve 4-6 and the 3rd mass flow controller 5-3 control heating after gas flow velocity, flow successively through oxidizing chamber
Outside 10-2 and even air chamber 10-1, using heated oxide room 10-2 and even air chamber 10-1 temperature as setting value, so as to control dioxy
Change the environment temperature of sulphur conversion.Air as thermal source can be recycled, to improve the utilization rate of energy.
In the present embodiment, the dry air provided via the gas circuit of air pump 7 is additionally operable to carrier gas and reverse blow
The supply of gas.Supply as carrier gas is passed through by carrier gas conveyance conduit 2-2, and with the second stop valve 4-2 and the second mass
Flowmeter 5-2 controls air tolerance；During reverse blow, stop valve 4-1,4-2,4-3,4-6 should be at closed mode, purge gass warp
Main body generating means 10 is entered by Cleaning pipes 2-4, the 4th mass flowmenter 5-4 and the 4th stop valve 4-4, by floss hole through
Five stop valve 4-5 are discharged.
Due to there is the presence of a small amount of water in the mixture of sulfur dioxide and air, a part of sulphur trioxide conversion can be caused to be
Sulfuric acid, embodiment of the present utility model control the modes such as temperature, oxidizing chamber 10-2 by gas source control and temperature sensor
Water-less environment or control humidity environment are provided for the reaction of sulfur dioxide and oxygen-containing gas on catalyst case 10-3 surfaces, is used
In the process that Sulphur Dioxide is sulfur trioxide.When water content very little, the admixture of gas bag that such as the first air accumulator 1-1 is provided
During containing millionth water, these water can not pollute sulfur dioxide conveyance conduit 2-1, oxidizing chamber 10-2, dilution letter shoot
The admixture of gas of the parts such as road 2-2, it is ensured that caused sulfur trioxide possesses concentration known.
Fig. 3 is the flow chart of utility model works, and in step I, main body generating means 10 receives the two of concentration known
Sulfur oxide, such as the sulfur dioxide that the first air accumulator 1-1 is provided.Due to the stability of sulfur dioxide at ambient temperature, can incite somebody to action
It is temporarily stored into oxidizing chamber 10-2 gas tank.The gas can be pure sulfur dioxide, or comprising some carbon dioxide, nitrogen or its
The sulfur dioxide gaseous mixture of the concentration known of its inert gas.Wherein, the concentration of sulfur dioxide is expressed as hundred a ten thousandths
Or part per billion (ppb) (ppm).
In step II, main body generating means 10 receives the oxygen-containing gas of concentration known.Oxygen-containing gas can pass through first
Air accumulator 1-1 (to be mixed with a certain amount of oxygen in the sulfur dioxide gaseous mixture that now air accumulator provides) directly supply.This
When, mass flow controller 5-2,5-3 are closed to prevent other oxygen-containing gas to be mixed into, and pass through the first mass flow controller
5-1 controls and detected the flow velocity that gaseous mixture is exposed in oxidizing chamber 10-2 before catalyst case 10-3.
In another embodiment, in addition to the first air accumulator 1-1 is provided and contained sulfur dioxide gas, also with air accumulator 1-2
There is provided carrier gas (now air accumulator 1-1 provide sulfur dioxide be high-purity gas or using inert gas as background gas) with occur
Sulfur trioxide gas, the stream of sulfur dioxide and oxygen-containing gas is controlled and detected respectively by mass flow controller 5-1 and 5-2
Speed, and the mixing for controlling above two gas to be exposed to before catalyst case 10-3.
In a further alternative, passed through with air pump 7 by extracting air from the surrounding environment of main body generating means 10
Fed after being dried by drying device 8 as oxygen-containing gas in oxidizing chamber 10-2.Second stop valve 4-2 and the second mass flowmenter 5-
The gas source of 2 control oxygen-containing gas.
In step III, main body generating means 10 receive concentration known sulfur dioxide uniformly mixed with oxygen-containing gas after
Exposed to the surface of catalyst case 10-3 middle catalyst.Catalyst can reduce oxidizing sulfur dioxide as required for sulfur trioxide
Activation energy so that reaction can be carried out under relatively low temperature conditionss.Conventional catalyst includes metal or metallics
Mixture, such as palladium, platinum, stainless steel, iron oxide or vanadic anhydride.Catalyst case 10-3 has several configuration modes, can use
Loose metal material (such as particulate, powder, thin slice, particle) with establish the necessary path of mixed gas, increase mixed gas
In the contact area of catalyst surface, to promote conversion of the sulfur dioxide to sulfur trioxide.
Heater 6 can be used to heat for catalyst in oxidizing chamber 10-2, so as to promote concentration known sulfur dioxide and contain
The reaction of carrier of oxygen.Such as tube heater thermal source can be selected in heater 6.Under conditions of without catalyst, work as oxidizing chamber
Fully heated in 10-2, when being higher than 600 degrees Celsius such as temperature, sulfur dioxide is converted.And the main body equipped with catalyst occurs
Device 10 can effectively produce sulfur trioxide in 400 degrees centigrades.Therefore, by controlling the parameter of main body generating means 10 can
The conversion ratio of sulfur dioxide is controlled, so as to produce the sulfur trioxide of concentration known.
Sulphur Dioxide is man-to-man reaction for the reaction of sulfur trioxide, i.e., when the initial concentration of sulfur dioxide is
When 100ppm and conversion ratio are 100%, the sulfur trioxide of generation is 100ppm.And in the case of oxygen excess, influence dioxy
Changing the parameter of sulphur conversion ratio includes oxidizing chamber 10-2 entrance and exit flow velocity, catalyst case 10-3 temperature, surface area, relative
Humidity etc..By controlling these parameters, the main body generating means 10 of sulfur trioxide generating means can be by about 100% sulfur dioxide
It is converted into sulfur trioxide.
In step IV, the sulfur trioxide gas of the concentration known of generation are remained gas shape by main body generating means 10
State.In one embodiment, by Cleaning pipes 2-4 and mass flow controller 5-4 into sulfur trioxide output channel 2-6
The air of heating is passed through to dilute sulfur trioxide gas, and controls tubular type waste-heat recovery device 9, maintains sulfur trioxide to use gas
Temperature be higher than sulfuric acid conversion/condensation point.
In running, it may occur that catalyst poisoning phenomenon, i.e. catalyst condition are degenerated, and cause Sulphur Dioxide rate
Decline.This phenomenon is typically betided after sulfur trioxide produces several days or a few houres, generally reversible process.It is catalyzed to reply
Agent activity, can temporarily heatable catalyst to more than 550 degrees Celsius, with during burn off use in catalyst 0-3 surface aggregations
Impurity.After the process, catalyst can effective activity recovery (such as larger than 98%).
The utility model is improved existing process, optimizes reaction condition, improves Sulphur Dioxide efficiency
And capacity usage ratio, the generation of gaseous sulfur trioxide is effectively realized, reduces Meteorological, beneficial to promoting the use of for device.
Tthe utility model system has following beneficial technique effect：
1. the waste-heat recovery device in system, the heat transfer of high temperature sulfur trioxide gas can be entered to main body generating means
The gaseous mixture of mouth sulfur dioxide and oxygen-containing gas, to realize the purpose of reacting gas preheating, so as to improve the utilization rate of energy, drop
Low Meteorological.
2. being provided with aft cover plate group in even air chamber, the uniformity of the mixing of gas can be optimized；Cloth is set below catalyst case
Air bound plate, make uniform distribution of the gaseous mixture in catalyst surface, be more beneficial for the progress of Sulphur Dioxide reaction.
3. the conversion process of sulfur dioxide fully takes into account the condition that chemical reaction is carried out that influences, urged using vanadic anhydride
Agent, increase the time of contact of gaseous mixture and catalyst, optimize reaction temperature condition, reach the conversion ratio of sulfur dioxide
100%.
4. there is automatic temp controller inside device, the automaticity of system is improved, makes simple operation, beneficial to device
Promote the use of.
Preferred embodiment of the present utility model, still, the utility model and unlimited is described in detail above in association with accompanying drawing
Detail in above-mentioned embodiment, can be to skill of the present utility model in range of the technology design of the present utility model
Art scheme carries out a variety of simple variants, and these simple variants belong to the scope of protection of the utility model.
Claims (7)
- Sulfur trioxide and the system that maintains its gaseous state are produced 1. a kind of, including n feeder and the main body that is attached thereto Generating means (10), mass flow controller (5), its feature are connected between the feeder and main body generating means (10) It is, the main body generating means (10) is internal to be separated into even air chamber (10-1) and oxidizing chamber (10-2), the main body with dividing plate Generating means (10) outer surface installation shell (10-4), the main body generating means (10) are connected with the first temperature sensor The heater (6) of (11-2), n >=2.
- 2. the system according to claim 1 for producing sulfur trioxide and maintaining its gaseous state, it is characterised in that the master Body generating means (10) is cylinder.
- 3. the system according to claim 1 for producing sulfur trioxide and maintaining its gaseous state, it is characterised in that described outer Shell (10-4) is made up of heat-barrier material, and outside installation waste-heat recovery device (9).
- 4. the system according to claim 1 for producing sulfur trioxide and maintaining its gaseous state, it is characterised in that described even Aft cover plate group (13) is provided with air chamber (10-1).
- 5. the system according to claim 1 for producing sulfur trioxide and maintaining its gaseous state, it is characterised in that the oxygen Change and catalyst case (10-3) is set inside room (10-2).
- 6. the system according to claim 1 for producing sulfur trioxide and maintaining its gaseous state, it is characterised in that the master Body generating means (10) configuration installation heater (6).
- 7. the system according to claim 1 for producing sulfur trioxide and maintaining its gaseous state, it is characterised in that also include Automatic controller (12).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720403372.8U CN206881688U (en) | 2017-04-18 | 2017-04-18 | A kind of system for producing sulfur trioxide and maintaining its gaseous state |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720403372.8U CN206881688U (en) | 2017-04-18 | 2017-04-18 | A kind of system for producing sulfur trioxide and maintaining its gaseous state |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206881688U true CN206881688U (en) | 2018-01-16 |
Family
ID=61324468
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201720403372.8U Active CN206881688U (en) | 2017-04-18 | 2017-04-18 | A kind of system for producing sulfur trioxide and maintaining its gaseous state |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206881688U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107020053A (en) * | 2017-04-18 | 2017-08-08 | 北京清新环境技术股份有限公司 | A kind of system and method for producing sulfur trioxide and maintaining its gaseous state |
-
2017
- 2017-04-18 CN CN201720403372.8U patent/CN206881688U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107020053A (en) * | 2017-04-18 | 2017-08-08 | 北京清新环境技术股份有限公司 | A kind of system and method for producing sulfur trioxide and maintaining its gaseous state |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10918992B2 (en) | System and method for desulfurization and dedusting of flue gas from coke oven | |
| CN103191640B (en) | A kind of SCR denitration reducing agent urea pyrolysis thermal source supply method and device | |
| CN110354630A (en) | Cold blast rate control method and device for Analytic Tower in flue gas purification system | |
| CN110538560A (en) | System and method for circularly combining desulfurization and ozone preoxidation denitration by using sintering flue gas | |
| CN107162060A (en) | A kind of uranyl nitrate air-blast atomization dry thermal cracking denitration prepares UO3Technique | |
| CN105582803A (en) | Desulfurization and denitrification method in boiler and desulfurization and denitrification reaction furnace thereof | |
| CN206881688U (en) | A kind of system for producing sulfur trioxide and maintaining its gaseous state | |
| CN203990273U (en) | Equipment for reducing the nitrous oxides concentration in the burning gases that produced by burner | |
| CN1071133C (en) | Method for-conditioning flue gas | |
| CN113713599A (en) | Circulating fluidized bed semi-dry method low-load desulfurization system and control method | |
| CN108844085A (en) | A kind of multi-stage heat exchanger point builds formula catalytic oxidation system and its processing method | |
| CN209406056U (en) | Sintering flue gas denitrification apparatus | |
| CN107020053A (en) | A kind of system and method for producing sulfur trioxide and maintaining its gaseous state | |
| CN109824017A (en) | Sulfur recovery facility and method based on the automatic adjustment of Crouse's air distribution | |
| CN110115927A (en) | A kind of ultralow nitrogen discharged processing method of ammonia-contaminated gas and system | |
| CN209865734U (en) | Sintering flue gas circulation is united ozone preoxidation's SOx/NOx control system | |
| CN112403181B (en) | Flue gas desulfurization and denitrification treatment system and method | |
| CN112403182B (en) | Analytic tower and flue gas heating system | |
| CN211782802U (en) | Energy-saving efficient synergistic treatment system for multiple pollutants in flue gas | |
| CN209828684U (en) | System for circularly combining desulfurization and ozone preoxidation denitration by using sintering flue gas | |
| CN206593090U (en) | Combustion system | |
| CN206229181U (en) | A kind of flue gas mercury removal system | |
| CN217016097U (en) | SCR flue gas denitration device | |
| CN212651632U (en) | Flue gas denitration system for diluting ammonia gas by desulfurized flue gas | |
| CN112403179B (en) | Shunting type flue gas desulfurization and denitrification treatment system and method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |