CN106881012A - A kind of coking furnace desulfurization and denitrification integral system - Google Patents
A kind of coking furnace desulfurization and denitrification integral system Download PDFInfo
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- CN106881012A CN106881012A CN201710157149.4A CN201710157149A CN106881012A CN 106881012 A CN106881012 A CN 106881012A CN 201710157149 A CN201710157149 A CN 201710157149A CN 106881012 A CN106881012 A CN 106881012A
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- hydrogen peroxide
- ozone
- metering system
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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
- B01D53/79—Injecting reactants
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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
- B01D53/60—Simultaneously removing sulfur oxides and nitrogen oxides
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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
- B01D53/76—Gas phase processes, e.g. by using aerosols
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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Abstract
The present invention relates to a kind of coking furnace desulfurization and denitrification integral system, including ozone generator (1), ozone metering system (2), ozone loading system (3), dioxygen water storage tank (4), hydrogen peroxide metering system (5) and hydrogen peroxide loading system, the gas outlet of ozone generator (1) connects ozone metering system (2) by pipeline, ozone metering system (2) is connected in the flue before desulfurizing tower (7) by ozone loading system (3), hydrogen peroxide loading system is provided between desulfurizing tower (7) desulfurization spraying layer and demisting plate, hydrogen peroxide loading system connects hydrogen peroxide metering system (5) by pipeline, hydrogen peroxide metering system (5) connects dioxygen water storage tank (4) by dioxygen water pump (6)；Compared with the existing technology, denitration efficiency is high, equipment volume is smaller, change small to existing equipment, and does not use ammoniacal liquor, without the escaping of ammonia, can adapt to the acute variation of flue gas flow, high degree of automation for the present invention.
Description
[technical field]
The present invention relates to gas denitrifying technology field, specifically a kind of coking furnace desulfurization and denitrification integral system.
[background technology]
Denitration technology is relatively ripe in China, and the denitration technology for flue gas is mainly：Selective catalytic reduction
And SNCR method (SNCR) (SCR).Wherein, the advantage of selective catalytic reduction is：(1) denitration efficiency
It 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) have an impact to boiler furnace heat efficiency, after installing SCR reactors additional, the radiation loss of boiler kiln
Increase, may also change local heating's area, operating condition receives influence；(3) there is catalyst clogging phenomenon；(4) due to
There is the escaping of ammonia phenomenon, ammonia has stronger stickiness in SO3 reaction generation hydrogen sulfate ammonia, ammonium hydrogen sulfate in low-temperature zone, pair can set
It is standby to cause stifled ash, corrosion.And the advantage of SNCR method is:(1) equipment investment is low；(2) catalyst, nothing are not used
The stifled ash of catalyst, poisoning；(3) urea can be used, without building ammoniacal liquor storage facility.Its shortcoming is:(1) denitration efficiency is low, takes off
Nitre efficiency is in 30%-50%, it is impossible to meet existing environmental requirement；(2) need to transform boiler furnace；(3) in burner hearth
Spray ammoniacal liquor or urea liquid have an impact to boiler efficiency.At present, flue gas desulfurization and denitration is divided to two mode process to carry out, this
Sample investment is high with operating cost, is not suitable for China's actual conditions.
[content of the invention]
A kind of coking furnace desulfurization and denitrification integral system is provided present invention aim to solve above-mentioned deficiency, is taken off
Nitre efficiency high, equipment volume are smaller, change small to existing equipment, and do not use ammoniacal liquor, without the escaping of ammonia, are applicable low-temperature denitration, nothing
Catalyst poisoning, can adapt to the acute variation of flue gas flow, high degree of automation.
A kind of coking furnace desulfurization and denitrification integral system, including ozone generator 1, ozonometer are designed to achieve the above object
Amount system 2, ozone loading system 3, dioxygen water storage tank 4, hydrogen peroxide metering system 5 and hydrogen peroxide loading system, the ozone hair
The gas outlet of raw device 1 connects ozone metering system 2 by pipeline, and the ozone metering system 2 is connected by ozone loading system 3
In flue before to desulfurizing tower 7, hydrogen peroxide loading system is provided between the desulfurization spraying layer of the desulfurizing tower 7 and demisting plate, it is described
Hydrogen peroxide loading system connects hydrogen peroxide metering system 5 by pipeline, and the hydrogen peroxide metering system 5 is connected by dioxygen water pump 6
Connect dioxygen 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 ozone generator 1, ozone metering system 2, hydrogen peroxide metering system 5, hydrogen peroxide
Pump 6, air compressor machine 10 pass through connection electric-control system 11 respectively.
The present invention compared with the existing technology, has the following advantages that：
(1) denitration efficiency of the present invention is high, equipment volume is smaller, for original hydrogen peroxide oxidation method, ozone with
The affinity of NOX is strong, and denitration reaction speed is fast (mainly being controlled by gas film mass transfer), and denitration efficiency is up to more than 95%, and operation is flat
Surely；And be combined with new injection loading system using accurate metering system, make the use of equipment volume and ozone and hydrogen peroxide
Amount further reduces；
(2) catalyst is not used, catalyst poisoning will not be caused when being applied in coke oven flue gas, and in denitrification process
In, the solubility in follow-up desulfurizing agent solution of the denitration product for being formed is higher, less scaling；Even if caused by misoperation
Temporary transient scale formation, can also 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 is only caused, and the new pollution for causing, easily cause downstream flue and inner wall of stack to scab, discharge flue gas and contain
Aerosol and excitant ammonia taste etc.；Even if carrying out precooling to flue gas and except tower flue gas washing is also difficult to thoroughly solve above-mentioned asking
Topic；
(4) hydrogen peroxide is filled in desulfurizing tower afterbody further to remove remaining NOX, due in flue gas herein SO2 amounts compared with
Small, hydrogen peroxide is little with the amount of SO2 reactions, and most of and NOx reactions reduce the consumption of H2O2.
To sum up, denitration efficiency of the present invention is high, equipment volume is smaller, change small to existing equipment, and does not use ammoniacal liquor, without ammonia
Escape, can adapt to the acute variation of flue gas flow, high degree of automation.
[brief description of the drawings]
Fig. 1 is structural representation of the invention；
In figure：1st, ozone generator 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]
Further explained below is made to the present invention below in conjunction with the accompanying drawings：
As shown in Figure 1, for carrying out desulphurization denitration treatment to the flue gas that coke oven is produced, system includes the present invention：Ozone
Generator 1, ozone metering system 2, ozone loading system 3, dioxygen water storage tank 4, hydrogen peroxide metering system 5 and hydrogen peroxide filling system
System, the gas outlet of ozone generator 1 connects ozone metering system 2 by pipeline, and ozone metering system 2 passes through ozone loading system
3 are connected in the flue before desulfurizing tower 7, and hydrogen peroxide loading system, dioxygen are provided between the desulfurization spraying layer of desulfurizing tower 7 and demisting plate
Water loading system connects hydrogen peroxide metering system 5 by pipeline, and hydrogen peroxide metering system 5 connects hydrogen peroxide by dioxygen water pump 6
Storage tank 4.Used as the preferred technical solution of the present invention, system for desulfuration and denitration top can also be provided with scrubbing tower, scrubbing tower connection
There is chimney.
In the present invention, the gas approach of desulfurizing tower 7 is provided with venturi driving nozzle 8, and venturi driving nozzle 8 passes through pipeline
Connection compressed air reservoir 9, the air inlet of compressed air reservoir 9 is connected with air compressor machine 10, and compressed air reservoir 9 goes out
Gas port is also connected to hydrogen peroxide loading system by pipeline.Hydrogen peroxide loading system includes that hydrogen peroxide fills shower nozzle, and hydrogen peroxide adds
Note shower nozzle is arranged in desulfurizing tower 7 between desulfurization spraying layer and demisting plate at position.Also include electric-control system 11, ozone generator
1st, ozone metering system 2, hydrogen peroxide metering system 5, dioxygen water pump 6, air compressor machine 10 pass through connection electric-control system 11 respectively.
In the present invention, ozone generator produces ozone, and measuring system meters by ozone needs the amount of filling, then by smelly
Be delivered to for ozone in the flue before desulfurizing tower by oxygen loading system.Hydrogen peroxide in dioxygen water storage tank passes through hydrogen peroxide metering system
In measuring the hydrogen peroxide loading system being pumped between desulfurizing tower spraying layer and demisting plate by hydrogen peroxide after the amount of output.This dress
Put and combined on the basis of original hydrogen peroxide oxidation method the stronger ozone of oxidisability, reduce the consumption of hydrogen peroxide, improve de-
Nitre efficiency, solves the problems, such as the denitration of low-temperature flue gas.
Amount ozone metering a certain amount of ozone of system meters according to nitrogen oxides in coke oven flue gas is delivered to desulfurizing tower and enters
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 conveying 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, H2O2In this position, filling will not be with SO2Reaction, 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 fluctuation 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.Often there is a small amount of Jiao
Producer gas is mixed into flue gas, wherein micro reducible sulfur compound (such as vulcanization chlorine, carbon disulfide 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 using some oxidizing substances such as (ozone, hydrogen peroxide) by flue gas
With the nitrogen oxides of NO (being insoluble in water) form presence into NO2NO2Then 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 reaction speeds is obtained soon with gas phase is all, while ozone is to NOx
With SO2Reaction have selectivity, preferentially with NOx react.Oxidizing process does not use catalyst, it is to avoid catalyst poisoning failure and
The jejune problem of low temperature catalyst, while being transformed without to coking furnace shaft.It is all in coking furnace desulphurization denitration engineering
Set foot in and belong to patent of the present invention for Ozonation, double air water oxidizing process and ozone hydrogen peroxide co-oxidation method technological requirement
Protection of usage right category.
The present invention is not limited by above-mentioned implementation method, other any without departing from Spirit Essence of the invention and principle
Lower made change, modification, replacement, combination, simplification, should be equivalent substitute mode, be included in protection model of the invention
Within enclosing.
Claims (6)
1. a kind of coking furnace desulfurization and denitrification integral system, it is characterised in that：Including ozone generator (1), ozone metering system
(2), ozone loading system (3), dioxygen water storage tank (4), hydrogen peroxide metering system (5) and hydrogen peroxide loading system, the ozone
The gas outlet of generator (1) connects ozone metering system (2) by pipeline, and the ozone metering system (2) is filled by ozone
System (3) is connected in the flue before desulfurizing tower (7), and dioxygen is provided between desulfurizing tower (7) the desulfurization spraying layer and demisting plate
Water loading system, the hydrogen peroxide loading system connects hydrogen peroxide metering system (5), the hydrogen peroxide metering system by pipeline
(5) dioxygen water storage tank (4) is connected by dioxygen water pump (6).
2. coking furnace desulfurization and denitrification integral system as claimed in claim 1, it is characterised in that：Desulfurizing tower (7) entrance
Flue is provided with venturi driving nozzle (8), and the venturi driving nozzle (8) connects compressed air reservoir by pipeline
(9), the air inlet of the compressed air reservoir (9) is connected with air compressor machine (10).
3. coking furnace desulfurization and denitrification integral system 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 desulfurization and denitrification integral system as claimed in claim 3, it is characterised in that：The hydrogen peroxide loading system
Shower nozzle is filled including hydrogen peroxide, 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 desulfurization and denitrification integral system as claimed in claim 4, it is characterised in that：Desulfurizing tower (7) top
Scrubbing tower is connected with by pipeline, the scrubbing tower connects chimney by pipeline.
6. coking furnace desulfurization and denitrification integral system as claimed in claim 5, it is characterised in that：Also include electric-control system
(11), the ozone generator (1), ozone metering system (2), hydrogen peroxide metering system (5), dioxygen water pump (6), air compressor machine
(10) connection electric-control system (11) is passed through respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710157149.4A CN106881012A (en) | 2017-03-16 | 2017-03-16 | A kind of coking furnace desulfurization and denitrification integral system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201710157149.4A CN106881012A (en) | 2017-03-16 | 2017-03-16 | A kind of coking furnace desulfurization and denitrification integral system |
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| CN106881012A true CN106881012A (en) | 2017-06-23 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107694314A (en) * | 2017-10-18 | 2018-02-16 | 大唐南京发电厂 | A kind of system and technique for being classified oxidative absorption formula flue gas desulfurization and denitrification |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5511033A (en) * | 1978-07-10 | 1980-01-25 | Mitsubishi Heavy Ind Ltd | Simultaneous sampling method of nitrogen oxide and sulfur oxide |
| CN102343212A (en) * | 2011-10-11 | 2012-02-08 | 浙江天蓝环保技术股份有限公司 | Denitration process combining co-oxidation of ozone and hydrogen peroxide with wet absorption |
| CN104857835A (en) * | 2015-06-05 | 2015-08-26 | 北京中晶佳镁环境科技股份有限公司 | Integrated flue gas treatment device and method |
| CN204768208U (en) * | 2015-01-30 | 2015-11-18 | 邱吉康 | Flue gas to chain boiler carries out SOx/NOx control integration system |
| CN105983311A (en) * | 2015-01-30 | 2016-10-05 | 邱吉康 | Desulfurization and denitrification integrated system for flue gas of chain-grate boiler |
| CN206082111U (en) * | 2016-10-12 | 2017-04-12 | 黄胜建 | Coking furnace SOx/NOx control system |
-
2017
- 2017-03-16 CN CN201710157149.4A patent/CN106881012A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5511033A (en) * | 1978-07-10 | 1980-01-25 | Mitsubishi Heavy Ind Ltd | Simultaneous sampling method of nitrogen oxide and sulfur oxide |
| CN102343212A (en) * | 2011-10-11 | 2012-02-08 | 浙江天蓝环保技术股份有限公司 | Denitration process combining co-oxidation of ozone and hydrogen peroxide with wet absorption |
| CN204768208U (en) * | 2015-01-30 | 2015-11-18 | 邱吉康 | Flue gas to chain boiler carries out SOx/NOx control integration system |
| CN105983311A (en) * | 2015-01-30 | 2016-10-05 | 邱吉康 | Desulfurization and denitrification integrated system for flue gas of chain-grate boiler |
| CN104857835A (en) * | 2015-06-05 | 2015-08-26 | 北京中晶佳镁环境科技股份有限公司 | Integrated flue gas treatment device and method |
| CN206082111U (en) * | 2016-10-12 | 2017-04-12 | 黄胜建 | Coking furnace SOx/NOx control system |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107694314A (en) * | 2017-10-18 | 2018-02-16 | 大唐南京发电厂 | A kind of system and technique for being classified oxidative absorption formula flue gas desulfurization and denitrification |
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Application publication date: 20170623 |