CN104359113A - Waste gas and waste liquid incineration system and method - Google Patents
Waste gas and waste liquid incineration system and method Download PDFInfo
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- CN104359113A CN104359113A CN201410611056.0A CN201410611056A CN104359113A CN 104359113 A CN104359113 A CN 104359113A CN 201410611056 A CN201410611056 A CN 201410611056A CN 104359113 A CN104359113 A CN 104359113A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/05—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste oils
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/10—Liquid waste
- F23G2209/102—Waste oil
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/14—Gaseous waste or fumes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
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- General Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Incineration Of Waste (AREA)
Abstract
The invention discloses a waste gas and waste liquid incineration system. The system comprises oxygen production equipment, a local oxygen increasing, combustion and mixing chamber, a primary incineration chamber, a secondary catalytic incineration chamber, an air heat exchanger and a waste heat utilization and smoke purification device which are sequentially connected; harmful waste gas or atomized waste liquid, compressed air and pure oxygen are proportionally mixed in the mixing chamber and then are fed into the primary incineration chamber for incineration. The waste gas and waste liquid incineration system has the advantages that the content of oxygen is locally improved in the primary incineration chamber for waste gas and waste liquid, the combustion speed is accelerated, the complete combustion is facilitated, the smoke exhaust amount after combustion is reduced, and the heat utilization ratio is improved; smoke after primary incineration enters the secondary catalytic incineration chamber and reacts with catalyst, toxic gases such as ammonia and hydrogen cyanide produced after primary incineration is decomposed into N2, H2 and CO2, the problem of environmental pollution caused by smoke exhaust is solved, and the energy saving and emission reduction are facilitated.
Description
Technical field
The present invention relates to the energy-efficient treatment equipment of a kind of waste gas, waste liquid environmental protection burning, be related specifically to a kind of waste gas, liquid waste incineration system and method.
Background technology
China is the emerging nation of high speed development, and the proportion that resource consumption, pollutant emission account for the whole world is increasing.Development resource economizing type, environment friendly economy will become the Main way of the national economic development from now on, and low-carbon economy becomes the prevailing model of China's economic development from now on.
China is in industrial processes, create a large amount of waste water,waste gas and industrial residue, wherein major part is that chemical disintoxication and biodegradation mode process, and most administering method essence is a kind of concentration technique, solid, semisolid, mud or liquid after concentrated, its toxicity is growing on and on.Traditional landfill, pond, earth's surface, discarded stacking method, as final disposal, cause the accidents such as water body severe contamination to occur repeatedly.Therefore incineration treatment method, has many irreplaceable advantages.When burning waste liquid, first by Waste liquid atomization, after then mixing with air, pass into high temperature incineration in Burning Room.The flue gas produced after burning carries out heat recovery by passing into waste heat boiler after settlement treatment, enters air finally by the flue gas after heat recovery after purified treatment.
The burning facility quantity that current China is relevant is increasing rapidly, and the administration of energy conservation of burning disposal, pollutant emission management, safety management problem also become increasingly conspicuous, and carry out the energy-saving and emission-reduction of waste gas, waste fluid burning plant, tool is of great significance.
Summary of the invention
The research emphasis of current energy-saving and emission-reduction is that the number of times by increasing energy exchange reaches energy regenerating high as far as possible more, namely makes last gas temperature of discharging more low better; And the research reducing toxic emission is also conceived to eliminate or reduce toxic and harmful more.And the inventor of this patent is by thinking after great many of experiments and deep thought: in waste gas and waste liquid burning disposal process, non-harmful gas, as the nitrogen in air, substantially do not participate in combustion-supporting at burning process, and proportion is very high again in atmosphere, so a large amount of heats can be taken away when discharging, thus, by suitably reducing the ratio of the non-combustion-supporting gas such as nitrogen, carbon dioxide in air, thus greatly reduce last flue gas discharge rate, and then energy ezpenditure during reduction liquid waste incineration process, or improve the organic efficiency of heat energy.
For solving the problem, a kind of waste gas of the present invention, liquid waste incineration system comprise: the oxygen generating plant connected successively, local oxygen-enriched air combustion mixing chamber, Burning Room, quadric catalysis Burning Room, air heat exchanger, UTILIZATION OF VESIDUAL HEAT IN and a smoke eliminator; Harmful waste gas or the waste liquid of atomization, compressed air pass in a Burning Room after mixing in setting ratio in described mixing chamber with pure oxygen and carry out burning disposal.
Further, described waste gas, liquid waste incineration system comprise Waste liquid atomization device, and atomising device is connected with air compression plant.
Further, the air intlet of described air heat exchanger is connected with oxygenating blower fan, and the air outlet slit of heat exchanger is connected with a Burning Room and quadric catalysis Burning Room by pipeline.
Further, described UTILIZATION OF VESIDUAL HEAT IN and smoke eliminator comprise the waste heat boiler, alkali liquid washing device, mist water separator, air-introduced machine and the aiutage that are connected successively.
Further, a described Burning Room and/or quadric catalysis Burning Room are provided with spiral dry method slag-tapping system, described spiral dry method slag-tapping system comprises Water cooling jacket type and goes out slag bath and spiral slag remover, wherein, Water cooling jacket type goes out slag bath and comprises slag catcher and water jacket, slag catcher is arranged in water jacket, and the cooling water in water jacket surrounds the outer wall of slag catcher; Run through in slag catcher and be provided with spiral slag remover, the alkaline residue salt slag that incinerator produces enters in slag catcher after water jacket cooling, is carried discharge by spiral slag remover.
A method for waste gas, liquid waste incineration, specifically comprises the steps:
1) waste liquid of waste gas or atomization, compressed air and oxygen are mixed in mixing chamber, wherein, the ratio of oxygen and air is 1:10-1:25;
2) mist that step 1) produces is inputted in a Burning Room and carries out a burning disposal; Temperature: 750-850 DEG C, flue gas is in once indoor holdup time 1.5-2 second;
3) by step 2) carry out quadric catalysis burning disposal in the flue gas that produces input quadric catalysis Burning Room; Wherein incineration temperature is 1100-1150 DEG C of holdup time 2-4 second;
4) flue gas that step 3) produces is carried out air heat-exchange process, the flue-gas temperature after heat exchange is 800-850 DEG C;
5) flue gas after heat exchange process is passed into waste heat boiler and carry out waste heat recovery, then discharge after purified treatment.
Under the state that auxiliary fuel addition is constant, the oxygen of 1/25 ~ 1/10 is added in compressed air, the oxygen content in air is made to reach 25-28%, the temperature of Burning Room can improve about 100-200 DEG C, add the air capacity also corresponding minimizing 20 ~ 47.6% in waste liquid waste gas combustion furnace in addition, oxygen enrichment improves heat transfer efficiency in waste gas and waste liquid incinerator after burning, simultaneously, because the air capacity participating in burning reduces, the input quantity also corresponding minimizing 20 ~ 47.6% of the nitrogen in air, after burning, the nitrogen of discharging in flue gas reduces with it in proportion, and then the heat also corresponding reduction to be slatterned by fume emission.
Air capacity in addition because entering a Burning Room reduces, CO in flame
2with H
2the volume by volume concentration of O raises.The blackness also corresponding increase of flame.When the oxygen content in secondary combustion air is 25%, CO
2concentration expressed in percentage by volume bring up to about 17%, the corresponding raising 17% of concentration expressed in percentage by volume of water vapour, due to CO
2with H
2the concentration of O all increases, and the corresponding increase of blackness of flame, illustrates that the C in waste gas or waste liquid is fully burned.The toxic gases such as carbon monoxide, nitric oxide and other sour gas also corresponding inverse proportion reduce, and cause new pollution when avoiding liquid waste incineration process to air.
And when the concentration of oxygen in air is 21%, the blackness of flame calculates 0.210, when the concentration of oxygen in air is 25%, the blackness of flame is calculated as 0.224, the degree about 6.7% of increase, and flame passes through the degree that the radiant heat transfer amount of the waste liquid burned, waste gas improves and is calculated as 20%, improve the oxygen concentration required for incinerator, the organic matter in incinerator can be made to be more prone to ignition, and furnace temperature rises, and is more prone to after-flame, fully.Flue dust changes into heat energy in oxygen enrichment.
Further, in described step 1), waste liquid passes into mixing chamber by mixing with compressed air after high-pressure atomization, and compressed-air actuated design pressure is 0.2-0.3MPa; Often liter of atomization waste liquid uses compressed-air actuated ratio for 0.5-1Nm
3/ L; Waste gas passes into mixing chamber after being mixed with air or oxygen by waste gas nozzle, and the pressure design of waste gas nozzle is 1KPa.
Further, the gas used of the air heat-exchange process in described step 4) is air, and this air inputs a Burning Room and quadric catalysis Burning Room respectively after heat exchange process; Inputting two Burning Room Airflow amounts is do the chain control of frequency conversion according to the online Control for Oxygen Content instrument of secondary burning room and oxygenating blower fan, and the oxygen content of secondary burning room is controlled at 6-10%.
Further, described quadric catalysis burns catalyst used and is
946ammonia decomposition catalyzer.
Residual harmful smoke enters secondary high-temperature Burning Room, and ignition temperature can reach more than 1100 DEG C, and flue gas, more than the 2 seconds time of staying that quadric catalysis burns, guarantees that the waste gas and waste liquid entering CIU burns fully thoroughly completely.Through dual firing chamber, clean-burning high-temperature flue gas sends into flue gas waste heat recovery and flue gas controller.
Further, purified treatment described in step 6) comprises alkali liquid washing, fog is separated.
Further, the calorific value of described waste liquid is: 100-10000Kcal/kg, and waste liquid COD concentration is 50000-2000000mg/l.
Further, the processing speed of described waste gas or atomization waste liquid is 50-10000kg/h, is preferably 50-5000kg/h.
The content of oxygen is improved in patent of the present invention local in waste gas, waste liquid incinerator, accelerates burning velocity and promotes to burn completely, reduces the flue gas exhaust amount after burning, increases heat utilization ratio; Flue gas after once burning enters quadric catalysis Burning Room and catalyst reaction, and the toxic gas such as ammonia, hydrogen cyanide once burning rear generation is resolved into N
2, H
2, CO
2, solve fume emission environmental pollution, be conducive to energy-saving and emission-reduction.
Accompanying drawing explanation
Fig. 1-1 is the structural representation once burning part of the present invention;
Fig. 1-2 is the structural representation of quadric catalysis burning part of the present invention;
Fig. 1-3 is the structural representation of UTILIZATION OF VESIDUAL HEAT IN and smoke eliminator;
Fig. 2 is equipment connecting relation of the present invention and process method flow chart.
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described.
embodiment 1
As shown in Figure 1-2, in the present embodiment, a kind of waste gas, liquid waste incineration system comprise: the oxygen generating plant connected successively, local oxygen-enriched air combustion mixing chamber, Burning Room, quadric catalysis Burning Room, air heat exchanger, UTILIZATION OF VESIDUAL HEAT IN and a smoke eliminator; Harmful waste gas or the waste liquid of atomization, compressed air pass in a Burning Room after mixing in setting ratio in described mixing chamber with pure oxygen and carry out burning disposal.UTILIZATION OF VESIDUAL HEAT IN and smoke eliminator comprise the waste heat boiler, alkali liquid washing device, mist water separator, air-introduced machine and the aiutage that are connected successively.
Waste gas, liquid waste incineration system comprise Waste liquid atomization device, and atomising device is connected with air compression plant.
The air intlet of air heat exchanger is connected with oxygenating blower fan, and the air outlet slit of heat exchanger is connected with a Burning Room and quadric catalysis Burning Room respectively by pipeline and flow control valve.Control for Oxygen Content instrument is provided with in quadric catalysis Burning Room.Waste gas, liquid waste incineration system comprise intelligent controller, and controller is connected with oxygen content controller, flow control valve and oxygenating blower fan.The switch that controller controls oxygenating blower fan and the air mass flow inputting two Burning Rooms respectively make the oxygen content of quadric catalysis Burning Room control at 6-10%.
Proved through great many of experiments, oxygen content in quadric catalysis Burning Room is controlled can realize optimum marginal benefit at 6-10%.And under the prerequisite not promoting oxygen content, production cost is controlled in rational scope, simultaneously by arranging catalyst layer in quadric catalysis Burning Room, make as clean-burning pernicious gas is thoroughly decomposed into harmless molecule, both combinations achieve two optimums of economy and benefit.
The processing speed of the waste gas of the present embodiment, the waste gas of liquid waste incineration system or atomization waste liquid is 50-10000kg/h, and optimal processing speed is about 5000kg/h.
In addition, a Burning Room and/or quadric catalysis Burning Room adopt dry method to slag tap, and the salt slag after heat exchange adopts the discharging of spiral dry method slag-tapping system.Spiral dry method slag-tapping system comprises Water cooling jacket type and goes out slag bath and spiral slag remover, and wherein, Water cooling jacket type goes out slag bath and comprises slag catcher and water jacket, and slag catcher is arranged in water jacket, and the cooling water in water jacket surrounds the outer wall of slag catcher; Run through in slag catcher and be provided with spiral slag remover, the alkaline residue salt slag that incinerator produces enters in slag catcher after water jacket cooling, is carried discharge by spiral slag remover.
embodiment 2
A method for waste gas, liquid waste incineration, specifically comprises the steps:
1) waste liquid of waste gas or atomization, compressed air and oxygen are mixed in mixing chamber, wherein, the ratio of oxygen air is 1:25; Wherein, waste liquid passes into mixing chamber after mixing with compressed air after high-pressure atomization, and compressed-air actuated design pressure is 0.2-0.3MPa; Often liter of atomization waste liquid uses compressed-air actuated ratio for 0.5-1Nm
3/ L; If what need burning disposal is waste gas, then waste gas is by passing into mixing chamber after waste gas nozzle and oxygen mix, and the pressure design of waste gas nozzle is 1KPa.
2) mist that step 1) produces is inputted in a Burning Room and carries out a burning disposal; Temperature: 750-850 DEG C, flue gas is in once indoor 2 seconds holdup times;
3) by step 2) carry out quadric catalysis burning disposal in the flue gas that produces input quadric catalysis Burning Room; Wherein incineration temperature is about 3 seconds 1100 DEG C of holdup times;
4) flue gas that step 3) produces is carried out air heat-exchange process, the flue-gas temperature after heat exchange is 800-850 DEG C; Air heat-exchange process gas used is air, inputs a Burning Room and quadric catalysis Burning Room after this air heat-exchange respectively; Inputting two Burning Room Airflow amounts is do the chain control of frequency conversion according to the online Control for Oxygen Content instrument of secondary burning room and oxygenating blower fan, and the oxygen content of two catalytic burning indoor is controlled 8%.
5) flue gas after heat exchange process is passed into waste heat boiler and carry out waste heat recovery, then discharge after the purified treatment such as alkali liquid washing, fog separation.
The calorific value of the waste liquid in the present embodiment is 100-10000Kcal/kg, and waste liquid COD concentration is 50000-2000000mg/l.
In addition, quadric catalysis burns catalyst used and is
946ammonia decomposition catalyzer; Design parameter is as following table.
| Sequence number | Project name | Unit | Parameter |
| 1 | Color | Grey black | |
| 2 | Shape | Nest honeybee shape, Raschig ring shape, column | |
| 3 | Size | mm | ∮18×20 |
| 4 | Nickel content | % | 6 |
| 5 | Bulk density | g/ml | 1.2-1.5 |
| 6 | Specific area | m 2/g | 1-5 |
| 7 | Compression strength | N | 1100 |
| 8 | Resistance to temperature | ℃ | ≥1350 |
The waste gas such as ammonia, hydrogen cyanide that contains that waste gas and waste liquid once burns rear generation enters quadric catalysis combustion chamber, catalyst heat endurance of the present invention is better, intensity is higher, it is poisoning to resist and anticoking capability is more excellent, this catalyst runs under 1000-1200 DEG C of environment, the ammonia in waste gas, hydrogen cyanide pernicious gas is resolved into: N
2, H
2, CO
2, reaction equation is as follows:
NH3 → 0.5 N
2+ 1.5H
2
2HCN + 2H
2O + O
2→ N
2+ 5H
2+ 2CO
2
Residual harmful smoke enters secondary high-temperature Burning Room, and ignition temperature can reach more than 1100 DEG C, and flue gas more than 2 seconds, guarantees that the waste gas and waste liquid entering CIU burns fully thoroughly completely in time of staying of quadric catalysis Burning Room.Through experimental results demonstrate, there is above-mentioned parameter
946ammonia decomposition catalyzer catalytic effect is better, and pernicious gas decomposes more thorough.Further, catalyst is arranged between quadric catalysis Burning Room inner burner and exhanst gas outlet, and the flue gas of discharge is all just discharged after this catalyst layer catalyzes decomposes, and effectively prevent the leakage of pernicious gas.
Flue gas waste heat recovery and flue gas controller is sent into through the two clean-burning high-temperature flue gas in catalytic burning room.
That per kilogram waste gas or waste liquid required air adjust required air capacity according to the calorific value of waste gas or waste liquid in step 1).As needs process high-concentration waste liquid 500kg/h, waste liquid COD concentration is 200000mg/l, is 720Kcal/kg according to formulae discovery waste liquid calorific value, is 2.7Nm according to the calorific value calculation theoretical air requirement of waste liquid
3/ kg, auxiliary fuel adopts natural gas auxiliary combustion.Auxiliary air amount (oxygen content of 21%), excess air coefficient is 1.1, and the calorific value of natural gas is: 8400-8600Kcal/m
3, the air capacity required for every cubic natural gas burns is: 9.52 m
3/ m
3, exhaust gas volumn 10.5 m of generation
3/ m
3, the supplemental heat of the required evaporation of per kilogram liquid waste incineration about: 1000Kcal/kg, burn the amount of natural gas required for waste liquid of 500Kg/h about: 500Kg/h × 1000Kcal/kg ÷ 8600Kcal/m
3=59.52m
3; The waste liquid additional natural gas burning 500Kg/h burns required air capacity and is: 9.52 m
3/ m
3× 59.52m
3× 1.1=623.3m
3/ h; The waste liquid additional natural gas burning 500Kg/h burns generation exhaust gas volumn and is: 10.5 m
3/ m
3× 59.52m
3=624.96 m
3/ h; Air capacity required for 500Kg/h liquid waste incineration: V=500Kg/h × 2.7 Nm
3/ kg × 1.1=1485Nm
3/ h;
Oxygen amount 21% (air capacity: 623.3Nm in air required for 500Kg/h liquid waste incineration
3/ h+1485Nm
3/ h=2108.3 Nm
3/ h), pure oxygen content now: 442.74Nm
3/ h; The concentration of the oxygen content when burning 500Kg/h waste liquid in air brings up to 25%(pure oxygen amount: 527Nm
3/ h) time, required supplementary air capacity 1770.96Nm
3/ h.
When burning 500Kg/h waste liquid, the concentration of oxygen content is brought up to 25% and is decreased air capacity about 16%, enters the N of Burning Room
2amount correspondingly have dropped 16-20%, total flue gas volume of liquid waste incineration room is declined, under the state that auxiliary fuel addition is constant, when the oxygen content in air reaches 25%, through adjusting, the temperature of Burning Room improves about 100 DEG C, and the air capacity added in waste liquid waste gas combustion furnace reduces, and improves the thermal efficiency total in waste gas and waste liquid incinerator after improving oxygen content.
Under the state that auxiliary fuel addition is constant, the oxygen of 1/25 ~ 1/10 is added in compressed air, the oxygen content in air is made to reach 25-28%, the temperature of Burning Room can improve about 100-200 DEG C, add the air capacity also corresponding minimizing 20 ~ 47.6% in waste liquid waste gas combustion furnace in addition, oxygen enrichment improves heat transfer efficiency in waste gas and waste liquid incinerator after burning, simultaneously, because the air capacity participating in burning reduces, the input quantity also corresponding minimizing 20 ~ 47.6% of the nitrogen in air, after burning, the nitrogen of discharging in flue gas reduces with it in proportion, and then the heat also corresponding reduction to be slatterned by fume emission.
Inventor finds through great many of experiments and after summing up, oxygen and compressed-air actuated proportioning marginal cost between 1/25 ~ 1/10 minimum, marginal benefit is maximum, when oxygen blending ratio is more than 28%, the security performance of system can significantly reduce, and production cost also can significantly rise thereupon.
Below only describe several preferred embodiments of the application by reference to the accompanying drawings, but the application is not limited thereto, every those of ordinary skill in the art are under the spirit not departing from the application, and any improvement made and/or distortion, all belong to the protection domain of the application.
Claims (10)
1. a method for waste gas, liquid waste incineration, is characterized in that, it specifically comprises the steps:
1) waste liquid of waste gas or atomization, compressed air and oxygen are mixed in mixing chamber, wherein, the ratio of oxygen and air is 1:10-1:25;
2) mist that step 1) produces is inputted in a Burning Room and carries out a burning disposal; Temperature: 750-850 DEG C, flue gas is in once indoor holdup time 1.5-2 second;
3) by step 2) carry out quadric catalysis burning disposal in the flue gas that produces input quadric catalysis Burning Room; Wherein incineration temperature is 1100-1150 DEG C of holdup time 2-4 second;
4) flue gas that step 3) produces is carried out air heat-exchange process, the flue-gas temperature after heat exchange is 800-850 DEG C;
5) flue gas after heat exchange process is passed into waste heat boiler and carry out waste heat recovery, then discharge after purified treatment.
2. the method for waste gas, liquid waste incineration as claimed in claim 1, it is characterized in that, in described step 1), waste liquid passes into mixing chamber by mixing with compressed air after high-pressure atomization, and compressed-air actuated design pressure is 0.2-0.3MPa; Often liter of atomization waste liquid uses compressed-air actuated ratio for 0.5-1Nm
3/ L; Waste gas passes into mixing chamber after being mixed with air or oxygen by waste gas nozzle, and the pressure design of waste gas nozzle is 1KPa.
3. the method for waste gas, liquid waste incineration as claimed in claim 1, is characterized in that, the gas used of the air heat-exchange process in described step 4) is air, and this air inputs a Burning Room and quadric catalysis Burning Room respectively after heat exchange process; Inputting two Burning Room Airflow amounts is do the chain control of frequency conversion according to the online Control for Oxygen Content instrument of secondary burning room and oxygenating blower fan, and the oxygen content of secondary burning room is controlled at 6-10%.
4. the method for waste gas, liquid waste incineration as claimed in claim 1, it is characterized in that, described quadric catalysis burns catalyst used and is
946ammonia decomposition catalyzer.
5. the method for waste gas, liquid waste incineration as claimed in claim 1, is characterized in that, purified treatment described in described step 6) comprises alkali liquid washing, fog is separated.
6. waste gas, a liquid waste incineration system, it is characterized in that, it comprises: the oxygen generating plant connected successively, local oxygen-enriched air combustion mixing chamber, Burning Room, quadric catalysis Burning Room, air heat exchanger, UTILIZATION OF VESIDUAL HEAT IN and a smoke eliminator; Harmful waste gas or the waste liquid of atomization, compressed air pass in a Burning Room after mixing in setting ratio in described mixing chamber with pure oxygen and carry out burning disposal.
7. CIU as claimed in claim 6, it is characterized in that, described waste gas, liquid waste incineration system comprise Waste liquid atomization device, and atomising device is connected with air compression plant.
8. CIU as claimed in claim 6, it is characterized in that, the air intlet of described air heat exchanger is connected with oxygenating blower fan, and the air outlet slit of heat exchanger is connected with a described Burning Room and quadric catalysis Burning Room by pipeline.
9. CIU as claimed in claim 6, it is characterized in that, described UTILIZATION OF VESIDUAL HEAT IN and smoke eliminator comprise the waste heat boiler, alkali liquid washing device, mist water separator, air-introduced machine and the aiutage that are connected successively.
10. CIU as claimed in claim 6, it is characterized in that, a described Burning Room and/or quadric catalysis Burning Room are provided with spiral dry method slag-tapping system, described spiral dry method slag-tapping system comprises Water cooling jacket type and goes out slag bath and spiral slag remover, wherein, Water cooling jacket type goes out slag bath and comprises slag catcher and water jacket, and slag catcher is arranged in water jacket, and the cooling water in water jacket surrounds the outer wall of slag catcher; Run through in slag catcher and be provided with spiral slag remover, the alkaline residue salt slag that incinerator produces enters in slag catcher after water jacket cooling, is carried discharge by spiral slag remover.
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| CN106556004A (en) * | 2016-11-23 | 2017-04-05 | 东莞市东燃热能科技有限公司 | A kind of method that NOx emission control is reduced during firing biomass fuel |
| CN107044646A (en) * | 2017-03-24 | 2017-08-15 | 马鞍山市人智能环保科技有限公司 | A kind of liquid waste treatment system and its processing method |
| CN107642785A (en) * | 2017-06-21 | 2018-01-30 | 太仓隆尹机电有限公司 | Waste combustion processing system and equipment |
| CN109442438A (en) * | 2018-10-24 | 2019-03-08 | 江苏大信环境科技有限公司 | The comprehensive processing technique and system of a kind of organic exhaust gas containing ammonia and the organic wastewater containing ammonia |
| CN111306549A (en) * | 2020-02-25 | 2020-06-19 | 南京航空航天大学 | Green and efficient rotary kiln incineration treatment method for hazardous wastes based on oxygen-enriched air supply of secondary combustion chamber |
| CN112313177A (en) * | 2019-05-28 | 2021-02-02 | 株式会社Lg化学 | Waste water incineration method and waste water incineration apparatus |
| CN112313451A (en) * | 2019-05-28 | 2021-02-02 | 株式会社Lg化学 | Method and apparatus for incinerating waste water |
| CN114151806A (en) * | 2021-11-30 | 2022-03-08 | 山东蓝天新材料科技有限公司 | Color coating curing waste gas treatment device and system |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6436337B1 (en) * | 2001-04-27 | 2002-08-20 | Jupiter Oxygen Corporation | Oxy-fuel combustion system and uses therefor |
| RU2004138107A (en) * | 2004-12-27 | 2006-06-10 | Военна академи Ракетных войск стратегического назначени им. Петра Великого (RU) | METHOD OF AFTERBURNING OF COMPLETE COMBUSTION PRODUCTS DURING DISPOSAL OF ROCKET ENGINES OF SOLID FUELS |
| CN201363733Y (en) * | 2009-01-19 | 2009-12-16 | 袁永扬 | Integrated processing equipment for rubbish high-temperature incineration |
| CN101825285A (en) * | 2010-05-17 | 2010-09-08 | 北京航天动力研究所 | Burning treatment method and device for organic waste water containing salt |
| CN102198365A (en) * | 2011-05-11 | 2011-09-28 | 北京丰汉工程咨询有限公司 | Processing method of acid gas |
| CN102644922A (en) * | 2012-04-20 | 2012-08-22 | 天津辰创环境工程科技有限责任公司 | Incineration treatment device for nitrogen-containing organic wastes and incineration treatment process |
| CN204254633U (en) * | 2014-11-04 | 2015-04-08 | 宜兴市智博环境设备有限公司 | A kind of waste gas, liquid waste incineration system |
-
2014
- 2014-11-04 CN CN201410611056.0A patent/CN104359113B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6436337B1 (en) * | 2001-04-27 | 2002-08-20 | Jupiter Oxygen Corporation | Oxy-fuel combustion system and uses therefor |
| RU2004138107A (en) * | 2004-12-27 | 2006-06-10 | Военна академи Ракетных войск стратегического назначени им. Петра Великого (RU) | METHOD OF AFTERBURNING OF COMPLETE COMBUSTION PRODUCTS DURING DISPOSAL OF ROCKET ENGINES OF SOLID FUELS |
| CN201363733Y (en) * | 2009-01-19 | 2009-12-16 | 袁永扬 | Integrated processing equipment for rubbish high-temperature incineration |
| CN101825285A (en) * | 2010-05-17 | 2010-09-08 | 北京航天动力研究所 | Burning treatment method and device for organic waste water containing salt |
| CN102198365A (en) * | 2011-05-11 | 2011-09-28 | 北京丰汉工程咨询有限公司 | Processing method of acid gas |
| CN102644922A (en) * | 2012-04-20 | 2012-08-22 | 天津辰创环境工程科技有限责任公司 | Incineration treatment device for nitrogen-containing organic wastes and incineration treatment process |
| CN204254633U (en) * | 2014-11-04 | 2015-04-08 | 宜兴市智博环境设备有限公司 | A kind of waste gas, liquid waste incineration system |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106482131A (en) * | 2015-08-24 | 2017-03-08 | 中石化洛阳工程有限公司 | A kind of wastewater treatment field waste gas processing method |
| CN105423315A (en) * | 2015-11-23 | 2016-03-23 | 翟树军 | Method for recycling vented waste gases generated in coal chemical industry |
| CN106556004B (en) * | 2016-11-23 | 2019-03-26 | 东莞东燃热能科技股份有限公司 | A kind of method that firing biomass fuel reduces NOx emission control in the process |
| CN106556004A (en) * | 2016-11-23 | 2017-04-05 | 东莞市东燃热能科技有限公司 | A kind of method that NOx emission control is reduced during firing biomass fuel |
| CN107044646A (en) * | 2017-03-24 | 2017-08-15 | 马鞍山市人智能环保科技有限公司 | A kind of liquid waste treatment system and its processing method |
| CN107642785A (en) * | 2017-06-21 | 2018-01-30 | 太仓隆尹机电有限公司 | Waste combustion processing system and equipment |
| CN109442438A (en) * | 2018-10-24 | 2019-03-08 | 江苏大信环境科技有限公司 | The comprehensive processing technique and system of a kind of organic exhaust gas containing ammonia and the organic wastewater containing ammonia |
| CN112313177A (en) * | 2019-05-28 | 2021-02-02 | 株式会社Lg化学 | Waste water incineration method and waste water incineration apparatus |
| CN112313451A (en) * | 2019-05-28 | 2021-02-02 | 株式会社Lg化学 | Method and apparatus for incinerating waste water |
| CN112313451B (en) * | 2019-05-28 | 2023-03-10 | 株式会社Lg化学 | Method and apparatus for incinerating waste water |
| US11851348B2 (en) | 2019-05-28 | 2023-12-26 | Lg Chem, Ltd. | Waste water incinerating method and apparatus therefor |
| US11946642B2 (en) | 2019-05-28 | 2024-04-02 | Lg Chem, Ltd. | Waste water incineration method and apparatus for the same |
| CN111306549A (en) * | 2020-02-25 | 2020-06-19 | 南京航空航天大学 | Green and efficient rotary kiln incineration treatment method for hazardous wastes based on oxygen-enriched air supply of secondary combustion chamber |
| CN114151806A (en) * | 2021-11-30 | 2022-03-08 | 山东蓝天新材料科技有限公司 | Color coating curing waste gas treatment device and system |
| CN114151806B (en) * | 2021-11-30 | 2024-03-12 | 山东蓝天新材料科技有限公司 | Color-coating curing waste gas treatment device and system |
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