CN102644922B - Incineration treatment device for nitrogen-containing organic wastes and incineration treatment process - Google Patents
Incineration treatment device for nitrogen-containing organic wastes and incineration treatment process Download PDFInfo
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- CN102644922B CN102644922B CN201210118586.2A CN201210118586A CN102644922B CN 102644922 B CN102644922 B CN 102644922B CN 201210118586 A CN201210118586 A CN 201210118586A CN 102644922 B CN102644922 B CN 102644922B
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Abstract
The invention discloses an incineration treatment process for nitrogen-containing organic wastes, which includes: a, sending wastes into an incinerator to incinerate at a high temperature and maintaining the incineration temperature by injecting after-burning fuel; b, injecting combustion-supporting air which is divided into primary air and secondary air according to a certain proportion into a fire chamber for supporting combustion; c, injecting reducing agents to the tail of a hot oxidation furnace and reducing part of NOx in flue gas by the SNCR (selective non-catalytic reduction) method; d, leading high-temperature flue gas from the hot oxidation furnace into a waste heat boiler to recover part of heat; e, leading the flue gas from the waste heat boiler into an SCR(selective catalytic reduction) treater to reduce content of NOx in flue gas further; and f, further recovering afterheat of flue gas by the aid of an air preheater arranged at the downstream of the SCR treater and then discharging flue gas through a chimney. The incineration treatment process is simple and low in cost for incineration of organic wastes, denitration efficiency can be guaranteed by a two-stage denitration process, emission standards can be met, afterheat of flue gas can be recovered, and accordingly the incineration treatment process can be applied to the similar organic waste treatment projections in the chemical industry.
Description
Technical field
The invention belongs to the treatment technology of chemical industry nitrogenouz wastes, particularly relate to and a kind ofly will there is the debirs burning disposal of certain calorific value, and take denitration method for flue gas to remove NOx, make flue gas qualified discharge.
Background technology
Because the mankind expect that to industrial negative effect it is unfavorable to prevent, and has caused three global large crises: shortage of resources, environmental pollution, ecological disruption not.The mankind are constantly to environmental emission polluter.When the material of discharge has exceeded the self-purification capacity of environment, will there is disadvantageous changes in environmental quality, the healthy and existence of harm humans, and just there is environmental pollution in this.Environmental pollution meeting causes direct destruction and impact to the ecosystem, as desertification, forest deterioration, also cause indirectly harm can to the ecosystem and human society, sometimes the direct harm that the hazard ratio of this indirectly environmental effect caused is at that time larger, also more difficult elimination.For example, greenhouse effects, acid rain and depletion of the ozone layer are exactly the environmental effect being derived by atmosphere pollution.In Chemical Manufacture, the organic wastewater waste gas of discharge etc. adopt incinerating method conventionally, can be by debirs high-temperature oxydation, be decomposed into water and carbon dioxide, reduce the direct destruction of refuse to environment, also can pollute atmosphere but the discharged nitrous oxides that burning method produces is excessive, it is the main cause that causes acid rain and photochemical fog.Therefore there is strict restriction countries in the world to the discharge of nitrogen oxide in industrial production.How effectively by debirs pyrolytic, and take certain measure to reduce the discharge of nitrogen oxide, be during refuse is processed, to be devoted to the problem that solves always.
At present at home in debirs burning disposal industry, because of the variation of refuse kind, selection and layout for burner are difficult problems, often occur that atomization is insufficient, easily stop up, burner hearth flow field and temperature field skewness, cause organic matter not decompose completely, and thermal NO produces more.And exist to adopt in the flue gas of discharge and mix air or only adopt the method for single selective oxidation reduction to reduce the problems such as the concentration of emission efficiency of nitrogen oxide is not high.
Summary of the invention
For prior art, the invention provides a kind of incineration treatment technology of nitrogenous debirs, by nitrogenous organic exhaust gas and waste water, the burner by reasonable Arrangement and spray gun spray into combustion decomposition in the thermal oxidation furnace burner hearth of particular design to this technique, in flue gas is processed, adopt SNCR (SNCR) and SCR (SCR) two stages for the treatment of method effectively to reduce the nitrogen oxide in flue gas, and in technique, be provided with the heat of waste heat boiler and air preheater recovered flue gas.Both process debirs, controlled the amount that enters the pollutant in atmosphere, reclaimed again a part of heat energy, realized the object of energy-saving and emission-reduction.
In order to solve the problems of the technologies described above, the present invention for the structure of the incinerating and treating device of nitrogenous debirs is: comprise burner, thermal oxidation furnace, waste heat boiler, SCR SCR processor, air preheater, air-introduced machine, chimney and a furnace pressure control loop of series connection successively, described furnace pressure control loop comprises that a pressure-measuring-point that is arranged on described thermal oxidation furnace furnace front forms with the variable-frequency motor being connected with described air-introduced machine; The afterbody of described thermal oxidation furnace (2) is provided with a SNCR SNCR processor, described SNCR SNCR processor is in series with a blender A and a dilution air A, described SCR SCR processor is in series with a blender B and a dilution air B, and described blender A and blender B are for entering respectively described SCR SCR processor and SNCR SNCR processor after diluent air and ammonia mixing; Also comprise a combustion fan and combustion air house steward, the exhaust outlet of described combustion fan is connected with described air preheater, connect with air preheater in described combustion air house steward's upstream, described combustion air house steward's downstream is connected to respectively described burner and described thermal oxidation furnace by a threeway; Also comprise injection apparatus, described injection apparatus comprises the central lance that needs postcombustion for spraying maintaining heat oxidation furnace incineration temperature that is arranged on center in described burner, for spray the ring-type spray gun of waste gas to thermal oxidation furnace, according to atomizing nozzle and the medium atomization nozzle on the headwall of described thermal oxidation furnace, spray waste water for flame region in thermal oxidation furnace of being circular layout; Also comprise two temperature points, two flowmeters and three flue gas measuring points, described three flue gas measuring points comprise the first flue gas measuring point, the second flue gas measuring point and the 3rd flue gas measuring point, above-mentioned each measuring point coordinates and forms multiple control loops to relevant control valve.
The present invention carries out the technique of burning disposal to nitrogenous debirs, be to adopt above-mentioned incinerating and treating device, and its burning disposal comprises the following steps:
A. be gaseous state or liquid state according to refuse, adopt suitable injection apparatus to be sent into and in thermal oxidation furnace, carry out high temperature incineration; The fuel of afterburning adopts central lance to spray in the burner hearth of thermal oxidation furnace; In high temperature incineration process, by controlling incineration temperature in described thermal oxidation furnace burner hearth at 900～1200 ℃ by being arranged on the temperature point at burner hearth rear portion of described thermal oxidation furnace and temperature control loop TIC01 that fuel control valve forms; After incineration of waste, the flue-gas temperature that the temperature control loop TIC02 control forming by another temperature point and cooling sea water regulating valve enters SNCR reactor is 900～1050 ℃;
B. combustion air provides by combustion fan, the total amount of combustion air is to utilize by the variable-frequency motor being connected with combustion fan and be arranged on the control loop AIC03 that the 3rd flue gas measuring point on chimney forms to control, oxygen content in the flue gas collecting according to the 3rd flue gas measuring point is as parameter, regulate the frequency of frequency conversion fan, thereby control the flow of the combustion air that enters combustion air house steward, first the air of discharging from combustion fan outlet enters air preheater preheating, and the air after preheating is divided into wind and Secondary Air by a certain percentage, and to enter the burner hearth of thermal oxidation furnace combustion-supporting, connecting line between described combustion fan and described burner is a wind branched pipe, connecting line between described combustion fan and described thermal oxidation furnace is Secondary Air arm, form a control loop FIC01-02 by two two flowmeters that are separately positioned on described combustion air main pipe rail and a wind branched pipe with the volume damper being arranged on a wind branched pipe, the flow that this control loop FIC01-02 controls a wind accounts for 60～80% of total air mass flow, according to the numerical value of the flowmeter on wind branched pipe of setting parameter of combustion air main pipe rail flowmeter, enter the amount of the combustion air of burner with control by this control loop of the Flow-rate adjustment FIC01-02 on a wind branched pipe, adopt segmentation air distribution to reduce combustion zone temperature, thereby the generation of thermal NO x in minimizing combustion process,
C. the reaction temperature of controlling SNCR SNCR processor is 900～1050 ℃, spray into reducing agent in SNCR SNCR processor before, control the flow realization of the cooling water that enters thermal oxidation furnace by temperature control loop TIC02 flue gas is lowered the temperature, guarantee the flue-gas temperature that enters SNCR SNCR processor; The ammonia import department of described blender A is provided with the first air inlet adjustment valve, the flue gas pipeline of described SNCR SNCR processor is provided with the first flue gas measuring point, and the first air inlet adjustment valve and described the first flue gas measuring point form the control loop AIC01 that enters the reducing agent flow of conversion zone in described SNCR SNCR reactor in order to control; Spray into the conversion zone of SNCR SNCR processor the reducing agent that the mist of ammonia below 5% concentration and air forms by blender A, the flow that the amount of this reducing agent detects the NOx in flue gas by control loop AIC01 is controlled, and the method that adopts SNCR (SNCR) is first reduced to N by 30～70% NOx in flue gas
2and O
2:
D. enter waste heat boiler from thermal oxidation furnace high-temperature flue gas out through SNCR SNCR reactor and carry out the recovery of part heat, and produce steam, thereby waste heat boiler outlet temperature is reduced to below 400 ℃;
The flue gas of e. discharging from waste heat boiler enters SCR SCR processor, wherein, reducing agent adopts ammonia below 5% concentration and the mist of air, the flow that the amount of this reducing agent detects the NOx in flue gas by control loop AIC02 is controlled, and adopts the method for SCR (SCR) that the NOx in flue gas is reduced to N
2and O
2thereby, make flue gas reach the discharge standard of NOx;
F., the waste heat of the further recovered flue gas of air preheater is set in SCR SCR processor downstream;
G. be admitted to chimney and discharge by air-introduced machine from air preheater flue gas out.
Further, in above-mentioned steps a, if refuse is waste gas, adopt ring-type spray gun waste gas to be sprayed in the burner hearth of thermal oxidation furnace; If refuse is waste liquid, select according to the character of this waste liquid multiple mechanical atomizations or the medium atomization nozzle arranged in the form of a ring, waste liquid is sprayed into the burner hearth flame of centre region of thermal oxidation furnace.
Further, in above-mentioned steps a, when the refuse of burning disposal is while not belonging to the debirs of hazardous waste, its incineration temperature is 900～1100 ℃, and in the time of debirs that the refuse of burning disposal is hazardous waste, its incinerator bore temperature is 1100～1200 ℃.
Compared with prior art, the invention has the beneficial effects as follows:
By the research to nitrogenous organic exhaust gas and wastewater property, select suitable shower nozzle, and by the position of reasonable Arrangement burner and spray gun, that fuel and waste water and gas spray into combustion decomposition in the thermal oxidation furnace burner hearth of particular design, combustion air is divided into according to a certain percentage wind and Secondary Air and enters burner hearth and help so, burner hearth flow field and uniform distribution of temperature field, there is not dead band, debirs can fully decompose, and combustion air point the two poles of the earth enter burner hearth, effectively reduce the temperature in flame kernel district, greatly reduce the generation of thermal NO, reduce the pressure of denitrification apparatus during flue gas is processed.
In processing, denitrating flue gas adopt SNCR (SNCR) and SCR (SCR) two stages for the treatment of method effectively to reduce the nitrogen oxide in flue gas, for the not high project of NOx concentration in flue gas, domestic SCR denitrification apparatus be can adopt, cost of investment and operating cost reduced.And in technique, be provided with the heat of waste heat boiler and air preheater recovered flue gas.
Technological process of the present invention is simple, has both processed debirs, has controlled the amount that enters the pollutant in atmosphere, has reclaimed again a part of heat energy, has realized the object of energy-saving and emission-reduction, can be widely used in this type of refuse processing project of chemical industry.
Accompanying drawing explanation
Accompanying drawing is the nitrogenous debirs processing technological flow of the present invention figure.
The specific embodiment
Below in conjunction with accompanying drawing, the present invention is described in further detail.
As shown in drawings, the present invention is for the incinerating and treating device of nitrogenous debirs, comprise burner 1, thermal oxidation furnace 2, waste heat boiler 4, SCR SCR processor 5, air preheater 6, air-introduced machine 7, chimney 8 and a furnace pressure control loop of series connection successively, described furnace pressure control loop comprises that a pressure-measuring-point that is arranged on described thermal oxidation furnace 2 furnace fronts forms with the variable-frequency motor being connected with described air-introduced machine 7, regulate the frequency of id-motor by this pressure-measuring-point, thereby guarantee that burner hearth has certain negative pressure.The afterbody of described thermal oxidation furnace 2 is provided with a SNCR SNCR processor 3, described SNCR SNCR processor 3 is in series with a blender A11 and a dilution air A10, described SCR SCR processor 5 is in series with a blender B13 and a dilution air B12, and described blender A11 and blender B13 are for entering respectively described SCR SCR processor 5 and SNCR SNCR processor 3 after diluent air and ammonia mixing.
In incinerating and treating device of the present invention, also comprise a combustion fan 9 and combustion air house steward 14, the exhaust outlet of described combustion fan 9 is connected with described air preheater 6, connect with air preheater 6 in described combustion air house steward's 14 upstream, described combustion air house steward's 15 downstream is connected to respectively described burner 1 and described thermal oxidation furnace 2 by a threeway;
In incinerating and treating device of the present invention, also comprise injection apparatus, described injection apparatus comprises the central lance that needs postcombustion for spraying maintaining heat oxidation furnace 2 incineration temperatures that is arranged on center in described burner, for spray the ring-type spray gun of waste gas to thermal oxidation furnace 2, according to atomizing nozzle and the medium atomization nozzle on the headwall of described thermal oxidation furnace 2, spray waste water for flame region in thermal oxidation furnace of being circular layout;
In incinerating and treating device of the present invention, also comprise two temperature points, two flowmeters and three flue gas measuring points, described three flue gas measuring points comprise the first flue gas measuring point, the second flue gas measuring point and the 3rd flue gas measuring point, and above-mentioned each measuring point coordinates and forms multiple control loops to relevant control valve.
Described two temperature points are all located at the burner hearth rear portion of described thermal oxidation furnace 2, and one of them temperature point coordinates formation one for controlling the temperature control loop TIC01 of incineration temperature with a fuel control valve; Another temperature point coordinates with a cooling sea water regulating valve and has formed one for controlling the temperature control loop TIC02 of the flue-gas temperature that enters described SNCR SNCR reactor.
Pipeline between described combustion fan 9 and described burner 1 is a wind branched pipe 15, pipeline between described combustion fan 9 and described thermal oxidation furnace 2 is Secondary Air arm 16, two flowmeters are located at respectively on described combustion air main pipe rail 14 and a wind branched pipe 15, thereby on a described wind branched pipe 15, be also provided with a volume damper FCV02 and form wind flow control loop FIC01-02 of burner, in order to control the flow of the primary air that enters described burner 1.
The ammonia import department of described blender A11 is provided with the first air inlet adjustment valve ACV01, the flue gas pipeline of described SNCR SNCR processor 3 is provided with the first flue gas measuring point, and the first air inlet adjustment valve ACV01 and described the first flue gas measuring point form the control loop AIC01 that enters the reducing agent flow of conversion zone in described SNCR SNCR reactor in order to control; The ammonia import department of described blender B13 is provided with the second air inlet adjustment valve ACV02, described chimney 8 is provided with the second flue gas measuring point, and the second air inlet adjustment valve ACV02 and described the second flue gas measuring point form the control loop AIC02 in order to control the reducing agent flow that enters described SCR SCR processor 5.
Described combustion fan 9 connects a variable-frequency motor M, and described chimney 8 is provided with the 3rd flue gas measuring point, and described variable-frequency motor M and described the 3rd flue gas measuring point form the control loop AIC03 of the flow in order to control the combustion air that enters combustion air house steward 14.
If debirs, except Nitrogen element, also contain element sulphur, more to strictly control NH
3escape amount, and the lower tail air preheater section of whole device temperature (that is, being positioned at the heat exchanger tube outside wall temperature of air preheater compared with the air preheater afterbody heat-transfer surface place of lower part) increase soot blower, avoid NH
4hSO
3be attached to and on heating surface, affect heat transfer efficiency.
Utilizing incinerating and treating device of the present invention to carry out burning disposal to nitrogenous debirs comprises the following steps:
A. be gaseous state or liquid state according to refuse, adopt suitable injection apparatus to be sent into and in thermal oxidation furnace, carry out high temperature incineration; The fuel of afterburning adopts central lance to spray in the burner hearth of thermal oxidation furnace 2; If refuse is waste gas, adopt ring-type spray gun waste gas to be sprayed in the burner hearth of thermal oxidation furnace; If refuse is waste liquid, select nozzle arrangements according to performance indications such as the viscosity of this waste liquid, specifically select multiple mechanical atomizations or the medium atomization nozzle arranged in the form of a ring, waste liquid is sprayed into the burner hearth flame of centre region of thermal oxidation furnace 2.
In high temperature incineration process, by controlling incineration temperature in described thermal oxidation furnace 2 burner hearths at 900～1200 ℃ by being arranged on the temperature point at burner hearth rear portion of described thermal oxidation furnace 2 and temperature control loop TIC01 that fuel control valve TCV01 forms; When the refuse of burning disposal is while not belonging to the debirs of hazardous waste, its incineration temperature is 900～1100 ℃, and in the time of debirs that the refuse of burning disposal is hazardous waste, its incinerator bore temperature is 1100～1200 ℃.
After incineration of waste, the flue-gas temperature that the temperature control loop TIC02 control forming by another temperature point and cooling sea water regulating valve enters SNCR reactor is 900～1050 ℃.
B. combustion air provides by combustion fan 9, the total amount of combustion air is to utilize by the variable-frequency motor M being connected with combustion fan 9 and be arranged on the control loop AIC03 that the 3rd flue gas measuring point on chimney 8 forms to control, oxygen content in the flue gas collecting according to the 3rd flue gas measuring point is as parameter, regulate the frequency of frequency conversion fan, thereby control the flow of the combustion air that enters combustion air house steward 14, first the air of discharging from combustion fan 9 outlet enters air preheater 6 preheatings, and the air after preheating is divided into wind and Secondary Air by a certain percentage, and to enter the burner hearth of thermal oxidation furnace 2 combustion-supporting, connecting line between described combustion fan 9 and described burner 1 is a wind branched pipe 15, connecting line between described combustion fan 9 and described thermal oxidation furnace 2 is Secondary Air arm 16, form a control loop FIC01-02 by two two flowmeters that are separately positioned on described combustion air main pipe rail 14 and a wind branched pipe 15 with a volume damper FCV02 who is arranged on a wind branched pipe 15, the flow that this control loop FIC01-02 controls a wind accounts for 60～80% of total air mass flow, according to the numerical value of the flowmeter on wind branched pipe of setting parameter of flowmeter on combustion air main pipe rail 14, enter the amount of the combustion air of burner 1 with control by this control loop of the Flow-rate adjustment FIC01-02 on a wind branched pipe 15, adopt segmentation air distribution to reduce combustion zone temperature, thereby the generation of thermal NO x in minimizing combustion process,
C. the reaction temperature of controlling SNCR SNCR processor is 900～1050 ℃, spray into reducing agent in SNCR SNCR processor 3 before, control the flow realization of the cooling water that enters thermal oxidation furnace 2 by temperature control loop TIC02 flue gas is lowered the temperature, guarantee the flue-gas temperature that enters SNCR SNCR processor 3; The ammonia import department of described blender A11 is provided with the first air inlet adjustment valve ACV01, the flue gas pipeline of described SNCR SNCR processor 3 is provided with the first flue gas measuring point, and the first air inlet adjustment valve ACV01 and described the first flue gas measuring point form the control loop AIC01 that enters the reducing agent flow of conversion zone in described SNCR SNCR reactor in order to control; Spray into the conversion zone of SNCR SNCR processor 3 reducing agent that the mist of ammonia below 5% concentration and air forms by blender A11, the flow that the amount of this reducing agent detects the NOx in flue gas by control loop AIC01 is controlled, and the method that adopts SNCR SNCR is first reduced to N by 30～70% NOx in flue gas
2and O
2:
D. enter waste heat boiler 4 from thermal oxidation furnace 2 high-temperature flue gas out through SNCR SNCR reactor 3 and carry out the recovery of part heat, and produce steam, thereby waste heat boiler 4 outlet temperatures are reduced to below 400 ℃;
The flue gas of e. discharging from waste heat boiler 4 enters SCR SCR processor 5, wherein, reducing agent adopts ammonia below 5% concentration and the mist of air, the flow that the amount of this reducing agent detects the NOx in flue gas by control loop AIC02 is controlled, and adopts the method for SCR SCR that the NOx in flue gas is reduced to N
2and O
2thereby, make flue gas reach the discharge standard of NOx;
F., the waste heat of the further recovered flue gas of air preheater is set in SCR SCR processor 5 downstreams;
G. be admitted to discharge chimney 8 from air preheater 6 flue gas out by air-introduced machine 7.
Further understand the present invention by an embodiment research material below, it is the convenience in order to understand that this research material is provided, and is never restriction the present invention.
Embodiment research material brief introduction: the tail gas of certain built extraordinary amine process units discharge comprises PSA tail gas, nitrogenous technology waste gas and nitrogenous effluent, be characterized in that composition, flow and the pressure of PSA tail gas, technology waste gas and waste water are all in irregular variation, sometimes change violent especially.Itrogenous organic substance has ethamine, propylene cyanogen, propylamine etc., requires incineration temperature more than 1100 ℃, but while exceeding 1300 ℃, thermal NO will produce in a large number, therefore must control the incineration temperature of thermal oxidation furnace 2.For the refuse that will burn, the bavin oil and gas of afterburning sprays into from burner 1 central lance, than relatively large waste gas also from entering into burner 1, spray into the burner hearth of thermal oxidation furnace 2 by the interior ring-type spray gun of burner 1, other waste liquids adopt medium atomization nozzle to spray into burner hearth, nozzle is in burner hearth sidewall annular configuration, combustion air is divided into two parts, wind enters the burner hearth of thermal oxidation furnace 2 from burner 1 air inlet by wind branched pipe 15, Secondary Air enters from burner hearth sidewall by secondary air separating arm 16, can guarantee like this even of burner hearth flow field, and there is no district of localized hyperthermia, can guarantee that refuse fully decomposes, avoid again generating a large amount of nitrogen oxide.Under enough time of staying, the smoke components after burning is as follows:
Smoke components after table 1 burns
Flue gas after burning adopts the out of stock nitrogen oxide removing in flue gas of two-stage, the temperature province of SNCR SNCR method is arranged on 1000 ℃ of left and right, the temperature province of SCR SCR method is arranged on 350 ℃ of left and right, determining of this temperature is relevant with the selection of SCR device catalyst, its corresponding relation between the two belongs to common practise in the art, does not repeat them here.In the flow process for the treatment of process of the present invention, be provided with waste heat boiler and the air preheater waste heat in order to recovered flue gas.Content through NOx in the flue gas of processing can drop to below 400mg/m3.
To sum up, the invention solves organic compounds containing nitrogen waste gas waste water and fully decompose in thermal oxidation furnace, decomposition efficiency reaches 99.99%, and has solved refuse and in the time of oxygen enrichment high-temp combustion, produce a large amount of fuel type NOx and high temperature modification NOx emission problem.
Although in conjunction with figure, invention has been described above; but the present invention is not limited to the above-mentioned specific embodiment; the above-mentioned specific embodiment is only schematic; rather than restrictive; those of ordinary skill in the art is under enlightenment of the present invention; in the situation that not departing from aim of the present invention, can also make a lot of distortion, within these all belong to protection of the present invention.
Claims (9)
1. the incinerating and treating device for nitrogenous debirs, comprise burner (1), thermal oxidation furnace (2), waste heat boiler (4), SCR SCR processor (5), air preheater (6), air-introduced machine (7), chimney (8) and a furnace pressure control loop of series connection successively, described furnace pressure control loop comprises that a pressure-measuring-point that is arranged on described thermal oxidation furnace (2) furnace front forms with the variable-frequency motor being connected with described air-introduced machine (7);
It is characterized in that:
The afterbody of described thermal oxidation furnace (2) is provided with a SNCR SNCR processor (3), described SNCR SNCR processor (3) is in series with a blender A(11) and a dilution air A(10), described SCR SCR processor (5) is in series with a blender B(13) and a dilution air B(12), described blender A(11) and blender B(13) for entering respectively described SNCR SNCR processor (3) and SCR SCR processor (5) after diluent air and ammonia mixing;
Also comprise a combustion fan (9) and combustion air house steward (14), the exhaust outlet of described combustion fan (9) is connected with described air preheater (6), connect with air preheater (6) in described combustion air house steward's (14) upstream, described combustion air house steward's (14) downstream is connected to respectively described burner (1) and described thermal oxidation furnace (2) by a threeway;
Also comprise injection apparatus, described injection apparatus comprises the central lance that needs postcombustion for spraying maintaining heat oxidation furnace (2) incineration temperature that is arranged on center in described burner, for spray the ring-type spray gun of waste gas to thermal oxidation furnace (2), according to atomizing nozzle and the medium atomization nozzle on the headwall of described thermal oxidation furnace (2), spray waste water for flame region in thermal oxidation furnace of being circular layout;
Also comprise two temperature points, two flowmeters and three flue gas measuring points, described three flue gas measuring points comprise the first flue gas measuring point, the second flue gas measuring point and the 3rd flue gas measuring point, and above-mentioned two temperature points, two flowmeters and three flue gas measuring points coordinate and form multiple control loops to relevant control valve.
2. the incinerating and treating device for nitrogenous debirs according to claim 1, it is characterized in that, described two temperature points are all located at the burner hearth rear portion of described thermal oxidation furnace (2), and one of them temperature point coordinates formation one for controlling the temperature control loop TIC01 of incineration temperature with a fuel control valve; Another temperature point coordinates with a cooling sea water regulating valve and has formed one for controlling the temperature control loop TIC02 of the flue-gas temperature that enters described SNCR SNCR reactor.
3. the incinerating and treating device for nitrogenous debirs according to claim 1, it is characterized in that, pipeline between described combustion fan (9) and described burner (1) is a wind branched pipe (15), pipeline between described combustion fan (9) and described thermal oxidation furnace (2) is Secondary Air arm (16), two flowmeters are located at respectively on described combustion air main pipe rail (14) and a wind branched pipe (15), on a described wind branched pipe (15), be also provided with a volume damper (FCV02) thereby wind flow control loop FIC01-02 of formation burner, in order to control the flow of the primary air that enters described burner (1).
4. the incinerating and treating device for nitrogenous debirs according to claim 1, it is characterized in that, described blender A(11) ammonia import department be provided with the first air inlet adjustment valve (ACV01), the flue gas pipeline of described SNCR SNCR processor (3) is provided with the first flue gas measuring point, and the first air inlet adjustment valve (ACV01) and described the first flue gas measuring point form the control loop AIC01 that enters the reducing agent flow of conversion zone in described SNCR SNCR reactor in order to control; Described blender B(13) ammonia import department be provided with the second air inlet adjustment valve (ACV02), described chimney (8) is provided with the second flue gas measuring point, and the second air inlet adjustment valve (ACV02) and described the second flue gas measuring point form the control loop AIC02 in order to control the reducing agent flow that enters described SCR SCR processor (5).
5. the incinerating and treating device for nitrogenous debirs according to claim 1, it is characterized in that, described combustion fan (9) connects a variable-frequency motor (M), described chimney (8) is provided with the 3rd flue gas measuring point, and described variable-frequency motor (M) and described the 3rd flue gas measuring point form the control loop AIC03 of the flow in order to control the combustion air that enters combustion air house steward (14).
6. the incinerating and treating device for nitrogenous debirs according to claim 1, is characterized in that, described air preheater section is provided with soot blower.
7. a technique of nitrogenous debirs being carried out to burning disposal, is characterized in that, adopts incinerating and treating device as claimed in claim 1, nitrogenous debirs is carried out to burning disposal and comprise the following steps:
A. be gaseous state or liquid state according to refuse, adopt suitable injection apparatus to be sent in thermal oxidation furnace (2) and carry out high temperature incineration; The fuel of afterburning adopts central lance to spray in the burner hearth of thermal oxidation furnace (2); In high temperature incineration process, by controlling incineration temperature in described thermal oxidation furnace (2) burner hearth at 900～1200 ℃ by being arranged on the temperature point at burner hearth rear portion of described thermal oxidation furnace (2) and temperature control loop TIC01 that fuel control valve (TCV01) forms; After incineration of waste, the flue-gas temperature that the temperature control loop TIC02 control forming by another temperature point and cooling sea water regulating valve enters SNCR reactor is 900～1050 ℃;
B. combustion air provides by combustion fan (9), the total amount of combustion air is to utilize by the variable-frequency motor (M) being connected with combustion fan (9) and be arranged on the control loop AIC03 that the 3rd flue gas measuring point on chimney (8) forms to control, oxygen content in the flue gas collecting according to the 3rd flue gas measuring point is as parameter, regulate the frequency of frequency conversion fan, thereby control the flow of the combustion air that enters combustion air house steward (14), first the air of discharging from combustion fan (9) outlet enters air preheater (6) preheating, and the air after preheating is divided into wind and Secondary Air by a certain percentage, and to enter the burner hearth of thermal oxidation furnace (2) combustion-supporting, connecting line between described combustion fan (9) and described burner (1) is a wind branched pipe (15), connecting line between described combustion fan (9) and described thermal oxidation furnace (2) is Secondary Air arm (16), form a control loop FIC01-02 by two two flowmeters that are separately positioned on described combustion air main pipe rail (14) and a wind branched pipe (15) with the volume damper (FCV02) being arranged on a wind branched pipe (15), the flow that this control loop FIC01-02 controls a wind accounts for 60～80% of total air mass flow, according to the numerical value of the flowmeter on wind branched pipe of setting parameter of the upper flowmeter of combustion air main pipe rail (14), enter the amount of the combustion air of burner (1) with control by this control loop of the Flow-rate adjustment FIC01-02 on a wind branched pipe (15), adopt segmentation air distribution to reduce combustion zone temperature, thereby the generation of thermal NO x in minimizing combustion process,
C. the reaction temperature of controlling SNCR SNCR processor is 900～1050 ℃, spray into reducing agent in SNCR SNCR processor (3) before, control the flow realization of the cooling water that enters thermal oxidation furnace (2) by temperature control loop TIC02 flue gas is lowered the temperature, guarantee the flue-gas temperature that enters SNCR SNCR processor (3); Described blender A(11) ammonia import department be provided with the first air inlet adjustment valve (ACV01), the flue gas pipeline of described SNCR SNCR processor (3) is provided with the first flue gas measuring point, and the first air inlet adjustment valve (ACV01) and described the first flue gas measuring point form the control loop AIC01 that enters the reducing agent flow of conversion zone in described SNCR SNCR reactor in order to control; By blender A(11) spray into the conversion zone of SNCR SNCR processor (3) reducing agent that the mist of ammonia below 5% concentration and air forms, the amount of this reducing agent detects the NO in flue gas by control loop AIC01
xflow control, adopt the method for SNCR (SNCR) first 30～70% NOx in flue gas to be reduced to N
2and O
2:
D. enter waste heat boiler (4) from thermal oxidation furnace (2) high-temperature flue gas out through SNCR SNCR reactor (3) and carry out the recovery of part heat, and produce steam, thereby waste heat boiler (4) outlet temperature is reduced to below 400 ℃;
The flue gas of e. discharging from waste heat boiler (4) enters SCR SCR processor (5), and wherein, reducing agent adopts ammonia below 5% concentration and the mist of air, and the amount of this reducing agent detects the NO in flue gas by control loop AIC02
xflow control, adopt SCR (SCR) method the NOx in flue gas is reduced to N
2and O
2thereby, make flue gas reach the discharge standard of NOx;
F., the waste heat of the further recovered flue gas of air preheater is set in SCR SCR processor (5) downstream;
G. be admitted to discharge chimney (8) from air preheater (6) flue gas out by air-introduced machine (7).
8. the technique of according to claim 7 nitrogenous debirs being carried out burning disposal, is characterized in that, further, in step a, if refuse is waste gas, adopts ring-type spray gun waste gas to be sprayed in the burner hearth of thermal oxidation furnace; If refuse is waste liquid, select according to the character of this waste liquid multiple mechanical atomizations or the medium atomization nozzle arranged in the form of a ring, waste liquid is sprayed into the burner hearth flame of centre region of thermal oxidation furnace (2).
9. according to claim 7 nitrogenous debirs are carried out the technique of burning disposal, it is characterized in that, further, in step a, when the refuse of burning disposal is while not belonging to the debirs of hazardous waste, its incineration temperature is 900～1100 ℃, and in the time of debirs that the refuse of burning disposal is hazardous waste, its incineration temperature is 1100～1200 ℃.
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0803278A1 (en) * | 1996-04-22 | 1997-10-29 | Applied Utility Systems, Inc. | Integrated catalytic/non-catalytic process for selective reduction of nitrogen oxides |
| KR101002888B1 (en) * | 2010-06-03 | 2010-12-21 | 한국전력기술 주식회사 | The hybrid de-nox system for boiler emission |
| CN201954556U (en) * | 2010-12-23 | 2011-08-31 | 北京机电院高技术股份有限公司 | Emission limit device for reducing nitrogen oxide in waste incineration smoke |
| CN202010510U (en) * | 2010-05-21 | 2011-10-19 | 中国神华能源股份有限公司 | Flue gas denitration equipment |
| KR20120009347A (en) * | 2010-07-23 | 2012-02-01 | 한모기술주식회사 | The chemical injection method of de-NOx system |
-
2012
- 2012-04-20 CN CN201210118586.2A patent/CN102644922B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0803278A1 (en) * | 1996-04-22 | 1997-10-29 | Applied Utility Systems, Inc. | Integrated catalytic/non-catalytic process for selective reduction of nitrogen oxides |
| CN202010510U (en) * | 2010-05-21 | 2011-10-19 | 中国神华能源股份有限公司 | Flue gas denitration equipment |
| KR101002888B1 (en) * | 2010-06-03 | 2010-12-21 | 한국전력기술 주식회사 | The hybrid de-nox system for boiler emission |
| KR20120009347A (en) * | 2010-07-23 | 2012-02-01 | 한모기술주식회사 | The chemical injection method of de-NOx system |
| CN201954556U (en) * | 2010-12-23 | 2011-08-31 | 北京机电院高技术股份有限公司 | Emission limit device for reducing nitrogen oxide in waste incineration smoke |
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