CN206082111U - Coking furnace SOx/NOx control system - Google Patents
Coking furnace SOx/NOx control system Download PDFInfo
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- CN206082111U CN206082111U CN201621116800.0U CN201621116800U CN206082111U CN 206082111 U CN206082111 U CN 206082111U CN 201621116800 U CN201621116800 U CN 201621116800U CN 206082111 U CN206082111 U CN 206082111U
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- hydrogen peroxide
- ozone
- denitration
- desulfurizing tower
- metering system
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Abstract
The utility model relates to a coking furnace SOx/NOx control system, including ozone generator (1), ozone measurement system (2), ozone filling system (3), hydrogen peroxide solution storage tank (4), dioxygen water metering system (5) and hydrogen peroxide solution filling system, pipe connection ozone measurement system (2) is passed through to the gas outlet of ozone generator (1), ozone measurement system (2) are connected to in desulfurizing tower (7) preceding flue through ozone filling system (3), desulfurizing tower (7) desulfurization sprays and is equipped with hydrogen peroxide solution filling system between layer and the mist eliminating board, hydrogen peroxide solution filling system passes through pipe connection dioxygen water metering system (5), dioxygen water metering system (5) connects hydrogen peroxide solution storage tank (4) through dioxygen water pump (6), compared with the prior art, the utility model, denitration efficiency is high, the equipment volume is less, it is little to change the existing equipment, and does not adopt the aqueous ammonia, and no ammonia is escaped, can adapt to flue gas flux's violent change, and degree of automation is high.
Description
[technical field]
This utility model is related to gas denitrifying technology field, specifically a kind of coking furnace system for desulfuration and denitration.
[background technology]
At present, for the technology that the denitration of flue gas is adopted mainly has：Selective catalytic reduction (SCR) and selectivity are non-
Catalytic reduction method (SNCR).Wherein, the advantage of selective catalytic reduction is：(1) denitration efficiency is high；(2) operating temperature is moderate
At 350 DEG C -420 DEG C；(3) denitration product is nitrogen and water non-secondary pollution.Its shortcoming is：(1) investment and operating cost are high；
(2) boiler furnace heat efficiency is had an impact, after installing SCR reactors additional, the radiation loss of boiler kiln is increased, and may also be changed
Local heating's area, operating condition receives impact；(3) there is catalyst clogging phenomenon；(4) due to there is the escaping of ammonia phenomenon, ammonia
Gas generates hydrogen sulfate ammonia in SO3 reactions, and ammonium hydrogen sulfate has stronger stickiness in low-temperature zone, and stifled ash, corrosion can be caused to equipment.And
The advantage of SNCR method is:(1) equipment investment is low；(2) catalyst is not used, without the stifled ash of catalyst, poisoning；
(3) carbamide can be used, without building ammonia storage facility.Its shortcoming is:(1) denitration efficiency is low, and denitration efficiency is in 30%-
50%, it is impossible to meet existing environmental requirement；(2) need to transform boiler furnace；(3) spray ammonia in burner hearth or carbamide is molten
Liquid has an impact to boiler efficiency.
[utility model content]
The purpose of this utility model seeks to solve above-mentioned deficiency and provide a kind of coking furnace system for desulfuration and denitration, denitration
Efficiency high, equipment volume are less, change little to existing equipment, and do not adopt ammonia, without the escaping of ammonia, can adapt to flue gas flow
Acute variation, high degree of automation.
A kind of coking furnace system for desulfuration and denitration, including ozonator 1, ozone metering system are designed for achieving the above object
2nd, ozone loading system 3, dioxygen water storage tank 4, hydrogen peroxide metering system 5 and hydrogen peroxide loading system, the ozonator 1
Gas outlet connects ozone metering system 2 by pipeline, and the ozone metering system 2 is connected to desulfurization by ozone loading system 3
In flue before tower 7, hydrogen peroxide loading system, the hydrogen peroxide are provided between the desulfurization spraying layer of the desulfurizing tower 7 and demisting plate
Loading system connects hydrogen peroxide metering system 5 by pipeline, and the hydrogen peroxide metering system 5 connects dioxygen by dioxygen water pump 6
Water storage tank 4.
The gas approach of the desulfurizing tower 7 is provided with venturi driving nozzle 8, and the venturi driving nozzle 8 passes through pipeline
Connection compressed air reservoir 9, the air inlet of the compressed air reservoir 9 is connected with air compressor machine 10.
The gas outlet of the compressed air reservoir 9 is connected to hydrogen peroxide loading system by pipeline.
The hydrogen peroxide loading system includes that hydrogen peroxide fills shower nozzle, and the hydrogen peroxide filling shower nozzle is arranged on desulfurizing tower 7
Between interior desulfurization spraying layer and demisting plate at position.
The top of the desulfurizing tower 7 is connected with scrubbing tower by pipeline, and the scrubbing tower connects chimney by pipeline.
Also include electric-control system 11, the ozonator 1, ozone metering system 2, hydrogen peroxide metering system 5, hydrogen peroxide
Pump 6, air compressor machine 10 pass through respectively connection electric-control system 11.
This utility model compared with the existing technology, has the advantage that：
(1) this utility model denitration efficiency height, equipment volume are less, smelly for original hydrogen peroxide oxidation method
Oxygen is strong with the affinity of NOX, and denitration reaction speed is fast (mainly being controlled by gas film mass transfer), and denitration efficiency is transported up to more than 95%
Row is steady；And equipment volume and ozone and hydrogen peroxide are made in combination with new injection loading system using accurate metering system
Consumption further reduce；
(2) catalyst is not adopted, catalyst poisoning will not be caused when being applied in coke oven flue gas, and in denitrification process
In, the dissolubility in follow-up desulfurizing agent solution of the denitration product for being formed is higher, less scaling；Even if because misoperation is caused
Temporarily scale formation, also can be eliminated by reducing the method for the pH value of doctor solution；
(3) smokeless band ammonia and other secondary pollution problems, in SCR and sncr methods, in order to ensure certain denitration rate,
Ammonia density needs to maintain higher level, but now under heat smoke effect, the ammonia in solution is easy to be volatized into flue gas, no
The loss of raw material, and the new pollution for causing only are caused, easily caused downstream flue and inner wall of stack to scab, discharged flue gas and contain
Aerosol and zest ammonia taste etc.；Even if pre-cooling is carried out to flue gas and except tower flue gas washing is also difficult to thoroughly solve above-mentioned asking
Topic；
(4) fill hydrogen peroxide in desulfurizing tower afterbody further to remove remaining NOX, due in flue gas herein SO2 amounts compared with
Little, hydrogen peroxide is little with the amount of SO2 reactions, and most of and NOx reactions reduce the consumption of H2O2.
To sum up, this utility model denitration efficiency is high, equipment volume is less, change little to existing equipment, and does not adopt ammonia,
Without the escaping of ammonia, the acute variation of flue gas flow, high degree of automation are can adapt to.
[description of the drawings]
Fig. 1 is structural representation of the present utility model；
In figure：1st, ozonator 2, ozone metering system 3, ozone loading system 4, dioxygen water storage tank 5, hydrogen peroxide
Metering system 6, dioxygen water pump 7, desulfurizing tower 8, venturi driving nozzle 9, compressed air reservoir 10, air compressor machine 11,
Electric-control system.
[specific embodiment]
Below in conjunction with the accompanying drawings further explained below is made to this utility model：
As shown in Figure 1, this utility model is used to carry out desulphurization denitration process to the flue gas that coke oven is produced, and system includes：
Ozonator 1, ozone metering system 2, ozone loading system 3, dioxygen water storage tank 4, hydrogen peroxide metering system 5 and hydrogen peroxide add
Injection system, the gas outlet of ozonator 1 connects ozone metering system 2 by pipeline, and ozone metering system 2 is filled by ozone
System 3 is connected in the flue before desulfurizing tower 7, and between the desulfurization spraying layer of desulfurizing tower 7 and demisting plate hydrogen peroxide loading system is provided with,
Hydrogen peroxide loading system connects hydrogen peroxide metering system 5 by pipeline, and hydrogen peroxide metering system 5 connects double by dioxygen water pump 6
Oxygen water storage tank 4.Used as optimal technical scheme of the present utility model, the system for desulfuration and denitration top can also be provided with scrubbing tower, and this is washed
Wash tower and be connected with chimney.
In this utility model, the gas approach of desulfurizing tower 7 is provided with venturi driving nozzle 8, and venturi driving nozzle 8 passes through
Pipeline connects compressed air reservoir 9, and the air inlet of compressed air reservoir 9 is connected with air compressor machine 10, compressed air reservoir 9
Gas outlet also hydrogen peroxide loading system is connected to by pipeline.Hydrogen peroxide loading system includes that hydrogen peroxide fills shower nozzle, dioxygen
Water filling shower nozzle is arranged in desulfurizing tower 7 between desulfurization spraying layer and demisting plate at position.Also include electric-control system 11, ozone is sent out
Raw device 1, ozone metering system 2, hydrogen peroxide metering system 5, dioxygen water pump 6, air compressor machine 10 pass through respectively the automatically controlled system of connection
System 11.
In this utility model, ozonator produces ozone, and measuring system meters by ozone needs the amount of filling, then leads to
Cross ozone loading system ozone is delivered in the flue before desulfurizing tower.Hydrogen peroxide in dioxygen water storage tank is measured by hydrogen peroxide
In the hydrogen peroxide loading system being pumped between desulfurizing tower spraying layer and demisting plate by hydrogen peroxide after the amount of system meters output.
This device combines the higher ozone of oxidisability on the basis of original hydrogen peroxide oxidation method, reduces the consumption of hydrogen peroxide, improves
Denitration efficiency, solves the problems, such as the denitration of low-temperature flue gas.
Desulfurizing tower is delivered to according to a certain amount of ozone of amount ozone metering system meters of nitrogen oxides in coke oven flue gas to enter
In venturi driving nozzle on mouth flue, by compressed air injection ozone, it is sufficiently mixed with flue gas, with reaction of nitrogen oxides.
H is set between desulfurizing tower desulfurization spraying layer and demister202Filling shower nozzle, hydrogen peroxide is delivered to metering device by conveyer device
The amount of controlled output, is filled into flue gas by compressed air injection shower nozzle.Due to substantial amounts of SO in flue gas2Gas is taken off
Remove, H2O2Will not be with SO in this position filling2Reaction, reduces H2O2Consumption.
In actual applications, specific course of reaction is：
(1) ozone denitration reaction:
NO+O3→NO2+O2
NO2+O3→NO3+O2
NO3+NO2→N2O5
NO+O+M→NO2+M
NO2+O→NO3
(2) hydrogen peroxide denitration reaction：
2NO2+H2O (liquid phase) → HNO3+HNO2
HNO2+NO2→HNO3+NO
2NO2+H2O2(liquid phase) → 2HNO3
HNO2+H2O2(liquid phase) → HNO3+H2O
NO+NO2+H2O2(liquid phase) → 2HNO3
SO2+H2O2(liquid phase) → H2SO4
Because coke oven denitration has flue gas flow undulatory property big, concentration is high, while flue-gas temperature is low, general only 200 DEG C-
300 DEG C, general SCR catalyst optimal reaction temperature is at 350 DEG C -420 DEG C.So being difficult to effectively using conventional SCR catalyst
Operation, and low temperature catalyst (referring to 320 DEG C of temperature below windows of satisfaction) also immature, the service life for being found out at present
And contamination resistance is preferable not enough.It is not enough good due to being sealed in work especially for coking kiln gas.Jing often has a small amount of Jiao
Producer gas is mixed in flue gas, wherein micro reducible sulfur compound (such as sulfuration chlorine, Carbon bisulfide and organic sulfur etc.) is to SCR macro agent
Toxic action is stronger, easily causes catalyst to inactivate.
In view of current technology above shortcomings, propose the New Technologies of coking flue gas desulfurization and denitrification integration,
It is the oxidative absorption method of nitrogen oxides.Its essence is in flue gas using some oxidizing substances such as (ozone, hydrogen peroxide)
The nitrogen oxides existed in NO (being insoluble in water) form are into NO2. and NO2Then readily soluble alkaline solution, can be together with sulfur dioxide
Removed by alkaline doctor solution.
Ozone is all gaseous state with nitrogen oxides in effluent, NOx response speeds is obtained soon with gas phase is all, while ozone is to NOx
With SO2Reaction there is selectivity, preferentially with NOx react.Oxidizing process do not use catalyst, it is to avoid catalyst poisoning failure and
The jejune problem of low temperature catalyst, while without transforming coking furnace shaft.It is all in coking furnace desulphurization denitration engineering
Set foot in and belong to this utility model for Ozonation, double air water oxidizing process and ozone hydrogen peroxide co-oxidation method technological requirement
Patent claim protection category.
This utility model is not limited by above-mentioned embodiment, other any real without departing from spirit of the present utility model
Matter and the change, modification, replacement made under principle, combine, simplify, should be equivalent substitute mode, being included in this practicality
Within new protection domain.
Claims (6)
1. a kind of coking furnace system for desulfuration and denitration, it is characterised in that：Including ozonator (1), ozone metering system (2), smelly
Oxygen loading system (3), dioxygen water storage tank (4), hydrogen peroxide metering system (5) and hydrogen peroxide loading system, the ozonator
(1) gas outlet connects ozone metering system (2) by pipeline, and the ozone metering system (2) is by ozone loading system (3)
It is connected in the flue before desulfurizing tower (7), hydrogen peroxide filling system is provided between desulfurizing tower (7) the desulfurization spraying layer and demisting plate
System, the hydrogen peroxide loading system connects hydrogen peroxide metering system (5) by pipeline, and the hydrogen peroxide metering system (5) passes through
Dioxygen water pump (6) connection dioxygen water storage tank (4).
2. coking furnace system for desulfuration and denitration as claimed in claim 1, it is characterised in that：On desulfurizing tower (7) gas approach
Venturi driving nozzle (8) is provided with, the venturi driving nozzle (8) connects compressed air reservoir (9) by pipeline, described
The air inlet of compressed air reservoir (9) is connected with air compressor machine (10).
3. coking furnace system for desulfuration and denitration as claimed in claim 2, it is characterised in that：The compressed air reservoir (9)
Gas outlet is connected to hydrogen peroxide loading system by pipeline.
4. coking furnace system for desulfuration and denitration as claimed in claim 3, it is characterised in that：The hydrogen peroxide loading system includes double
Oxygen water fills shower nozzle, and the hydrogen peroxide filling shower nozzle is arranged between the interior desulfurization spraying layer of desulfurizing tower (7) and demisting plate at position.
5. coking furnace system for desulfuration and denitration as claimed in claim 4, it is characterised in that：Desulfurizing tower (7) top is by pipe
Road is connected with scrubbing tower, and the scrubbing tower connects chimney by pipeline.
6. coking furnace system for desulfuration and denitration as claimed in claim 5, it is characterised in that：Also include electric-control system (11), it is described
Ozonator (1), ozone metering system (2), hydrogen peroxide metering system (5), dioxygen water pump (6), air compressor machine (10) lead to respectively
Cross connection electric-control system (11).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621116800.0U CN206082111U (en) | 2016-10-12 | 2016-10-12 | Coking furnace SOx/NOx control system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621116800.0U CN206082111U (en) | 2016-10-12 | 2016-10-12 | Coking furnace SOx/NOx control system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206082111U true CN206082111U (en) | 2017-04-12 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201621116800.0U Expired - Fee Related CN206082111U (en) | 2016-10-12 | 2016-10-12 | Coking furnace SOx/NOx control system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN206082111U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106881012A (en) * | 2017-03-16 | 2017-06-23 | 黄胜建 | A kind of coking furnace desulfurization and denitrification integral system |
| CN107158907A (en) * | 2017-06-29 | 2017-09-15 | 大连好月亮环保科技有限公司 | Oxidation plus wet absorption flue gas desulfurization and denitrification integral method and its device |
-
2016
- 2016-10-12 CN CN201621116800.0U patent/CN206082111U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106881012A (en) * | 2017-03-16 | 2017-06-23 | 黄胜建 | A kind of coking furnace desulfurization and denitrification integral system |
| CN107158907A (en) * | 2017-06-29 | 2017-09-15 | 大连好月亮环保科技有限公司 | Oxidation plus wet absorption flue gas desulfurization and denitrification integral method and its device |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20170801 Address after: 201203 Shanghai Zhangjiang hi tech park fanchun Road No. 400 Building 1 floor 301-324 room 3 Patentee after: SHANGHAI SHENLYU ENERGY SAVING ENVIRONMENTAL PROTECTION ENGINEERING DESIGN RESEARCH AND DEVELOPMENT CO., LTD. Address before: Pudong New Area Heqing town Dongchuan road 201201 Shanghai City No. 5227 Building 2 Patentee before: Huang Shengjian |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20170412 Termination date: 20171012 |