CN111928251A - Combustion treatment device and process for nitrogen-containing raw material - Google Patents

Combustion treatment device and process for nitrogen-containing raw material Download PDF

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Publication number
CN111928251A
CN111928251A CN202010968229.XA CN202010968229A CN111928251A CN 111928251 A CN111928251 A CN 111928251A CN 202010968229 A CN202010968229 A CN 202010968229A CN 111928251 A CN111928251 A CN 111928251A
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pyrolysis
combustion
section
combustion chamber
nitrogen
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熊绍武
马洪玺
杜先
孙国辉
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Shanghai Lanke Petrochemical Engineering & Technology Co ltd
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Shanghai Lanke Petrochemical Engineering & Technology Co ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/008—Incineration of waste; Incinerator constructions; Details, accessories or control therefor adapted for burning two or more kinds, e.g. liquid and solid, of waste being fed through separate inlets
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • F23G5/16—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber
    • F23G5/165—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber arranged at a different level
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/103—Combustion in two or more stages in separate chambers
    • 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
    • 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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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Incineration Of Waste (AREA)

Abstract

The invention discloses a multiphase combustion treatment device for nitrogen-containing raw materials, which comprises a pyrolysis section and a combustion section which are connected into a whole; one end of the pyrolysis section is respectively provided with a multi-medium burner and a plurality of nitrogen-containing raw material inlets; the multi-medium burner is respectively provided with a plurality of inlets for introducing high-calorific-value waste gas and liquid and air for combusting the high-calorific-value waste gas and liquid; the combustion section comprises a plurality of communicated combustion chambers for completely combusting pyrolysis products step by step; the other end of the pyrolysis section is connected to one of the combustion chambers. The invention also provides a multiphase combustion treatment process of the nitrogenous raw material. The combustion treatment device and the process can particularly carry out integrated heterogeneous combustion for high-nitrogen three wastes, reduce the NOx conversion rate of raw material nitrogen to be below 5 percent, control the oxygen content of flue gas to be within 1 to 5 percent, reduce the flue gas quantity and the flue gas purification cost and realize better social and economic benefits.

Description

Combustion treatment device and process for nitrogen-containing raw material
Technical Field
The invention belongs to the technical field of chemical treatment, and relates to a multiphase combustion treatment device and process for a nitrogen-containing raw material.
Background
Some chemical enterprises or chemical parks need to treat solid waste, organic waste liquid and organic waste gas simultaneously, and the solid waste, the organic waste liquid and the organic waste gas have complex components, some have high heat value and some have low heat value. At present, the common treatment mode is that solid waste, waste liquid and waste gas with high calorific value and low calorific value are respectively treated, for example, the waste liquid and the waste gas with high calorific value are directly burnt, and the VOC waste gas with low calorific value is treated by catalytic oxidation. This results in several sets of incineration disposal devices being required to be built in a single park or a single chemical plant for different three wastes, which increases investment, land occupation and resource waste.
Chinese patent document CN201920201760.7 discloses a gas-liquid-solid waste comprehensive treatment system, which adopts a water-coal-slurry process, but the application range of the solid waste is limited to the high-calorific-value solid waste such as coal, biomass, petroleum coke, blue carbon, sludge, oil sand, waste activated carbon, etc., and many additives are required to be added in the preparation process of coal slurry, so that the burning amount of an incinerator is additionally increased, and the problems of limited application range and serious heat loss of slurry mixing water exist.
In solid waste, waste liquid and waste gas of chemical enterprises, the content of ammonia nitrogen is high frequently, the traditional incineration process combines various low-nitrogen combustion technologies, the proportion of converting the ammonia nitrogen into the NOx in the fuel can be controlled below 50% at the lowest, for a plurality of organic wastes with high ammonia nitrogen content, the conversion rate of 50% is still high, the investment of subsequent flue gas denitration is large, the medicament consumption is high, and the operation cost is high.
Chinese patent document CN202010124361.2 discloses a low-nitrogen incineration technology for waste liquid and waste gas, and NO of fuel nitrogenXThe conversion rate can be controlled to be about 10 percent, but for a lot of high-nitrogen raw materials, the conversion rate of 10 percent is still high, and the method cannot treat solid wastes, so the problem of comprehensive integrated ultralow nitrogen treatment of the solid wastes, waste liquid and waste gas of the high-nitrogen raw materials cannot be solved.
Disclosure of Invention
Aiming at the problems in the prior art, the invention aims to provide a multiphase combustion treatment device and process for nitrogen-containing raw materials, and particularly aims to perform integrated multiphase combustion for high raw material nitrogen three wastes, so that the NOx conversion rate of raw material nitrogen is reduced to be below 5%, the oxygen content of flue gas is controlled within 1% -5%, the flue gas amount and the flue gas purification cost are reduced, and better social and economic benefits are realized.
One of the purposes of the invention is to provide a multiphase combustion treatment device for nitrogenous raw materials, which adopts the following technical scheme:
a multiphase combustion processing device for nitrogen-containing raw materials comprises a pyrolysis section and a combustion section which are connected into a whole;
one end of the pyrolysis section is respectively provided with a multi-medium burner and a plurality of nitrogen-containing raw material inlets; the multi-medium burner is respectively provided with a plurality of inlets for introducing high-calorific-value waste gas and liquid and air for combusting the high-calorific-value waste gas and liquid;
the combustion section comprises a plurality of communicated combustion chambers and is used for gradually combusting and purifying pyrolysis products; the other end of the pyrolysis section is connected to one of the combustion chambers.
Preferably, the pyrolysis section adopts a rotary pyrolysis furnace or a fixed pyrolysis furnace according to different types of the nitrogen-containing raw materials, when solid waste in the nitrogen-containing raw materials is easily ground solid waste or does not contain the solid waste, the fixed pyrolysis furnace is adopted, and the easily ground solid waste is ground into particles of about 50 micrometers and then is blown into the fixed pyrolysis furnace by a feeding fan; when the solid waste in the raw materials is non-grindable or difficultly-grindable substances, the solid waste is crushed into blocky particles with the particle size of less than 10cm and then is sent into the rotary pyrolysis furnace in a feeding chute, a screw feeder, a pusher and other modes.
Preferably, the multi-medium burner is fixed at one end of the rotary pyrolysis furnace or the fixed pyrolysis furnace.
Preferably, the multi-medium burner is provided with a high-calorific-value waste liquid inlet, a high-calorific-value waste gas inlet and a pyrolysis section primary air inlet.
Preferably, the nitrogen-containing raw material inlet comprises any one or more of a solid waste inlet, a nitrogen-containing waste gas inlet and a nitrogen-containing waste liquid inlet.
Preferably, the combustion section comprises a primary combustion chamber and a secondary combustion chamber which are communicated with each other, and the secondary combustion chamber is positioned on the upper side of the primary combustion chamber;
the primary combustion chamber is communicated with the other end of the pyrolysis section, which is far away from the medium burner.
Furthermore, a combustion section primary air inlet is formed in the bottom of the primary combustion chamber.
Furthermore, a fluidization structure or a flow guide structure is arranged at the bottom of the primary combustion chamber above the primary air inlet of the combustion section. The fluidized structure is provided with fluidized bed materials, when the nitrogen-containing raw materials contain solid wastes, the fluidized structure is arranged above the primary air inlet of the combustion section, and the pyrolyzed solid residues and the fluidized bed materials are subjected to strong collision and are crushed into fine particles, so that the solid residues are completely combusted. When nitrogenous raw materials do not have solid waste, set up the water conservancy diversion structure in combustion section primary air inlet's top, the water conservancy diversion structure can be guide plate or water conservancy diversion grid etc to guarantee that primary air and the pyrolysis product flue gas after the pyrolysis of pyrolysis section and the waste liquid waste gas waste water misce bene of sending into primary combustion chamber.
Furthermore, a plurality of external interfaces are arranged on the outer wall of the primary combustion chamber, and comprise any one or combination of a recirculation flue gas interface, a low-heat-value waste liquid interface and a waste water interface; wherein, the flue gas of the burning section is escaped from the top, is connected to a recirculating flue gas interface after heat recovery and purification.
Furthermore, a contraction type mixing structure is communicated and arranged at an inlet of the secondary combustion chamber, and the contraction type mixing structure is positioned between the primary combustion chamber and the secondary combustion chamber; and a secondary air interface of a combustion section is arranged on the throat contraction section of the contraction type mixing structure.
The invention also aims to provide a multiphase combustion treatment process of the nitrogenous raw material, which comprises the following steps:
s1, feeding solid waste substances and/or nitrogen-containing waste gas and/or nitrogen-containing waste liquid into a pyrolysis section through corresponding inlets for pyrolysis treatment, and simultaneously burning the high-heat-value waste gas and waste liquid and primary air of the pyrolysis section through a multi-medium burner to provide heat for high-temperature pyrolysis of nitrogen-containing raw materials in the pyrolysis section;
and S2, enabling pyrolysis products of the pyrolysis section to enter a plurality of combustion chambers of the combustion section, gradually burning and purifying the pyrolysis products, and enabling flue gas after complete combustion to escape from the top of the combustion section.
Preferably, in step S2, the combustion section includes a primary combustion chamber, a contraction-type mixing structure, and a secondary combustion chamber sequentially arranged from bottom to top;
the pyrolysis product firstly enters a primary combustion chamber, primary air is introduced into the bottom of the primary combustion chamber through a primary air inlet of a combustion section, and meanwhile, waste water and/or low-heat-value waste gas and/or low-heat-value waste liquid introduced from the outside are converted into gaseous substances in the primary combustion chamber by using the high temperature of the pyrolysis product and then are uniformly mixed with the pyrolysis product and the primary air, so that the waste water and/or the low-heat-value waste gas and/or the low-heat-value waste liquid and the pyrolysis product are fully combusted in the primary combustion chamber, and the combusted flue gas escapes to a contraction type mixing structure;
wherein, when the nitrogenous raw material in the step S1 contains solid waste substances, nitrogenous waste gases and nitrogenous waste liquid: the pyrolysis product firstly enters a primary combustion chamber, and the pyrolyzed solid residue is fluidized by introducing primary air into a fluidized bed at the bottom of the primary combustion chamber and is strongly collided with bed materials on the fluidized bed to form fine particles, so that the pyrolyzed solid residue is completely combusted at the bottom. The high-temperature flue gas after pyrolysis is mixed with wastewater and/or low-heat-value waste liquid and/or low-heat-value waste gas introduced from the outside in a primary combustion chamber, the low-heat-value waste liquid and/or the wastewater are quickly evaporated and are uniformly mixed with the flue gas and primary air introduced from the bottom of the primary combustion chamber together with the low-heat-value waste gas, so that pyrolysis products and the low-heat-value waste gas are fully combusted in the primary combustion chamber and then escape to a contraction type mixing structure;
and the throat contraction section of the contraction type mixing structure is provided with a combustion section secondary air interface, secondary air and smoke coming from the primary combustion chamber are intensively mixed at the contraction type mixing structure and then upwards enter the secondary combustion chamber, so that unreacted combustible materials in the pyrolysis section and the primary combustion chamber are completely combusted in the secondary combustion chamber, and then the smoke escapes from the top of the secondary combustion chamber.
Further, in step S1, the primary air amount in the pyrolysis section is controlled to maintain the air-fuel ratio in the pyrolysis section between 0.6 and 0.9 and the temperature between 1200 and 1350 ℃, and the nitrogen in the raw material is controlled to be converted into N according to a reduction mechanism2The pyrolysis temperature is controlled to be more than 1200 ℃, and NH with higher activation energy can be ensured3Complete reaction, but the reaction temperature is too high and is higher than 1350 ℃, not only for NH3Does not contribute much and can result in excessive subsequent furnace temperatures and increased thermodynamic NOx production. High investment cost of incinerator,。
Further, in step S2, the temperature in the primary combustion chamber is maintained at 950 to 1200 ℃ by controlling the amount of the waste water and/or the low heating value waste liquid and/or the low heating value exhaust gas and/or the recirculated flue gas and the amount of the primary air.
Further, in step S2, the temperature in the secondary combustion chamber is maintained at 850 to 1100 ℃ and the oxygen content is maintained at 1 to 5% by controlling the amount of secondary air.
The invention can bring the following beneficial effects:
1) in the invention, a pyrolysis section and a combustion section are combined, the pyrolysis section is used for combusting high-heat-value waste liquid and waste gas through a multi-medium combustor and providing sufficient oxygen for the combustion process of the waste liquid and the waste gas, so that the high temperature required by the pyrolysis section is provided, and the specific temperature control is adjusted according to the composition of liquid, solid and three wastes of the treated gas, so as to realize the full pyrolysis of different phase-state substances (which can be multi-phase-state substances and can also be single-phase-state substances). But the whole pyrolysis section is in an anoxic reduction state, so that solid waste, waste liquid and waste gas are pyrolyzed to generate a large amount of CO and H2And hydrocarbon and the like, thereby inhibiting the conversion of ammonia nitrogen in the raw materials into nitrogen oxides, and simultaneously reducing the generated nitrogen oxides and the nitrogen oxides carried by the waste gas into nitrogen at high temperature. And the solid after the pyrolysis section treatmentThe residue and the gas products enter the combustion section, and the pyrolysis products can be subjected to full deep reaction treatment step by adopting a multi-combustion-chamber structure. Thereby, through integrating the advantage of pyrolysis and burning, raw materials nitrogen NOx conversion in can greatly reduced waste gas waste liquid and the solid useless realizes the low nitrogen of nitrogenous raw materials especially high nitrogen raw materials and handles, reduces and burns burning furnace export NOx concentration, reduces follow-up flue gas denitration treatment facility and running cost.
2) The invention can not only treat waste gas, waste liquid and waste water with various heat values and compositions, but also treat various solid wastes simultaneously, and has very strong raw material adaptability. Therefore, the integrated multiphase pyrolysis combustion is realized aiming at the three wastes of the high-nitrogen raw material, the integration level is high, the cost is saved, and the method is suitable for industrial popularization.
3) The combination of the process conditions in the invention can ensure that the NOx conversion rate of the raw material nitrogen in the waste gas and liquid as well as the solid waste is less than 5 percent, and the NOx in the raw material waste gas is reduced into N2The efficiency is more than 95%. Therefore, the concentration of NOx at the outlet of the incinerator can be greatly reduced, and the subsequent flue gas denitration treatment equipment and the operation cost are reduced.
4) According to the invention, through gradual pyrolysis combustion, complete combustion under low-oxygen combustion can be ensured, the oxygen content of flue gas escaping from the secondary combustion chamber is controlled within 1-5%, the flue gas amount and the flue gas purification cost are reduced, and better social and economic benefits are realized.
5) The invention is provided with the pyrolysis section and the plurality of combustion chambers, and can select and send the proper functional parts to be treated according to the characteristics of the organic matters, thereby ensuring the complete combustion of the organic matters as raw materials.
Drawings
FIG. 1 is a schematic view of a processing apparatus according to the present invention.
The meanings of the symbols in the drawings are as follows:
1-pyrolysis section, 11-multimedia burner, 12-solid waste inlet, 13-nitrogen-containing waste gas inlet, 14-nitrogen-containing waste liquid inlet, 15-high heat value waste liquid inlet, 16-high heat value waste gas inlet, 17-pyrolysis section primary air inlet, 2-combustion section, 20-primary combustion chamber, 21-combustion section primary air inlet, 22-fluidization device, 23-recirculated flue gas inlet, 24-waste water inlet, 25-low heat value waste liquid inlet, 26-low heat value waste gas inlet, 27-contraction type mixing device, 28-combustion section secondary air inlet, and 29-secondary combustion chamber.
Detailed Description
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following description will be made with reference to the accompanying drawings. It is obvious that the drawings in the following description are only some examples of the invention, and that for a person skilled in the art, other drawings and embodiments can be derived from them without inventive effort.
For the sake of simplicity, the drawings only schematically show the parts relevant to the present invention, and they do not represent the actual structure as a product.
According to an embodiment of the present invention, as shown in fig. 1, a multiphase combustion processing apparatus for nitrogen-containing raw materials is provided, which comprises a pyrolysis section 1 and a combustion section 2 connected as a whole;
one end of the pyrolysis section 1 is respectively provided with a multi-medium burner 11 and a plurality of nitrogen-containing raw material inlets; the multimedia burner 11 is respectively provided with a plurality of inlets for introducing high calorific value waste gas and liquid and air for combusting the high calorific value waste gas and liquid;
the combustion section 2 comprises a plurality of communicated combustion chambers and is used for gradually combusting and purifying pyrolysis products; the other end of the pyrolysis section 1 is connected to one of the combustion chambers.
In this embodiment, the pyrolysis section is combined with the combustion section, the pyrolysis section is used for combusting high-calorific-value waste liquid and waste gas through the multi-medium combustor and providing sufficient oxygen for the combustion process, so that high temperature required by the pyrolysis section is provided, and the specific temperature control is adjusted according to the composition of liquid, solid and three wastes of the treated gas, so as to realize the sufficient pyrolysis of different phase substances. However, the pyrolysis section is also provided with a nitrogen-containing raw material inlet, wherein a plurality of nitrogen-containing raw material inlets can be introduced with raw material inlets in different phases (including gas-liquid-solid three phases), such as a solid waste inlet 12, a nitrogen-containing waste gas inlet 13 and a nitrogen-containing waste liquid inlet 14,according to different forms of solid waste (called solid waste for short), the solid waste can be sent into the pyrolysis section 1 through a feeding chute, a screw feeder, powder injection, a pusher and the like, nitrogen-containing waste liquid is atomized by a spray gun and then sent into the pyrolysis section 1 or is mixed with the solid waste and then sent into the pyrolysis section 1, and nitrogen-containing waste gas is sent into the pyrolysis section 1 by the spray gun or a distributor; after the nitrogen-containing raw material is introduced, the whole pyrolysis section 1 is in an anoxic reduction state, so that solid waste, waste liquid, waste gas and the like are pyrolyzed to generate a large amount of CO and H2When the reducing gas is in the pyrolysis section 1, the amino and the nitro in the high-nitrogen waste liquid and the solid waste and the NOx and NH in the high-nitrogen waste gas3Etc. with CO, H2Reacting with reducing gas to generate N2And H2And O. That is, the solid waste material is pyrolyzed to generate a large amount of CO and H2And hydrocarbon and the like, thereby inhibiting the conversion of ammonia nitrogen in the raw materials into nitrogen oxides, and simultaneously reducing the generated nitrogen oxides and the nitrogen oxides carried by the waste gas into nitrogen at high temperature. And the residue (containing solid residue) after the pyrolysis section 1 treatment enters the combustion section, and the pyrolysis product can be subjected to sufficient deep reaction treatment step by adopting a multi-combustion-chamber structure. Therefore, by integrating the advantages of pyrolysis and combustion, the NOx conversion rate of raw material nitrogen in waste gas and waste liquid and solid waste can be greatly reduced, the concentration of NOx at the outlet of the incinerator is reduced, and the subsequent flue gas denitration treatment equipment and the operation cost are reduced.
In a preferred embodiment, the pyrolysis section 1 is a rotary pyrolysis furnace, and the multimedia burner 11 is fixed at one end of the rotary pyrolysis furnace. Specifically, the rotary pyrolysis furnace can adopt a feeding chute, a screw feeder or a pusher for feeding, and is suitable for various solid wastes with the particle size smaller than 10cm or semi-solid wastes with high water content. Therefore, the rotary pyrolysis furnace can fully mix the flue gas and the solid waste in the furnace through rotation, so that the complete pyrolysis of the solid waste and the full reduction of nitrogen oxides in the flue gas are ensured. Preferably, the cylinder body of the rotary pyrolysis furnace can rotate around the axis of the rotary pyrolysis furnace, and a disturbance structure can be arranged in the cylinder body to strengthen the turnover of the solid waste and promote the mixing of the solid waste and the high-temperature pyrolysis flue gas. The flue gas and the solid waste can be further mixed more fully in the rotary process, and the pyrolysis of the solid waste and the reduction of nitrogen oxides in the flue gas are deeply promoted. Of course, in some application scenarios, the pyrolysis section 1 may also employ a stationary pyrolysis furnace. For example, when no solid waste raw material exists, no residue is generated due to pyrolysis, and the gaseous state formed by pyrolysis of the gas-liquid phase material in the pyrolysis furnace can be spontaneously and uniformly mixed.
In another preferred embodiment, the multimedia burner 11 is provided with a high calorific value waste liquid inlet 15, a high calorific value waste gas inlet 16 and a pyrolysis section primary air inlet 17. Specifically, the high calorific value waste liquid inlet 15 is connected with a high calorific value waste liquid spray gun, so that the high calorific value waste liquid is atomized by the spray gun and then is sent into the pyrolysis section 1 for combustion; the high-calorific-value waste gas inlet 16 is connected with a high-calorific-value waste gas spray gun or distributor and is fed into the pyrolysis section 1 for combustion; the pyrolysis section primary air inlet 17 is used for introducing combustion air; the high-calorific-value waste gas and liquid is combusted through the multi-medium burner under the action of primary air of the pyrolysis section to provide heat for the pyrolysis section, so that the pyrolysis temperature is kept above 1200 ℃, and meanwhile, the temperature is controlled not to exceed 1350 ℃, and the pyrolysis efficiency is promoted.
Therefore, the pyrolysis section 1 is in a gas phase state, a liquid phase state and a solid phase state, heat is provided for the pyrolysis by burning the waste gas and the waste liquid with high heat value, and the high-nitrogen waste gas, the high-nitrogen waste liquid and the solid waste can be subjected to gas-liquid-solid three-phase pyrolysis in the pyrolysis section 1; the combustion section 2 is essentially in three phase states of gas, liquid and solid, including the combustion of pyrolysis flue gas, the combustion of low-calorific-value waste gas/liquid and the combustion of pyrolysis solid residues. Specifically, the mixed combustion process of any one or more phases may be selected as required.
As another preferred embodiment, the combustion section 2 comprises a primary combustion chamber 20 and a secondary combustion chamber 29 which are communicated with each other, and the secondary combustion chamber 29 is positioned at the upper side of the primary combustion chamber 20; the primary combustion chamber 20 is communicated with the other end of the pyrolysis section 1 far away from the medium burner 11.
Specifically, the bottom of the primary combustion chamber 20 is provided with a combustion section primary air inlet 21. Preferably, the bottom of the primary combustion chamber 20 is further provided with a fluidization structure 22 or a flow guide structure above the primary air inlet 21 of the combustion section. The fluidized structure 22 is provided with fluidized bed materials, when the nitrogen-containing raw material contains solid waste, the fluidized structure 22 is arranged above the primary air inlet 21 of the combustion section, and the pyrolyzed solid residues and the fluidized bed materials are subjected to strong collision and are crushed into fine particles, so that the solid residues are completely combusted; by adopting a fluidization structure at the bottom of the primary combustion chamber 20 and introducing primary air from the primary air inlet 21 of the combustion section, the effect of the primary air comprises burning off and fluidizing the pyrolyzed solid particles, the pyrolyzed solid particles are completely combusted in the fluidization area of the primary combustion chamber, and the ash ignition loss is less than 3%. When the nitrogenous raw materials do not have solid waste, set up the water conservancy diversion structure in the top of combustion section primary air entry 21, the water conservancy diversion structure can be guide plate or water conservancy diversion grid etc to guarantee that primary air and the pyrolysis product flue gas after 2 pyrolysis of pyrolysis section and the waste liquid and/or waste gas and/or the waste water misce bene of sending into primary combustion chamber 20.
More specifically, the outer wall of the primary combustion chamber 20 is provided with an external interface, which comprises any one or a combination of a recirculation flue gas interface 23, a low-calorific-value waste gas interface 26, a low-calorific-value waste liquid interface 25 and a waste water interface 24; wherein, the flue gas of the combustion section 2 is discharged from the top to an external device for treatment, and then is recycled and connected to the recycled flue gas interface 23.
In this embodiment, the primary combustion chamber 20 has CO and H from the pyrolysis section 12The reducing gas and the solid residue are burnt, and the temperature is very high; pyrolysis solid residues sent from the pyrolysis section 1 are blown up by primary air with fluidized bed materials in the fluidized structure 22 to form a fluidized state, collide with the fluidized bed materials to be crushed into fine particles, and carry out strong combustion chemical reaction with combustion-supporting primary air at high temperature, the incineration rate of the solid residues is high, the ash burning reduction rate is less than 3%, and most of the burnt fly ash is carried out of the combustion section 2 by combustion flue gas. At the same time, the recirculated flue gas and/or waste water and/or low calorie waste liquid and/or low calorie waste gas introduced from the outside are rapidly evaporated and decomposed in the primary combustion chamber 20, which is advantageous not only for controlling the temperature of the primary combustion chamber 20 and for complete combustion of organic matterMoreover, various chemical waste gas raw materials are effectively treated, and the adaptability of raw material treatment is strong. For example, the temperature of the primary combustion chamber 20 is controlled to 950 ℃ to 1200 ℃ (the specific temperature is adjusted according to the composition of the three wastes (liquid solid, gas, solid, and gas) in the process gas). It should be noted that the fluidization structure 22 may be eliminated when the material from the pyrolysis section 2 does not contain solid components.
Wherein, it should be noted that the recirculated flue gas is the flue gas escaping from the top of the combustion section 2, and the flue gas is recirculated and connected to the recirculated flue gas interface 23 after being processed by external equipment. The low heating value waste gas interface 26, the low heating value waste liquid interface 25 and the waste water interface 24 are used for introducing corresponding waste gas, waste liquid and waste water from the outside, and can be selectively configured according to the requirements of different projects. For example, the low heating value waste gas interface 26 is not needed when part of the application scenes do not have low heating value waste gas. Of course, other interfaces with different phases may be disposed on the outer wall of the primary combustion chamber 20 according to requirements, so as to introduce different raw materials.
Further, a contraction type mixing structure 27 is communicated with an inlet of the secondary combustion chamber 29, and the contraction type mixing structure 27 is positioned between the primary combustion chamber 20 and the secondary combustion chamber 29; and a secondary air interface 28 of a combustion section is arranged on the throat contraction section of the contraction type mixing structure 27. That is, the retractable mixing structure 27 is located at the upper part of the external interfaces (the recirculation flue gas interface 23, the low calorific value waste gas interface 26, the low calorific value waste liquid interface 25, the waste water interface 24, and the like) of the primary combustion chamber 20, so as to ensure that the external raw materials such as the low calorific value waste gas and the waste liquid firstly pass through the primary combustion chamber and then enter the secondary combustion chamber through the retractable mixing structure to be fully combusted step by step. In this embodiment, the primary combustion chamber 20 and the secondary combustion chamber 29 are respectively communicated with a retractable mixing structure 27, so that the pyrolysis products of the pyrolysis section 1 are sent into the primary combustion chamber 20, and the products after the combustion treatment are continuously subjected to retraction mixing with the supplemented secondary air of the combustion section and then enter the secondary combustion chamber 29 for sufficient combustion treatment. Specifically, through the throat effect of the contraction section, the secondary air and the flue gas from the primary combustion chamber 20 are intensively mixed at the contraction type mixing structure 27 and then upwards enter the secondary combustion chamber 29, so that the uniform mixing of the micro-scale can be ensured, the temperature of the flue gas is reduced, the temperature in the secondary combustion chamber 29 is 850 ℃ -1100 ℃ (the specific control temperature is adjusted according to the composition of the waste gas and waste liquid to be treated), and the secondary combustion chamber 29 is provided with enough flue gas retention space, so that the complete combustion reaction of combustible substances can be ensured.
According to another embodiment of the present invention, a multiphase combustion treatment process for a nitrogen-containing feedstock is provided, as shown in fig. 1, including the following steps:
s1, feeding the solid waste substances and/or the nitrogen-containing waste gas and liquid into the pyrolysis section 1 through corresponding inlets for pyrolysis treatment, and feeding the high-calorific-value waste gas and liquid and the primary air of the pyrolysis section into the pyrolysis section through the multi-medium burner 11 for combustion to provide heat for high-temperature pyrolysis of the nitrogen-containing raw material in the pyrolysis section 1;
and S2, enabling pyrolysis products of the pyrolysis section 1 to enter a plurality of combustion chambers of the combustion section 2, combusting and purifying the pyrolysis products step by step, and enabling purified flue gas to escape from the top of the combustion section.
In this embodiment, the pyrolysis section 1 is combined with the combustion section 2, the pyrolysis section 1 combusts waste liquid and waste gas with high heat value through the multi-medium combustor 11, and provides sufficient oxygen for the combustion process, so as to provide high temperature required by the pyrolysis section, and the specific temperature control is adjusted according to the composition of liquid, solid and three wastes of the treated gas, so as to realize sufficient pyrolysis of different phase substances. However, since the pyrolysis section is also respectively filled with solid waste substances, high-nitrogen waste gas and liquid waste and the like through the solid waste inlet 12, the nitrogen-containing waste gas inlet 13 and the nitrogen-containing waste liquid inlet 14, the whole pyrolysis section 1 is in an anoxic reduction state, and therefore, the solid waste, the waste liquid and the waste gas in the pyrolysis section are thermally explained to release a large amount of CO and H2Reducing gas, amino and nitro in the high-nitrogen waste liquid and the solid waste and NOx and NH in the high-nitrogen waste gas in the pyrolysis section 13Etc. with CO, H2Reacting with reducing gas to generate N2And H2And O. And the residue after the pyrolysis section treatment 1 enters the combustion section, and the pyrolysis product can be subjected to full deep reaction treatment step by adopting a multi-combustion-chamber structure. Thus, by integrating the advantages of pyrolysis and combustion, process parameters are combinedThe NOx in the raw material waste gas is reduced to N2The efficiency is more than 95%. By the process, the concentration of NOx at the outlet of the incinerator can be greatly reduced, and the subsequent flue gas denitration treatment equipment and operation cost are reduced. The conversion rate of raw material nitrogen NOx in waste gas and waste liquid and solid waste can be greatly reduced, the concentration of NOx at the outlet of the incinerator is reduced, and the subsequent flue gas denitration treatment equipment and the operation cost are reduced.
In practical application, in step S1, different types of pyrolysis furnaces are selected for the pyrolysis section according to whether the nitrogenous raw material to be treated contains solid waste; when the processed nitrogenous raw material contains solid waste, a rotary pyrolysis furnace is adopted, and the solid waste is rotated along with a barrel of the pyrolysis furnace to strengthen the pyrolysis of the solid waste; when the raw materials do not contain solid wastes, a fixed pyrolysis furnace is adopted, so that the construction cost is reduced.
As a preferred embodiment, in step S2, the combustion section 2 includes a primary combustion chamber 20, a convergent mixing structure 27, and a secondary combustion chamber 29, which are sequentially arranged from bottom to top;
the pyrolysis product firstly enters a primary combustion chamber 20, primary air is introduced into the bottom of the primary combustion chamber 20 through a combustion section primary air inlet 21, meanwhile, wastewater and/or low-heat-value waste gas and/or low-heat-value waste liquid introduced from the outside are converted into gaseous substances in the primary combustion chamber 20 by using the high temperature of the pyrolysis product, and then are uniformly mixed with the pyrolysis product and the primary air, so that the wastewater and/or the low-heat-value waste gas and/or the low-heat-value waste liquid and the pyrolysis product are fully combusted in the primary combustion chamber, and the combusted flue gas escapes to a contraction type mixing structure 27;
wherein, when the nitrogenous raw material in the step S1 contains solid waste substances, nitrogenous waste gases and nitrogenous waste liquid: the pyrolysis product firstly enters the primary combustion chamber 20, and the pyrolyzed solid residue is fluidized on the fluidized bed material at the bottom of the primary combustion chamber 20 by the introduced primary air and is strongly collided with the fluidized bed material to form fine particles, so that the pyrolyzed solid residue is completely combusted at the bottom. The high-temperature flue gas after pyrolysis is mixed with waste water and/or low-heat value waste liquid and/or low-heat value waste gas introduced from the outside in the primary combustion chamber 20, the low-heat value waste liquid and/or the waste water are rapidly evaporated and are uniformly mixed with the flue gas and primary air introduced from the bottom of the primary combustion chamber 20 together with the low-heat value waste gas, so that pyrolysis products and the low-heat value waste gas liquid are fully combusted in the primary combustion chamber 20 and then escape to the contraction type mixing structure 27;
and, the throat contraction section of the contraction type mixing structure 27 is provided with a combustion section secondary air interface 28, the secondary air and the flue gas from the primary combustion chamber 20 are intensively mixed at the contraction type mixing structure 27 and then upwards enter the secondary combustion chamber 29, so that the combustible materials such as CO and the like which are not reacted in the pyrolysis section 1 and the primary combustion chamber 20 are completely combusted in the secondary combustion chamber 29, and then the flue gas escapes from the top of the secondary combustion chamber 29.
Wherein, since the primary combustion chamber 20 mainly performs combustion of pyrolysis products and carbon residue, the combustion temperature is very high, and low-calorie waste gas and/or low-calorie waste liquid and/or waste water are rapidly evaporated and decomposed in the primary combustion chamber 20, which is advantageous for controlling the temperature of the primary combustion chamber 20 and sufficiently combusting organic matter. Preferably, the bottom of the primary combustion chamber 20 is provided with a fluidization structure 22 above the primary air inlet 21, so that the primary air is introduced into the primary combustion chamber 20 from the bottom of the fluidization structure 22 through the primary air inlet 21, thereby completely burning the pyrolyzed solid particles such as carbon residue in the primary combustion chamber 20, and the ash ignition loss is less than 3%.
In addition, flue gas escaping from the top of the secondary combustion chamber 29 can be connected to the recirculating flue gas interface 23 after being treated by external equipment, and then enters the primary combustion chamber for deep combustion treatment.
Preferably, in step S1, the amount of primary air in the pyrolysis section is controlled so that the air-fuel ratio in the pyrolysis section 1 is maintained at 0.6 to 0.9 and the temperature is 1200 ℃. The temperature is preferably 1200-1350 ℃, and the specific temperature control is adjusted according to the composition of liquid, solid and three wastes of the treated gas, so that the ammonia nitrogen in the raw material is inhibited from being converted into NOx, and the NOx contained in the waste gas is converted into N2。
Preferably, in step S2, the temperature in the primary combustion chamber is maintained at 950 to 1200 ℃ by controlling the amounts of the wastewater, the low calorific value waste liquid, the low calorific value waste gas, the recirculated flue gas, and the primary air. The specific temperature control is adjusted according to the composition of liquid-solid three wastes of the treated gas.
Preferably, in step S2, the temperature in the secondary combustion chamber 29 is maintained at 850 to 1100 ℃ by controlling the amount of secondary air, and the specific temperature control is adjusted according to the composition of the waste gas and liquid to be treated; the oxygen content in the secondary combustion chamber 29 is kept between 1 and 5 percent, and the specific oxygen content is adjusted according to the composition of liquid, solid and three wastes of the treated gas.
For the processing device and the process provided by the above embodiments, the following embodiments were formed by performing the specific project tests:
example 1 comprehensive disposal project for gas, liquid and solid three wastes of certain chemical plant
Raw materials: the combustion raw material comprises 2 kinds of solid waste, 3 kinds of waste liquid and 1 kind of waste gas, and the total nitrogen content of the raw material is 2.67 wt% (calculated by N, excluding N)2Content(s).
Solid waste 1: solid tar
Solid waste 2: waste activated carbon
Waste liquid 1: acrylonitrile waste liquid (containing 5.4 wt% of C)3H5N, the remainder being water)
Waste liquid 2: crude Acrylonitrile liquid (containing 49.13% wt C)2H3N、0.59％wt C3H3N, 2.28% wt HCN, remainder water)
Waste liquid 3: hydrocyanic acid (containing 99.6% wt HCN, the remainder being water)
Exhaust gas 1: air discharged from the absorption column (containing 58 mg/Nm)3 C3H3N、926mg/Nm3 NO2、88.34％wt N21.03% wt CO, the remainder being inert gas, oxygen, water)
A combustion processing device: by adopting the device, the pyrolysis section adopts a rotary pyrolysis furnace, the combustion section adopts two combustion chambers to form two-section combustion, and the primary combustion chamber adopts fluidized bed combustion.
Feeding: admittedly useless 1, useless 2 admits into the rotation pyrolysis oven through the batcher through useless entry 12 admits to admittedly, and pyrolysis section is sent into through the waste liquid spray gun through nitrogenous waste liquid entry 14 to high nitrogen waste liquid 1, 2, 3, and pyrolysis section is sent into through the waste gas distributor through nitrogenous waste gas entry 13 to high nitrogen waste gas 1, and the pyrolysis section still sets up the afterburning combustor. Here, after combustion burner's effect preheats and after-combustion (when the pyrolysis temperature is not enough) the pyrolysis oven when starting working, the waste liquid waste gas of easy burning is sent into through the multimedium combustor, and the burning of being difficult to sends into the pyrolysis oven through after combustion burner alone, because waste liquid 1, 2 water are many, and waste liquid 3 is incombustible, and 1 calorific value of waste gas is very low, consequently through setting up an after combustion burner alone, promotes the burning in the pyrolysis section. The primary combustion chamber of the combustion section is provided with a primary air inlet 21 of the combustion section and a recirculated flue gas interface 23, and the contraction type mixing structure 27 at the inlet of the secondary combustion chamber 29 is provided with a secondary air inlet 28 of the combustion section.
The combustion treatment process comprises the following steps: the pyrolysis temperature is controlled to be 1250-1280 ℃, the air-fuel ratio of a pyrolysis section is 0.85, the temperature of a primary combustion chamber is controlled to be 1100-1120 ℃, and the temperature of a secondary combustion chamber is controlled to be 950-1000 ℃.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 220mg/Nm3And the concentration of outlet oxygen is about 3.1%, VOCs cannot be detected, and the NOx conversion rate of the whole raw material nitrogen is about 0.83%.
Example 2: comprehensive disposal project for gas, liquid and solid three wastes of certain chemical plant
Raw materials: same as in example 1.
A combustion processing device: same as in example 1.
Feeding: same as in example 1.
The combustion treatment process comprises the following steps: the pyrolysis temperature is controlled to be 1200-1250 ℃, the air-fuel ratio of the pyrolysis section is 0.85, the temperature of the primary combustion chamber is controlled to be 1050-1100 ℃, and the temperature of the secondary combustion chamber is controlled to be 900-950 ℃.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 185mg/Nm3And the concentration of outlet oxygen is about 3.2%, VOCs cannot be detected, and the NOx conversion rate of the whole raw material nitrogen is about 0.70%.
Example 3: comprehensive disposal project for gas, liquid and solid three wastes of certain chemical plant
Raw materials: same as in example 1.
A combustion processing device: same as in example 1.
Feeding: admittedly useless 1, useless 2 send into the rotation pyrolysis oven through useless entry 12 admittedly through the batcher admittedly, and high nitrogen waste liquid 1, 2, 3 send into the pyrolysis section through the waste liquid spray gun through nitrogenous waste liquid entry 14, and the pyrolysis section still sets up the afterburning combustor. The primary combustion chamber of the combustion section is provided with a primary air inlet 21 of the combustion section and an interface of waste gas 1 (high-nitrogen waste gas 1 is sent into the primary combustion chamber through the interface of the waste gas 1), and a contraction type mixing structure 27 at the inlet of the secondary combustion chamber 29 is provided with a secondary air inlet 28 of the combustion section.
The combustion treatment process comprises the following steps: the pyrolysis temperature is controlled to be 1250-1280 ℃, the air-fuel ratio of the pyrolysis section is 0.7, the temperature of the primary combustion chamber is controlled to be 1050-1100 ℃, and the temperature of the secondary combustion chamber is controlled to be 900-950 ℃.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 430mg/Nm3And the concentration of outlet oxygen is about 4.3%, VOCs cannot be detected, and the NOx conversion rate of the whole raw material nitrogen is about 1.62%.
Example 4: comprehensive disposal project for gas, liquid and solid three wastes of certain chemical plant
Raw materials: same as in example 1.
A combustion processing device: same as in example 1.
Feeding: same as in example 3.
The combustion treatment process comprises the following steps: the pyrolysis temperature is controlled to be 1250-1280 ℃, the air-fuel ratio of a pyrolysis section is 0.7, the temperature of a primary combustion chamber is controlled to be 1050-1065 ℃, and the temperature of a secondary combustion chamber is controlled to be 950-1000 ℃.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 300mg/Nm3And the concentration of outlet oxygen is about 3.2%, VOCs cannot be detected, and the NOx conversion rate of the whole raw material nitrogen is about 1.13%.
Example 5: comprehensive disposal project for gas, liquid and solid three wastes of certain chemical plant
Raw materials: comprises 1 kind of solid waste, 5 kinds of waste liquid and 3 kinds of waste gas, and the total nitrogen content of the raw materials is 2.34 wt% (calculated by N, excluding N)2Content(s).
Solid waste 1: sludge (70% water, ammonia nitrogen 2000mg/kg)
Waste liquid 1: DMC purified lights (containing 41.95% wt MF, 49.14% wt ML, 8.4% wt ME, 0.51% wt DMC)
Waste liquid 2: DMC purification of heavies (containing 60% wt DMC, 40% wt DMO)
Waste liquid 3: ethylene glycol light component (containing 20.74% by weight of methyl glycolate, 30.99% by weight of butanediol, 27.57% by weight of ethylene glycol, 0.01% by weight of diethylene glycol, the remainder being water)
Waste liquid 4: ethylene glycol heavies (67.94% wt ethylene glycol, 14.26% wt triethylene glycol, 11.7% wt propylene glycol, 2.42% wt diethylene glycol, 3.68% wt ethylene carbonate)
Waste liquid 5: ethanol column wastewater (containing 4.78 wt% pentanol, 10.88 wt% ethylene glycol, 0.34 wt% ethanol, 0.26 wt% n-propanol, 1.13 wt% butanol, 0.7 wt% ethylene glycol monomethyl ether, the remainder being water)
Exhaust gas 1: MN recovery column vent gas (containing 1.25% wt methyl nitrite, 2.96% wt NO, 1.2% wt N)2O, 0.63% wt ML, 0.83% wt ME, 12.42% wt CO, the remainder being inert gas N2And CO2)
Exhaust gas 2: shift stripper acid gas component (containing 22.5 wt% ammonia, 14.32 wt% H)2S、0.01％wt H20.05% wt CO, the remainder being CO2And steam)
Exhaust gas 3: DMC plant offgas (containing 42.81% wt methyl nitrite, 1.08% wt NO, 2.47% wt N2O、0.69％wt CO、1.48％wt CH3Cl, 4.04% wt DME, 7.52% wt ML with the remainder being N2、CO2And steam)
A combustion processing device: by adopting the device of the invention, namely: the pyrolysis section adopts a rotary pyrolysis furnace, the combustion section adopts two combustion chambers to form two-section combustion, and the primary combustion chamber adopts fluidized bed combustion.
Feeding: the solid waste 1 is sent into the rotary pyrolysis section through the feeder, the high-heat value waste liquid 1, 2, 3, 4 is sent into the pyrolysis section through the waste liquid spray gun of the multi-medium burner panel, and the high- nitrogen waste gas 1, 2, 3 is sent into the pyrolysis section through the waste gas distributor. The primary combustion chamber of the combustion section is provided with a primary air inlet 21 of the combustion section, a recycling flue gas interface 23 and a waste liquid 5 interface (the waste liquid 5 is sent into the primary combustion chamber), and a contraction type mixing structure 27 at the inlet of the secondary combustion chamber 29 is provided with a secondary air inlet 28 of the combustion section.
The combustion treatment process comprises the following steps: the pyrolysis temperature is controlled to be 1250-1300 ℃, the air-fuel ratio of the pyrolysis section is 0.6, the temperature of the primary combustion chamber is controlled to be 1100-1120 ℃, and the temperature of the secondary combustion chamber is controlled to be 1050-1065 ℃.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 125mg/Nm3And the concentration of outlet oxygen is about 3.5%, VOCs cannot be detected, and the NOx conversion rate of the whole raw material nitrogen is about 0.66%.
Example 6: incineration project for waste gas and waste liquid of certain chemical plant
Raw materials: same as in example 5.
A combustion processing device: same as in example 5.
Feeding: same as in example 5.
The combustion treatment process comprises the following steps: the pyrolysis temperature is controlled to be 1200-1250 ℃, the air-fuel ratio of a pyrolysis section is 0.65, the temperature of a primary combustion chamber is controlled to be 1050-1065 ℃, and the temperature of a secondary combustion chamber is controlled to be 950-1000 ℃.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 110mg/Nm3And the concentration of outlet oxygen is about 3.0%, VOCs cannot be detected, and the NOx conversion rate of the whole raw material nitrogen is about 0.58%.
Example 7: incineration project for waste gas and waste liquid of certain chemical plant
Raw materials: same as in example 5.
A combustion processing device: same as in example 5.
Feeding: the solid waste 1 is sent into the rotary pyrolysis furnace through the feeder, and high calorific value waste liquid 1, 2, 3, 4 are sent into the pyrolysis section through high calorific value waste liquid entry 15 through the waste liquid spray gun of multimedium combustor panel, and high nitrogen waste gas 1, 2, 3 are sent into the pyrolysis section through the waste gas distributor through nitrogenous waste gas entry 13. The primary combustion chamber of the combustion section is provided with a primary air inlet 21 of the combustion section, a recirculation flue gas interface 23, a waste gas 2 interface and a waste liquid 5 interface, and a contraction type mixing structure 27 at the inlet of a secondary combustion chamber 29 is provided with a secondary air inlet 28 of the combustion section.
The combustion treatment process comprises the following steps: the pyrolysis temperature is controlled to be 1300-1350 ℃, the air-fuel ratio of a pyrolysis section is 0.60, the temperature of a primary combustion chamber is controlled to be 1100-1120 ℃, and the temperature of a secondary combustion chamber is controlled to be 1000-1050 ℃.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 150mg/Nm3The outlet oxygen concentration is about 3.2%, VOCs cannot be detected, and the NOx conversion rate of the whole raw material nitrogen is about 0.79%.
Example 8: incineration project for waste gas and waste liquid of certain chemical plant
Raw materials: same as in example 5.
A combustion processing device: same as in example 5.
Feeding: same as in example 7.
The combustion treatment process comprises the following steps: the pyrolysis temperature is controlled to be 1200-1250 ℃, the air-fuel ratio of a pyrolysis section is 0.60, the temperature of a primary combustion chamber is controlled to be 1050-1100 ℃, and the temperature of a secondary combustion chamber is controlled to be 950-1000 ℃.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 100mg/Nm3The outlet oxygen concentration is about 2.7%, VOCs cannot be detected, and the NOx conversion rate of the whole raw material nitrogen is about 0.53%.
Example 9: burning of waste gas and waste liquid containing high nitrogen in a certain factory.
Raw materials: the combustion feed contained 4 streams of waste liquor and 2 streams of waste gas, the total nitrogen content of the feed being 2.35% wt (calculated as N, excluding N)2Content(s).
Waste liquid 1: MMA apparatus waste acid (containing 52.2% wt of ammonium bisulfate, 7.4% wt of MAA, 17.4% wt of sulfuric acid, the remainder being water),
waste liquid 2: acrylonitrile plant waste acid (containing 39.5 wt% ammonium sulfate, 21 wt% acrylic acid, 14.5 wt% C)6H8N2The rest is water),
waste liquid 3: waste acid from the alkylation unit (containing 91% wt sulfuric acid, 8.2% wt N-C)5H1Acrylic acid and the balance of water),
waste liquid 4: MMA apparatus wastewater (containing 0.4% wt sulfuric acid, 1% wt MMA, 4.4% wt acetone, remainder water).
Exhaust gas 1: MMA plant off-gas (containing 26.7% v CO, 4.2% v MMA, 12.4% v acetone, 5.8% v methanol, 30.4% v C2H6O，14.5％v N2，3.5％v SO2The rest is inert gas, oxygen and water
Exhaust gas 2: h2S gas (containing 95% v H)2S, 0.08 percent v C1+ C2+ C3, and the balance of inert gas, oxygen and water)
A combustion processing device: this embodiment is because there is not solid waste material, consequently optimizes pyrolysis section and combustion section, and the pyrolysis section adopts fixed pyrolysis oven, and fluidized structure is cancelled to the combustion section, only adopts the segmentation burning, sets up primary combustion chamber and postcombustion chamber and is located the contraction type mixed structure 27 between the two.
Feeding: high nitrogen waste liquid 1, 2, 3 send into the pyrolysis section through the nitrogen waste liquid entry 14 through the waste liquid spray gun, and high nitrogen waste gas 1 and waste gas 2 send into the pyrolysis section through the waste gas spray gun through nitrogen waste gas entry 13, and the pyrolysis section sets up the afterburning combustor. The primary combustion chamber 20 of the combustion section is provided with a primary air inlet 21 of the combustion section and a waste liquid 4 interface, and the contraction type mixing structure 27 at the inlet of the secondary combustion chamber 29 is provided with a secondary air inlet 28 of the combustion section.
The combustion treatment process comprises the following steps: the temperature of the pyrolysis section is controlled to be 1250-1280 ℃, the air-fuel ratio of the pyrolysis section is 0.70, the temperature of a primary combustion chamber of the combustion section is controlled to be 1150-1180 ℃, and the temperature of a secondary combustion chamber is controlled to be 1065-1080 ℃.
The treatment effect is as follows: concentration of NOx in flue gas at outlet of incinerator: 180mg/Nm3And the concentration of outlet oxygen is about 2.1%, VOCs cannot be detected, and the NOx conversion rate of the whole raw material nitrogen is about 0.76%.
Example 10: burning of waste gas and waste liquid containing high nitrogen in a certain factory.
Raw materials: same as in example 9.
A combustion processing device: same as in example 9.
Feeding: same as in example 9.
The combustion treatment process comprises the following steps: the pyrolysis temperature is controlled to be 1260-1300 ℃, the air-fuel ratio of the pyrolysis section is 0.80, the temperature of the combustion chamber is controlled to be 1170-1200 ℃, and the temperature of the secondary combustion chamber is controlled to be 1065-1080 ℃.
The treatment effect is as follows: concentration of NOx in flue gas at outlet of incinerator: 260mg/Nm3And the concentration of outlet oxygen is about 2.3%, and VOCs cannot be detected. Nitrogen of the whole raw materialThe NOx conversion of (a) is about 1.10%.
Comparative example 1: incineration project for waste gas and waste liquid of certain chemical plant
Raw materials: comprises 2 waste liquids and 2 waste gases, and the total nitrogen content of the raw materials is 2.5 percent by weight (calculated by N, excluding N)2Content(s).
Waste liquid 1: DMC purified lights (containing 41.95% wt MF, 49.14% wt ML, 8.4% wt ME, 0.51% wt DMC)
Waste liquid 2: DMC purification of heavies (containing 60% wt DMC, 40% wt DMO)
Exhaust gas 1: MN recovery column vent (containing 0.6% v methyl nitrite, 2.9% v NO, 0.8% v N)2O, 0.24% v ML, 0.76% v ME, 13.02% v CO, the remainder being inert gas N2And CO2)
Exhaust gas 2: DMC device offgas (containing 31.2% v methyl nitrite, 1.6% v NO, 2.5% v N)2O、 1.1％v CO、1.3％v CH3Cl, 2.9% v DME, 4.4% v ML, remainder N2、CO2And steam)
A combustion processing device: a two-stage furnace comprising a precombustion chamber and a burnout chamber.
Feeding: the exhaust gases 1, 2 and the waste fluids 1, 2 are injected into the prechamber through the panels of the multimedia burner.
The combustion treatment process comprises the following steps: and controlling the combustion temperature of the burnout chamber to be 1100-1150 ℃.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 11100mg/Nm3With an outlet oxygen concentration of about 6.0%, the non-methane total hydrocarbon operation may occasionally exceed 20mg/Nm3The NOx conversion of the total feed nitrogen was about 43.6%.
Comparative example 2: incineration project for waste gas and waste liquid of certain chemical plant
Raw materials: the treated raw material contained 1 waste liquid and 1 waste gas, and the total nitrogen content of the raw material was 0.8 wt% (calculated as N, excluding N)2Content(s).
Exhaust gas 1: absorption column vent gas (containing 60 mg/Nm)3 C3H3N、900mg/Nm3 NO2、88.34％wt N21.03 wt% CO, the remainder being inert gas, oxygen, water) high nitrogen exhaust gas
Waste liquid 1: acrylonitrile waste liquid (containing 5.4 wt% of C)3H5N, the remainder being water)
A combustion processing device: a two-stage furnace comprising a precombustion chamber and a burnout chamber.
Feeding: the flue gas 1 and the waste liquid 1 are injected into the prechamber through the multimedia burner panel.
The combustion treatment process comprises the following steps: and controlling the combustion temperature of the burnout chamber to be 1100-1150 ℃.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 3950mg/Nm3With an outlet oxygen concentration of about 6.1%, the non-methane total hydrocarbon operation may occasionally exceed 20mg/Nm3The overall feed nitrogen NOx conversion was about 50.5%.
It should be noted that the above embodiments can be freely combined as necessary. The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.

Claims (10)

1. The utility model provides a heterogeneous attitude burning processing apparatus of nitrogenous raw materials which characterized in that:
comprises a pyrolysis section and a combustion section which are connected into a whole;
one end of the pyrolysis section is respectively provided with a multi-medium burner and a plurality of nitrogen-containing raw material inlets; the multi-medium burner is respectively provided with a plurality of inlets for introducing high-calorific-value waste gas and liquid and air for combusting the high-calorific-value waste gas and liquid;
the combustion section comprises a plurality of communicated combustion chambers and is used for gradually combusting and purifying pyrolysis products; the other end of the pyrolysis section is connected to one of the combustion chambers.
2. The multiphase combustion processing device of a nitrogen-containing feedstock as set forth in claim 1, characterized in that:
the pyrolysis section adopts a rotary pyrolysis furnace or a fixed pyrolysis furnace, and the multi-medium burner is fixed at one end of the rotary pyrolysis furnace or the fixed pyrolysis furnace;
and/or;
the multi-medium burner is provided with a high-calorific-value waste liquid inlet, a high-calorific-value waste gas inlet and a pyrolysis section primary air inlet;
and/or;
the nitrogen-containing raw material inlet comprises any one or more of a solid waste inlet, a nitrogen-containing waste gas inlet and a nitrogen-containing waste liquid inlet.
3. The multiphase combustion processing device of a nitrogen-containing feedstock as set forth in claim 1, characterized in that:
the combustion section comprises a primary combustion chamber and a secondary combustion chamber which are communicated with each other inside, and the secondary combustion chamber is positioned on the upper side of the primary combustion chamber;
the primary combustion chamber is communicated with the other end of the pyrolysis section, which is far away from the medium burner.
4. The multiphase combustion processing unit of a nitrogen-containing feedstock as recited in claim 3, wherein:
and a combustion section primary air inlet is formed in the bottom of the primary combustion chamber.
5. The multiphase combustion processing unit of a nitrogen-containing feedstock as recited in claim 4, wherein:
a fluidization structure or a flow guide structure is arranged at the bottom of the primary combustion chamber above the primary air inlet of the combustion section, wherein the fluidization structure is provided with fluidized bed materials; the flow guide structure adopts a flow guide plate or a flow guide grid.
6. The multiphase combustion processing device of a nitrogen-containing feedstock as claimed in claim 4 or 5, characterized in that:
the outer wall of the primary combustion chamber is provided with an external interface which comprises any one or a combination of a recirculation flue gas interface, a low-heat-value waste liquid interface and a waste water interface; wherein, the flue gas of the burning section is escaped from the top, is connected to a recirculating flue gas interface after heat recovery and purification.
7. The multiphase combustion processing unit of a nitrogen-containing feedstock as recited in claim 5, wherein:
the inlet of the secondary combustion chamber is communicated with a contraction type mixing structure, and the contraction type mixing structure is positioned between the primary combustion chamber and the secondary combustion chamber; and a secondary air interface of a combustion section is arranged on the throat contraction section of the contraction type mixing structure.
8. A multiphase combustion treatment process of a nitrogen-containing raw material is characterized by comprising the following steps:
s1, feeding solid waste substances and/or nitrogen-containing waste gas and/or nitrogen-containing waste liquid into a pyrolysis section through corresponding inlets for pyrolysis treatment, and feeding high-heat-value waste gas and waste liquid and primary air of the pyrolysis section into the pyrolysis section through a multi-medium burner for combustion to provide heat for high-temperature pyrolysis of nitrogen-containing raw materials in the pyrolysis section;
and S2, enabling pyrolysis products of the pyrolysis section to enter a plurality of combustion chambers of the combustion section, combusting and purifying the pyrolysis products step by step, and enabling purified flue gas to escape from the top of the combustion section.
9. The multiphase combustion process of claim 8, wherein:
in step S2, the combustion section comprises a primary combustion chamber, a contraction type mixing structure and a secondary combustion chamber which are sequentially arranged from bottom to top;
the pyrolysis product firstly enters a primary combustion chamber, primary air is introduced into the bottom of the primary combustion chamber through a primary air inlet of a combustion section, meanwhile, waste water and/or low-heat-value waste gas and/or low-heat-value waste liquid introduced from the outside are converted into gaseous substances in the primary combustion chamber by using the high temperature of the pyrolysis product, and then are uniformly mixed with the pyrolysis product and the primary air, so that the waste water and/or the low-heat-value waste gas and/or the low-heat-value waste liquid and the pyrolysis product are fully combusted in the primary combustion chamber, and the combusted flue gas escapes to a contraction type mixing structure;
the throat contraction section of the contraction type mixing structure is provided with a combustion section secondary air interface, secondary air and smoke coming from the primary combustion chamber are intensively mixed at the contraction type mixing structure and then upwards enter the secondary combustion chamber, so that unreacted combustible materials in the pyrolysis section and the primary combustion chamber are completely combusted in the secondary combustion chamber, and then the smoke escapes from the top of the secondary combustion chamber.
10. The multiphase combustion process of claim 9, wherein:
in step S1, controlling the primary air quantity in the pyrolysis section to keep the air-fuel ratio in the pyrolysis section between 0.6 and 0.9 and the temperature between 1200 and 1350 ℃;
and/or;
in step S2, the temperature in the primary combustion chamber is kept at 950 ℃ to 1200 ℃ by controlling the waste water and/or the low-heat-value waste liquid and/or the low-heat-value waste gas and the primary air amount;
and/or;
in step S2, the temperature in the secondary combustion chamber is maintained at 850 to 1100 ℃ and the oxygen content is maintained at 1 to 5% by controlling the amount of secondary air.
CN202010968229.XA 2020-09-15 2020-09-15 Combustion treatment device and process for nitrogen-containing raw material Pending CN111928251A (en)

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