CN216448160U - Multi-chamber type multiphase low-nitrogen combustion treatment device - Google Patents
Multi-chamber type multiphase low-nitrogen combustion treatment device Download PDFInfo
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- CN216448160U CN216448160U CN202122598517.3U CN202122598517U CN216448160U CN 216448160 U CN216448160 U CN 216448160U CN 202122598517 U CN202122598517 U CN 202122598517U CN 216448160 U CN216448160 U CN 216448160U
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Abstract
The utility model discloses a multi-chamber multiphase low-nitrogen combustion treatment device, which comprises: the shell is internally divided into a plurality of hearths; the multiple hearths comprise a combustion hearth, a drying hearth, a pyrolysis hearth, a residue combustion hearth and a cooling hearth which are respectively arranged from top to bottom, and the multiple hearths are sequentially communicated; wherein, the center of casing runs through and is provided with and is used for carrying out the compounding and pay-off to the feeding mechanism of lower floor furnace to at least one furnace except that burning furnace. This setting makes solid waste need not to handle through the dry direct furnace that sends into of going into, still can the simultaneous coprocessing waste gas, waste liquid, waste water, realize the gaseous-liquid-solid integration heterogeneous low-nitrogen combustion, especially can carry out integration heterogeneous low-nitrogen combustion processing to the three wastes of high moisture content, high raw materials nitrogen, can reduce the NOx conversion rate of raw materials nitrogen to below 5%, and furnace outlet flue gas oxygen content control is within 1 ~ 6%, reduce flue gas volume and flue gas purification cost, realize better social and economic benefits.
Description
Technical Field
The utility model belongs to the technical field of environmental protection, and relates to a multi-chamber multi-phase low-nitrogen combustion treatment device.
Background
Some large petrochemical enterprises or industrial parks need to treat solid waste, organic waste liquid and organic waste gas simultaneously, wherein some solid waste has very high water content and very low calorific value, such as sludge, oil sludge, filter cakes and the like, the waste liquid and the waste gas have very complex components, some contain high nitrogen and some contain no nitrogen basically, some contain high content of combustible components and have high calorific value, and some contain little combustible components and have very low calorific value. At present, the conventional treatment mode is that solid waste with high water content is dried and then sent into a rotary kiln for incineration, waste liquid or waste gas with high calorific value is sent into a solid waste treatment secondary combustion chamber for incineration or a newly-built waste gas and waste liquid incinerator for incineration, and low calorific value waste gas is treated by means of catalytic oxidation or regenerative oxidation and the like. This results in several sets of different types of incineration treatment devices being required to be built for different three wastes in one park or one petrochemical enterprise, which increases investment and operation and management costs.
In solid waste, waste liquid and waste gas of petrochemical enterprises, the content of ammonia nitrogen is high frequently, the proportion of the ammonia nitrogen in the current hazardous waste incineration system fuel converted into NOx is generally between 20% and 50%, the conversion rate of 20% to 50% is still too high for a plurality of organic wastes with high ammonia nitrogen content, the investment of subsequent flue gas denitration is large, the medicament consumption is high, and the operation cost is high.
Chinese patent document CN2020220148411 discloses a combustion treatment device and process for nitrogen-containing raw materials, which adopts a combination of a fixed/rotary pyrolysis furnace and a secondary combustion chamber to perform heterogeneous combustion of the nitrogen-containing raw materials, wherein the fixed pyrolysis furnace can only treat powdery solid waste, and the rotary pyrolysis furnace generally treats solid waste with a water content of less than or equal to 60%. When the material is a high-moisture material (with more than 80% of moisture), the rotary pyrolysis furnace can only be provided with burners at two ends, so that the temperature field of the pyrolysis furnace is not uniform, slag bonding is easily caused, and solid waste is usually required to be dried to a certain degree in advance before being sent into the rotary pyrolysis furnace for treatment.
Chinese patent document CN202010395972.0 discloses a system for treating solid waste by using a multi-hearth furnace, which adopts various solid wastes to be respectively dried and then sent into the multi-hearth furnace system, and uses a traditional multi-hearth furnace to treat, and the treatment processes such as low nitrogen and the like are not performed in the furnace, and the treated waste is only solid waste, so that the problem of gas-liquid-solid integrated multiphase low nitrogen combustion at present cannot be solved.
Disclosure of Invention
In view of the problems in the prior art, an object of the present invention is to provide a multi-chamber multiphase low-nitrogen combustion processing apparatus, which is optimally designed based on a conventional multi-chamber furnace, so that solid waste can be directly sent to the furnace chamber for disposal without drying, and waste gas, waste liquid and waste water can be cooperatively processed at the same time, thereby realizing gas-liquid-solid integrated multiphase low-nitrogen combustion. The device and the process can particularly carry out integrated multiphase low-nitrogen combustion treatment on three wastes with high water content and high raw material nitrogen, can reduce the NOx conversion rate of the raw material nitrogen to below 5%, controls the oxygen content of the flue gas at the outlet of a hearth to be within 1-6%, reduces the flue gas amount and the flue gas purification cost, and realizes better social and economic benefits.
The utility model aims to provide a multi-chamber multi-phase low-nitrogen combustion treatment device, which adopts the following technical scheme:
a multi-chamber multiphase low-nitrogen combustion treatment device comprises:
the shell is internally divided into a plurality of hearths; the multiple hearths comprise a combustion hearth, a drying hearth, a pyrolysis hearth, a residue combustion hearth and a cooling hearth which are respectively arranged from top to bottom, and the multiple hearths are sequentially communicated;
the center of the shell is provided with a feeding mechanism which is used for mixing materials of at least one hearth except the combustion hearth and feeding the materials to the lower hearth in a penetrating mode.
Preferably, the combustion furnace chamber and the drying furnace chamber are separated by a porous distribution plate, and the surface of the porous distribution plate is uniformly distributed with spaced holes.
Furthermore, a plurality of layers of supporting pieces are arranged on the lower side of the porous distribution plate in the shell, and a hearth is formed between every two adjacent supporting pieces; and, either layer of the support member forms a blanking portion at the center of the housing or at the inner side wall of the housing.
Furthermore, the multilayer supporting piece alternately forms blanking parts at the center of the shell and on the inner side wall of the shell.
Furthermore, a refractory material is built on the supporting piece.
Further, when the blanking part is positioned between the rotating shaft and the supporting piece, the blanking part is set to be a circular hole in the center of the shell; when the blanking portion is located between the inner wall of the shell and the supporting piece, a plurality of square holes are uniformly distributed on the outer peripheral surface of the hearth by the blanking portion.
Further, the feeding mechanism comprises a rotating shaft penetrating through the center of the shell and a rake arm arranged on the rotating shaft; rake teeth are arranged on the rake arm at intervals, and the rotating shaft is in driving connection with a power source;
the rake teeth are arranged above the supporting piece, so that the rake teeth can push blanking on the supporting piece.
Furthermore, the rotating shaft is a double-layer hollow rotating shaft comprising an inner layer shaft and an outer layer shaft, a cooling air inlet and a cooling air outlet are arranged on the double-layer hollow rotating shaft, the cooling air inlet is connected with the inner layer shaft, and the cooling air outlet is connected with the outer layer shaft;
the double-layer hollow rake arm comprises an inner layer rake arm and an outer layer rake arm, the inner layer rake arm of the double-layer hollow rake arm is communicated with an inner layer shaft of the double-layer hollow rotating shaft, and the outer layer rake arm of the double-layer hollow rake arm is communicated with an outer layer shaft of the double-layer hollow rotating shaft;
wherein, spouts are distributed on the inner layer harrow arm of the double-layer hollow harrow arm.
Furthermore, the rake teeth and the inclination angle are arranged on the rake arm, and the material pushing direction of the rake teeth in the hearth is consistent with the direction of the rake teeth entering the lower hearth by controlling the inclination angle of the rake arm and the rake teeth.
Further, when the support piece forms a blanking part at the center of the shell, the blanking part is positioned between the rotating shaft and the support piece, and the blanking part is provided with a circular hole at the center of the shell; for the rake teeth on the layer of supporting piece, the number of the rake teeth pushing towards the center of the hearth is more than that of the rake teeth pushing towards the periphery of the hearth;
when the support piece forms a blanking part on the inner side wall of the shell, the blanking part is positioned between the inner wall of the shell and the support piece, and a plurality of square holes are uniformly distributed on the outer peripheral surface of the hearth by the blanking part; for the rabble teeth on the layer of supporting piece, the number of the rabble teeth pushed to the periphery of the hearth is more than that pushed to the center of the hearth.
Preferably, a low-heat-value waste liquid inlet, a combustion air inlet and a flue gas outlet are formed in the combustion hearth;
a solid waste inlet and a waste water inlet are arranged on the drying hearth;
combustion-supporting air inlets are formed in the pyrolysis hearth and the residue combustion hearth;
a combustion-supporting air inlet, a low-calorific-value waste gas inlet and a slag discharge port are formed in the cooling hearth;
the multi-media burners corresponding to the pyrolysis hearth are respectively provided with combustion-supporting air, nitrogen-containing waste gas, nitrogen-containing waste liquid and auxiliary fuel inlets; the multi-medium burner corresponding to the combustion hearth, the drying hearth and the residue combustion hearth is respectively provided with a combustion-supporting air inlet, a high-heat-value waste gas inlet, a high-heat-value waste liquid inlet and an auxiliary fuel inlet.
Based on the device provided by the utility model, a multi-chamber multi-phase low-nitrogen combustion treatment process can also be provided, and the process comprises the following steps:
s1, sending the low-heat-value waste liquid into a combustion hearth of the multi-hearth furnace through a corresponding inlet for treatment; the waste water is sent into a drying hearth of a plurality of hearths through corresponding inlets for evaporation treatment; solid waste substances are sent into a drying furnace chamber of a plurality of furnace chambers through corresponding inlets, the dried solid waste substances are sent into a pyrolysis furnace chamber through a feeding mechanism, and nitrogen-containing waste gas and/or nitrogen-containing waste liquid are sent into the pyrolysis furnace chamber through corresponding inlets for pyrolysis treatment;
s2, gaseous pyrolysis products generated by the pyrolysis hearth enter the combustion furnace hearth at the topmost layer through the drying hearth at the upper layer for combustion, solid pyrolysis products generated by the pyrolysis hearth enter the residue combustion furnace hearth at the lower layer for combustion through the feeding mechanism, and heat generated in the combustion process is supplied to the pyrolysis hearth at the upper layer for pyrolysis treatment, so that the pyrolysis products are completely combusted and purified through the combustion hearth arranged from top to bottom and the residue combustion hearth, and obtained ash residues are discharged after being subjected to heat exchange utilization by cooling hearth through the feeding mechanism.
Preferably, the secondary air is fed into a combustion hearth, the low-calorific-value waste liquid is sprayed into the combustion hearth, the combustion hearth is also provided with a multi-medium burner and a flue gas outlet, the high-calorific-value waste liquid and the high-calorific-value waste gas are combusted through the multi-medium burner, the temperature of the combustion hearth is controlled to be 850-1150 ℃, the oxygen content in the combustion hearth is controlled to be 1-6% by adjusting the feeding amount of the secondary air, so that the waste liquid, the waste gas and combustible components in the escaping gas of the lower hearth are completely combusted in the combustion hearth, and the combusted flue gas is discharged from the flue gas outlet 105 of the combustion hearth.
Preferably, the solid waste is fed into a drying hearth, the wastewater is sprayed into the drying hearth, and the drying hearth is also provided with a multi-medium burner and a blanking port; the waste liquid and the waste gas with high heat value are combusted through a multi-medium combustor, so that the solid waste is completely dried in a drying hearth; and the dried solid waste is subjected to material mixing and feeding by a feeding mechanism and then is discharged from a blanking port.
Preferably, the dried solid waste falls into the pyrolysis furnace from the blanking port of the upper layer drying furnace, secondary air enters the pyrolysis furnace, and the pyrolysis furnace is provided with multi-medium combustionA device and a blanking port; the method comprises the steps of burning waste liquid and waste gas containing nitrogen in a pyrolysis hearth through a multi-medium burner, controlling the temperature of the pyrolysis hearth to be 900-1300 ℃, controlling the air-fuel ratio in the pyrolysis hearth to be 0.6-0.9 by adjusting the entering amount of secondary air, carrying out pyrolysis reaction on the waste gas containing nitrogen and the waste liquid containing nitrogen in a high-temperature oxygen-deficient environment, and converting raw material nitrogen in the waste gas and the waste liquid into N in a reductive atmosphere2The NOx of the exhaust gas itself is also reduced to N in a reducing atmosphere2(ii) a And the solid pyrolysis product is mixed and fed by a feeding mechanism and then discharged from a blanking port.
Preferably, the solid pyrolysis product falls into the residue combustion furnace from a blanking port of the upper pyrolysis furnace, secondary air enters the residue combustion furnace, and the residue combustion furnace is provided with a multi-medium burner and a blanking port; burning high-heat waste liquid and waste gas in a residue combustion furnace chamber through a multimedia burner, controlling the temperature of the residue combustion furnace chamber to be 850-1100 ℃, and controlling the oxygen content of the residue combustion furnace chamber to be 3-6% by adjusting the amount of air entering from a secondary air inlet; the waste liquid, the waste gas and the solid pyrolysis product are completely combusted in the hearth of the residue combustion furnace; and discharging the residue from the blanking port after the residue is mixed and fed by the feeding mechanism.
Preferably, ash residues left after the combustion of the residue combustion furnace tank fall into the cooling furnace tank from a material dropping port of the upper residue combustion furnace tank, primary air and low-calorific-value waste gas are fed into the cooling furnace tank, and the cooling furnace tank is also provided with a slag discharging port; ash and slag carry out direct contact type heat exchange with primary air and low-calorific-value waste gas in a cooling hearth, the preheated primary air and the low-calorific-value waste gas flow upwards, sequentially pass through a residue combustion hearth, a pyrolysis hearth, a drying hearth and a combustion hearth, and participate in combustion reaction in the residue combustion hearth, the pyrolysis hearth and the combustion hearth; the ash slag is discharged through a slag discharge port after the temperature of the ash slag is reduced. The oxygen content and the temperature parameter of each hearth can meet the requirements by controlling the amount of primary air and low-heat-value waste gas and the secondary air of each hearth and the power of the multi-medium burner.
The utility model has the beneficial effects that:
1) according to the utility model, by adopting a multi-hearth structure, comprising a plurality of hearths such as a combustion hearth, a drying hearth, a pyrolysis hearth, a residue combustion hearth, a cooling hearth and the like, raw materials can be dried, pyrolyzed and combusted step by step, so that not only can waste gas, waste liquid and waste water with various heat values and compositions be treated, but also various high-water-content solid wastes can be treated simultaneously, and the raw materials have very strong adaptability; the integrated multiphase combustion disposal of gas, liquid and solid three wastes can be realized, the disposal flow of solid waste, waste liquid and waste gas is shortened, especially the disposal of high-water-content solid waste (the water content is more than 80 percent), the occupied area and the investment of equipment are reduced, and the method is suitable for industrial popularization.
2) According to the utility model, through a multi-hearth structure, the advantages of drying, pyrolysis and combustion processes are effectively combined, the conversion rate of raw material nitrogen NOx in waste gas, waste liquid and solid waste can be reduced to below 5%, and the reduction rate of NOx in the raw material waste gas is above 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.
3) According to the utility model, through gradual drying, pyrolysis and combustion, complete combustion of materials under low-oxygen combustion can be ensured, the oxygen content of flue gas escaping from the top combustion hearth is controlled within 1-6%, and the thermal ignition loss of ash slag discharged from the bottom is controlled within 1-3%, so that the flue gas quantity and the ash slag quantity are effectively reduced, and better social and economic benefits are realized.
4) The multi-hearth furnace comprises a plurality of hearths such as a combustion hearth, a drying hearth, a pyrolysis hearth, a residue combustion hearth, a cooling hearth and the like, organic matters with different characteristics can be fed into the hearths with different functions, for example, organic matters with low water content and low high heat value can be fed from the drying hearth, and the organic matters in materials can be completely combusted by the mode.
5) According to the utility model, different setting layers can be selected for the drying hearth, the pyrolysis hearth and the residue combustion hearth according to the water content, pyrolysis characteristics and combustion characteristics of the treated materials, so that the material treatment effect is fully ensured.
6) The utility model adopts a specially designed feeding mechanism, and through the structural design of the hollow rotating shaft and the rake arms, the movement direction of the solid waste in the hearth can be adjusted through adjusting the angles of the rake teeth, and the solid waste can be overturned up and down in the furnace through the distribution of the rake teeth with different angles, so that the retention time of the solid waste in the furnace is prolonged. In addition, the residence time of the solid waste can be adjusted by adjusting the rotating speed of the rotating shaft. And ingenious cooperation, let in the cooling air in rotation axis and harrow arm, guarantee the safety of rotation axis and harrow arm.
7) According to the utility model, the burner is independently arranged for each hearth, and the combustion-supporting air is introduced through the combustion-supporting air inlet, so that the temperature and the oxygen content of each hearth can be accurately controlled, and different process requirements can be realized.
Drawings
FIG. 1 is a schematic structural diagram of a multi-chamber multiphase low-nitrogen combustion treatment device of the utility model.
Fig. 2 is an enlarged structural view at a in fig. 1.
The notations in the figures have the following meanings:
1-shell, 2-rotating shaft, 21-outer rotating shaft, 22-inner rotating shaft, 23-shaft cooling air inlet, 24-shaft cooling air outlet, 3-harrow arm, 31-outer harrow arm, 32-inner harrow arm, 4-harrow tooth and 5-speed reducing motor; 10-a combustion hearth, 101-a secondary air inlet, 102-a low-calorific-value waste liquid inlet, 103-a multi-medium burner, 104-a porous distribution plate and 105-a flue gas outlet; 20-a drying hearth, 201-a solid waste inlet, 202-a wastewater inlet, 203-a multi-medium burner and 204-a blanking port; 30-a pyrolysis hearth, 301-a secondary air inlet, 302-a multi-medium burner and 303-a blanking port; 40-a residue combustion hearth, 401-a secondary air inlet, 402-a multi-medium burner and 403-a blanking port; 50-cooling hearth, 501-primary air inlet, 502-low heat value waste gas inlet, 503-slag discharging port.
Detailed Description
The technical solution of the present invention will be clearly and completely described below with reference to specific embodiments. The following examples are only for illustrating the technical solutions of the present invention more clearly, and the protection scope of the present invention is not limited thereby.
According to an embodiment of the present invention, the present invention provides a multi-chamber multiphase low-nitrogen combustion processing apparatus, comprising:
the device comprises a shell 1, a plurality of hearths are formed in the shell in a separated mode; the multiple hearths comprise a combustion hearth 10, a drying hearth 20, a pyrolysis hearth 30, a residue combustion hearth 40 and a cooling hearth 50 which are respectively arranged from top to bottom, and the multiple hearths are sequentially communicated; wherein, the center of the shell 1 is provided with a feeding mechanism which is used for mixing materials of at least one hearth except the combustion hearth 10 and feeding the materials to the lower hearth in a penetrating way.
According to this embodiment's low nitrogen combustion processing of many thorax formulas heterogeneous attitude has a plurality of hearths such as burning furnace, dry furnace, pyrolysis furnace, residue burning furnace, cooling furnace, and each furnace is fire-resistant furnace, can carry out drying, pyrolysis, combustion processing to the raw materials step by step, shortens solid useless, waste liquid, waste gas and deals with the flow, and especially the processing of high water content solid useless (moisture content > 80%), reduces equipment area and investment. And moreover, the arrangement of the feeding mechanism can promote the effective treatment of related procedures in multiple hearths, and the reliability and treatment effect of the device process are improved.
As a preferred embodiment, the combustion furnace 10 and the drying furnace 20 are separated by a porous distribution plate 104, and spaced holes are uniformly distributed on the surface of the porous distribution plate 104, and the preferred pore diameter is 50-150 mm, so that the flue gas of the lower furnace enters the combustion furnace 10 through small holes. In practical application, the porous distribution plate 104 is formed by a support structure and a refractory castable, and the lower layer flue gas enters the combustion furnace 10 from the spacing holes through the spacing holes uniformly distributed on the refractory porous distribution plate 104 which is separated from the combustion furnace 10 and the drying furnace 20. The support structure is typically carbon steel, which is covered with a refractory material.
A plurality of layers of supporting pieces 100 are arranged on the lower side of a porous distribution plate 104 in the shell 1, and each hearth is formed between every two adjacent supporting pieces 100. Referring to fig. 1, a drying furnace 20, a pyrolysis furnace 30, a residue burning furnace 40, and a cooling furnace 50 are sequentially formed at intervals by a plurality of supports 100 from top to bottom in the casing. Specifically, a drying furnace 20 is formed between the porous distribution plate 104 and the support 100 of the first layer, a pyrolysis furnace 30 is formed between the support 100 of the first layer and the support 100 of the second layer, a residue-burning furnace 40 is formed between the support 100 of the second layer and the support 100 of the third layer, and a cooling furnace 50 is formed between the support 100 of the third layer and the support 100 of the fourth layer. It should be noted that different setting layers can be respectively selected for the drying furnace, the pyrolysis furnace and the residue combustion furnace according to the water content of the processed material, the pyrolysis characteristic, the combustion characteristic and the like, so that the material processing effect is fully ensured.
Also, any one of the layer supports 100 forms a blanking portion at the center of the case 1 or at the inner side wall of the case 1. In order to improve the processing effect, the two ends of the multi-layer support 100 alternately form blanking portions at the center of the housing 1 and the inner side wall of the housing 1, and the processing path of the blanking is prolonged. In practical application, referring to fig. 1, each layer of support members 100 (made of refractory material) separated among the drying furnace 20, the pyrolysis furnace 30, the residue combustion furnace 40, and the cooling furnace 50 is respectively provided with a blanking port, the blanking ports are respectively and alternately arranged in the center of the furnace or on the outer side of the furnace, and when the blanking port of the upper furnace is in the center of the furnace, the blanking port of the furnace is on the outer side of the furnace. Therefore, the mass transfer process of the materials in the hearth is increased, and the full implementation of each process is ensured. More specifically, when the blanking portion is located between the rotary shaft 2 and the support 100, the blanking portion is provided as a circular hole in the center of the housing 1; when blanking portion was located between 1 inner wall of casing and support piece 2, blanking portion equipartition was a plurality of for example 6-18 quad slit on the periphery face of furnace, was favorable to carrying out orderly processing step by step to the material.
Based on the foregoing, in order to further improve the treatment effect of the present invention, the feeding mechanism for mixing and conveying the drying furnace 20, the pyrolysis furnace 30, the residue combustion furnace 40, and the cooling furnace 50 is configured to: the device comprises a rotating shaft 2 penetrating through the center of the shell 1 and a rake arm 3 arranged on the rotating shaft 2; rake teeth 4 are arranged on the rake arm 3 at intervals, and the rotating shaft 2 is in driving connection with a power source such as a speed reducing motor 5. Moreover, the rake teeth 4 are arranged above the supporting part 100, so that the rake teeth 4 push the blanking on the supporting part 100, and the full mixing and feeding of the materials on the supporting part 100 are facilitated.
The rotating shaft 2 is a double-layer hollow rotating shaft comprising an inner-layer shaft 21 and an outer-layer shaft 22, a cooling air inlet 23 and a cooling air outlet 24 are arranged on the double-layer hollow rotating shaft, the cooling air inlet 23 is connected with the inner-layer shaft 21, and the cooling air outlet 24 is connected with the outer-layer shaft 22;
the rake arm 3 is a double-layer hollow rake arm comprising an inner layer rake arm 31 and an outer layer rake arm 32, the inner layer rake arm 31 of the double-layer hollow rake arm is communicated with the inner layer shaft 21 of the double-layer hollow rotating shaft, and the outer layer rake arm 32 of the double-layer hollow rake arm is communicated with the outer layer shaft 22 of the double-layer hollow rotating shaft; wherein, the inner layer harrow arm 31 of the double-layer hollow harrow arm 3 is distributed with nozzles 310.
Through the structural matching design of the hollow rotating shaft 2 and the rake arms 3, cooling air is introduced into the rotating shaft 2, so that the cooling air flows into the inner-layer rake arms 31 from the inner-layer shaft 21, then flows into the outer-layer rake arms 32 from the nozzles 310 of the inner-layer rake arms 31, and finally flows into the outer-layer shaft 22 from the outer-layer rake arms 32, and the safety of the rotating shaft 2 and the rake arms 3 is ensured. Preferably, the nozzles are uniformly distributed on the inner layer rake arm 31, so that the cooling air uniformly enters the outer layer rake arm 32 and the cavity of the rotating shaft 2, and the safety and reliability of the rotating shaft 2 and the rake arm 3 are ensured.
Preferably, the rake teeth and the inclination angle are arranged on the rake arm in an adjustable manner, and the material pushing direction of the rake teeth in the hearth is consistent with the direction of the rake teeth entering the lower hearth by controlling the inclination angle of the rake arm and the rake teeth. In this embodiment, the rake teeth 4 and the rake arms 3 are installed at a certain angle, and the movement direction of the solid waste material in the hearth can be changed by adjusting the inclination angle of the rake teeth 3. And preferably, when the support 100 forms a blanking portion at the center of the housing 1, the blanking portion is located between the rotating shaft 2 and the support 100, and the blanking portion is provided as a circular hole at the center of the housing; for the rake teeth 4 arranged on the upper side of the layer of supporting part 100, the number of the rake teeth 4 pushing towards the center of the hearth is more than that of the rake teeth 4 pushing towards the periphery of the hearth; when the support piece 100 forms a blanking part on the inner side wall of the shell 1, the blanking part is positioned between the inner wall of the shell and the support piece, and a plurality of square holes are uniformly distributed on the outer peripheral surface of the hearth of the blanking part; for the rabble teeth 4 on the layer of support 100, the number of rabble teeth pushed towards the periphery of the furnace is greater than the number of rabble teeth pushed towards the centre of the furnace. Based on the technical scheme, when the blanking part of the multi-layer hearth is in the center, the number of the rake teeth pushing the center of the hearth is larger than that of the rake teeth pushing the periphery of the hearth, so that solid wastes integrally move to the center of the hearth while turning back and forth, and finally fall into the lower-layer hearth from the central blanking part; when the blanking portion of the multi-layer hearth is arranged on the outer side, the rake teeth pushing towards the periphery of the hearth are more than the rake teeth pushing towards the center of the hearth, so that solid wastes integrally move towards the periphery of the hearth while turning back and forth, and finally fall into the lower-layer hearth from the blanking portion on the periphery of the hearth, and the step-by-step treatment efficiency of the materials in the hearth is further improved on the basis of ensuring the treatment effect. Usually, the rake arm 3 and the rake teeth 4 are both made of high temperature and wear resistant castings.
More specifically, in order to effectively treat the multi-phase material in the furnace chamber, the following steps are combined as shown in fig. 1:
the casing 1 corresponding to the combustion chamber 10 is provided with a secondary air inlet 101, a low heating value waste liquid inlet 102, a multimedia burner 103 and a combustion flue gas outlet 105. And combustion-supporting air, high-calorific-value waste gas, high-calorific-value waste liquid and auxiliary fuel inlets are respectively arranged on the multi-medium burner 103. More specifically, the combustion flue gas outlet 105 is disposed at the top of the housing, so that the flue gas is exhausted after being sufficiently combusted and utilized in the combustion chamber 10.
A solid waste inlet 201 and a waste water inlet 202 are arranged on the shell corresponding to the drying hearth 20, and are connected with a multi-medium burner 203, and a blanking port 204 is arranged on the supporting piece 100 between the drying hearth 20 and the lower hearth; and a combustion-supporting air inlet, a high-calorific-value waste gas inlet, a high-calorific-value waste liquid inlet and an auxiliary fuel inlet are formed in the multi-medium combustor 203.
A secondary air inlet 301 is arranged on the shell corresponding to the pyrolysis hearth 30, a multi-medium burner 302 is also connected, and a blanking port 303 is arranged on the supporting piece 100 between the pyrolysis hearth 30 and the lower hearth. And a combustion-supporting air inlet, a nitrogen-containing waste gas inlet, a nitrogen-containing waste liquid inlet and an auxiliary fuel inlet are formed in the multi-medium combustor 302.
A secondary air inlet 401 is arranged on the shell corresponding to the residue combustion hearth 40, a multi-medium burner 402 is also connected, and a blanking port 403 is arranged on the supporting piece 100 between the residue combustion hearth 40 and the lower hearth. And a combustion-supporting air inlet, a high-calorific-value waste gas inlet, a high-calorific-value waste liquid inlet and an auxiliary fuel inlet are formed in the multimedia burner 402.
It should be noted that the number of the multi-media burners disposed in the combustion furnace 10, the drying furnace 20, the pyrolysis furnace 30, and the residue combustion furnace 40 is different, and can be adjusted according to the amount of various wastes to be treated and the nature of the waste to be treated, and usually, 1 to 4 multi-media burners are disposed in each furnace.
A primary air inlet 501 and a low-calorific-value waste gas inlet 502 are arranged on the shell corresponding to the cooling hearth 50, and a slag discharging port 503 for blanking is arranged on the supporting piece 100 positioned at the bottom of the cooling hearth 50. As shown in fig. 1, to facilitate the collection of ash, a slag discharge opening 503 is located at the periphery of the cooling hearth 50.
According to the above embodiment, the present invention may further embody a multi-chamber multiphase low-nitrogen combustion treatment process, including the following steps:
s1, sending the low-heat-value waste liquid into a combustion hearth 10 of the multi-hearth furnace through a corresponding inlet for treatment; the waste water is sent into a drying furnace 20 of a plurality of furnaces through corresponding inlets for evaporation treatment; the solid waste materials are sent into a drying hearth 20 of a multi-hearth through corresponding inlets, and the dried solid waste materials are sent into a pyrolysis hearth 30 through a feeding mechanism; the nitrogen-containing waste gas and/or the nitrogen-containing waste liquid are sent to the pyrolysis furnace 30 through corresponding inlets for treatment; wherein, the heat of the pyrolysis furnace 30 is provided by the combustion flue gas of the corresponding multi-medium burner 302 and the lower furnace;
s2, gaseous pyrolysis products generated by the pyrolysis hearth enter the topmost combustion hearth 10 through the drying hearth 20 on the upper layer, solid pyrolysis products generated by the pyrolysis hearth 30 enter the lower-layer residue combustion hearth 40 for combustion, heat generated in the combustion process in the residue combustion hearth is supplied to the upper-layer pyrolysis hearth 30 for pyrolysis treatment, and therefore the pyrolysis products are completely combusted and purified through the combustion hearths 10 and the residue combustion hearth 40 which are arranged up and down, and obtained ash is discharged after being cooled through the cooling hearth 50 and heat exchange of low-calorific-value waste gas and primary air.
The steps are further optimized to respectively obtain better multiphase substance treatment effects:
in the step S1, secondary air (combustion air) is fed into a combustion furnace chamber 10 through a secondary air inlet 101, low-heat-value waste liquid is sprayed into the combustion furnace chamber 10 through a low-heat-value waste liquid inlet 102, the combustion furnace chamber 10 is also provided with a multimedia burner 103 and a flue gas outlet 105, the multimedia burner 103 is provided with interfaces of high-heat-value waste liquid, high-heat-value waste gas, auxiliary fuel and combustion air, the high-heat-value waste liquid and waste gas are combusted through the multimedia burner 103, and the temperature of the combustion furnace chamber is guaranteed to be 850 ℃ -1150 ℃; by adjusting the amount of air entering the secondary air, the oxygen content of the combustion furnace is ensured to be between 1% and 6%, so that the waste liquid, the waste gas and combustible components in the escaping gas (supplementary description below) of the lower-layer furnace are completely combusted in the combustion furnace, and the combusted flue gas is discharged from a flue gas outlet 105 of the combustion furnace.
The solid waste is sent into the drying hearth 20 through a solid waste inlet 201, the wastewater is sprayed into the drying hearth 20 through a wastewater inlet 202, and the drying hearth is also provided with a multi-media burner 203 and a blanking port 204; the multimedia burner 203 is provided with interfaces of high-calorific-value waste liquid, high-calorific-value waste gas, auxiliary fuel and combustion-supporting air; the temperature of the drying hearth 20 is controlled to be 150-300 ℃ by adjusting the flow rates of the high-heat-value waste liquid, the high-heat-value waste gas and the auxiliary fuel, and the solid waste is ensured to be completely dried in the drying hearth 20. More specifically, the solid waste is fully dried and fed into the lower hearth through the blanking port 204 for continuous treatment by the feeding mechanism in the drying hearth 20, specifically, by the stirring action of the rake teeth 4 in the feeding mechanism for stirring and stirring the solid waste.
The gas escaping from the lower hearth entering the combustion hearth 10 comprises a gas-phase pyrolysis product of the pyrolysis hearth 30, the gas-phase pyrolysis product and the high-temperature flue gas enter the drying hearth 20 along with the high-temperature flue gas, the gas-phase pyrolysis product and the high-temperature flue gas in the drying hearth 20 exchange heat with the solid waste and the wastewater to reduce the temperature, and the water in the solid waste and the wastewater is evaporated; the gaseous pyrolysis product, the high-temperature flue gas and the dry and evaporated moisture enter the top combustion furnace 10 through the porous distribution plate 104 of the combustion furnace 10. In the top combustion furnace 10, a large amount of air is fed into the combustion furnace 10 through the secondary air inlet 101, and the temperature required by the combustion reaction in the combustion furnace 10 can be ensured through the combustion of high-calorific-value waste gas, high-calorific-value waste liquid and auxiliary fuel in the multi-medium combustor 103, so that the complete combustion of the gas-phase products of pyrolysis can be ensured.
The dried solid waste falls into the pyrolysis furnace 30 through the upper layer drying furnace blanking port 204, and the pyrolysis furnace 30 is provided with a secondary air inlet 301, a multi-medium burner 302 and a blanking port 304; the multi-medium burner 302 is provided with interfaces of nitrogen-containing waste gas and waste liquid, auxiliary fuel and combustion air; the temperature of a pyrolysis hearth is ensured to be 900-1300 ℃ through the combustion of nitrogen-containing waste gas, nitrogen-containing waste liquid and auxiliary fuel; through the air volume of adjusting secondary air entry 301 entering, guarantee that the air-fuel ratio in the pyrolysis furnace keeps between 0.6 ~ 0.9, make nitrogenous waste gas and nitrogenous waste liquid carry out burning and pyrolytic reaction under the environment of high temperature oxygen deficiency, provide the reaction heat simultaneously, make the solid waste after the drying heated to the required temperature of reaction, and abundant pyrolysis, under the atmosphere of reducibility, raw materials nitrogen in waste gas and the waste liquid is turned into N2The NOx of the exhaust gas itself is also reduced to N in a reducing atmosphere2. When the raw material contains NH3In this case, the pyrolysis temperature should be controlled substantially at 1300 ℃ to ensure NH with higher activation energy3Complete reaction without excessive temperature leading to subsequent excessive temperature in the residue burner 40 and increased thermodynamic NOx production. The specific temperature control is adjusted according to the composition of liquid-solid three wastes of the treated gas, thereby inhibiting the conversion of ammonia nitrogen in the raw material into NOx and converting the NOx contained in the waste gas into N2. Moreover, the solid waste is stirred by the rabble teeth 4 in the pyrolysis furnace chamber 30, so that the solid pyrolysis product is fully contacted with the secondary air for supporting combustion, and the solid waste after pyrolysis is discharged downwards towards the blanking port 304 by the stirring of the rabble teeth 4.
The pyrolyzed solid waste falls into the residue combustion furnace 40 from the blanking port 304 of the upper pyrolysis furnace 30, and the residue combustion furnace 40 is provided with a secondary air inlet 401, a multi-medium burner 402 and a blanking port 403; the multimedia burner 402 is provided with interfaces for high calorific value waste liquid, high calorific value waste gas, auxiliary fuel and combustion air; the high-heat-value waste liquid and gas are fully combusted in the residue combustion hearth 40 by adjusting the flow of the high-heat-value waste liquid and gas and the flow of the auxiliary fuel; the temperature of the residue combustion furnace hearth is ensured to be 850-1100 ℃, and the oxygen content of the residue combustion furnace hearth 40 is ensured to be 3-6% by adjusting the air amount entering from the secondary air inlet 401, so that the waste liquid, the waste gas and the pyrolysis residue (solid pyrolysis product) are completely combusted in the residue combustion furnace hearth. And moreover, the solid pyrolysis product is fully contacted with secondary air through the stirring effect of the rake teeth 4 in the residue combustion hearth on the solid pyrolysis product, so that the pyrolysis residue is fully and completely combusted.
The ash residue left after the combustion of the residue combustion furnace 40 falls into the cooling furnace 50 from the material dropping port 403 of the upper residue combustion furnace 40, and the residue combustion furnace is also provided with a primary air inlet 501, a low-calorific-value waste gas inlet 502 and a slag discharging port 503; the ash carries out direct contact type heat exchange with primary air and low-heat-value waste gas in the cooling hearth 50, the ash is discharged through a slag discharge opening 503 after the temperature of the ash is reduced, and the primary air and the low-heat-value waste gas are preheated. This approach facilitates ash heat recovery, reducing the operating costs of waste gas, waste liquid and solid waste disposal. And the slag is fully contacted with low-heat value waste gas and primary air through the stirring and stirring action of the rake teeth 4 in the cooling hearth 50 on the slag, and then the slag is discharged from a slag discharge port. Ash and slag carry out direct contact type heat exchange with primary air and low-heat value waste gas in the cooling hearth, the preheated primary air and the low-heat value waste gas flow upwards, and the preheated primary air and the preheated low-heat value waste gas pass through the residue combustion hearth 40, the pyrolysis hearth 30, the drying hearth 20 and the combustion hearth 10 for one time, and participate in combustion reaction in the residue combustion hearth 40, the pyrolysis hearth 30 and the combustion hearth 10; the ash slag is discharged through a slag discharge port after the temperature of the ash slag is reduced. The oxygen content and the temperature parameter of each hearth can meet the requirements by controlling the amount of primary air and low-heat-value waste gas and the secondary air of each hearth and the power of the multi-medium burner.
In the above embodiment, the drying, pyrolysis and combustion processes are combined to form a multi-hearthFrom top to bottom, there are a combustion chamber 10, a drying chamber 20, a pyrolysis chamber 30, a residue combustion chamber 40, and a cooling chamber 50. The pyrolysis furnace 30 provides sufficient oxygen for the combustion process through the combustion of the auxiliary fuel in the multi-media combustor 302, so as to provide the high temperature required by the pyrolysis of the raw materials, and the specific temperature control is adjusted according to the composition of the three wastes (liquid, solid and three wastes) of the treated gas, so as to realize the sufficient pyrolysis of different phase substances. Because the inside of the pyrolysis furnace chamber 30 is also provided with dry solid waste falling from the upper dry furnace chamber 20 and nitrogen-containing waste liquid and nitrogen-containing waste gas sent in by the multi-medium burner 302, the whole pyrolysis furnace chamber is in an oxygen-deficient state, and under the oxygen-deficient state, the solid waste, the waste liquid and the waste gas can be pyrolyzed to generate a large amount of CO and H2Reducing gases such as hydrocarbon, amino and nitro in the nitrogen-containing waste liquid, the nitrogen-containing waste gas and the solid waste and NOx and NH in the nitrogen-containing waste gas in the pyrolysis furnace chamber3Etc. react with CO and H2The reducing gases or the reducing gases are subjected to oxidation-reduction reaction with each other, and finally N is generated2And H2And O. The solid residue after the pyrolysis section treatment enters the residue combustion furnace 40 downwards, the gaseous pyrolysis product enters the top combustion furnace 10 upwards through the drying furnace 20, and the solid waste is dried by utilizing the pyrolysis smoke heat. Through adopting many furnace structures, can be step by step carry out drying, pyrolysis, combustion processing to the raw materials, through integrating the advantage of drying, pyrolysis, burning, combine technological parameter control, can guarantee that the raw materials nitrogen NOx conversion in waste gas waste liquid and the solid waste is less than 5%, NOx in the raw materials waste gas reduces 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 addition, can be according to the height, pyrolysis characteristic and the burning characteristic of handling material moisture content, select different setting numbers of piles respectively to dry furnace, pyrolysis furnace and residue burning furnace, fully guarantee the material and deal with the effect. Specifically, the drying furnace with different layers can be designed according to the moisture content of the material and the characteristics of the material, and the heat supply load of the multi-medium burner of the drying furnace is controlled, so that the solid waste of any moisture content can be completely dried in the drying furnace, and the complete combustion of the solid waste is further ensured. The pyrolysis furnace with different layers can be designed according to the characteristics and ammonia nitrogen content of materials, and the heat supply amount of the multi-medium burner of the pyrolysis furnace is controlled, so that the complete reaction of waste gas, waste liquid and solid waste in the pyrolysis furnace can be ensured. The residue combustion furnace chambers with different layers can be designed according to the combustion characteristics of the material pyrolysis residues, and the thermal ignition reduction rate of ash and slag discharged from the bottom layer can be controlled below 1-3% by controlling the heat supply amount and the secondary air amount of a multi-medium burner of the residue combustion furnace chamber.
Several specific examples are provided below:
example 1 comprehensive disposal project for gas, liquid and solid three wastes of certain chemical plant
Raw materials: the combustion raw material comprises 1 kind of solid waste, 3 kinds of waste liquid and 2 kinds of waste gas, and the total nitrogen content of the raw material is about 0.73 wt% (calculated by N, excluding N)2Content(s).
Solid waste 1: chemical sludge (water content 85%)
Solid waste 2: oil-containing sludge (water content 85%, oil content less than or equal to 2%)
Waste liquid 1: acrylonitrile waste liquid (containing 5.4 wt% of C)3H5N, the remainder being water)
Waste liquid 2: fusel waste liquid (containing 37 wt% of CH)4O、15.4％wt C2H6O、5.3％wt C3H8O、 5.3％wt C4H10O、2.7％wt C5H12O、2.3％wt C6H14O, the remainder being water)
Waste liquid 3: ethanol column wastewater (containing 10.88 wt% of C)2H6O2、4.87％wt C5H12O、0.34％wt C2H6O、0.26％wt C3H8O、1.13％wt C4H10O、0.7％wt C3H8O2The balance 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)
Exhaust gas 2: recovery column vent gas (30 mg/Nm in)3 CH4、100mg/Nm3 COS、50mg/Nm3 CO、14.32％wt H2S、27.78％wt H2O、22.5％wt NH3、35.4％wt CO2The rest is inert gas, oxygen and water
Exhaust gas 3: air for transportation (30 mg/Nm content)3 CH4O, the remainder being air)
A combustion processing device: by adopting the device, 13 layers of hearths (1 layer of combustion hearths, 3 layers of drying hearths, 3 layers of pyrolysis hearths, 4 layers of residue combustion hearths and 2 layers of cooling hearths are arranged from top to bottom in sequence) are arranged.
Feeding: after the solid waste 1 and the solid waste 2 are fed into the drying hearth 20 through the solid waste inlet 201 by the feeder, the dried solid waste falls into the pyrolysis hearth 30 (a rotary pyrolysis furnace) from the blanking part; the high-nitrogen waste liquid 1 is sent into the pyrolysis hearth 30 through a waste liquid spray gun through a multi-medium burner 302; high-nitrogen waste gases 1 and 2 are fed into the pyrolysis furnace 30 through a waste gas spray gun through a multi-medium burner 302; the waste liquid 2 and the waste liquid 3 have higher heat values and are respectively sent into a combustion hearth 10, a drying hearth 20, a pyrolysis hearth 30 and a residue combustion hearth 40 through a multi-medium burner 103/203/302/402 through a waste liquid spray gun to be used as fuels; the waste gas 3 has a low calorific value and is fed into the cooling furnace through a low calorific value waste gas inlet 502. In addition, the multi-medium burner of each hearth is provided with an auxiliary fuel interface and a combustion-supporting air interface for adjusting the combustion temperature and the oxygen content of each hearth.
The combustion treatment process comprises the following steps: the temperature of a combustion hearth 10 is controlled to 1150 ℃, and the air-fuel ratio is 1.15; controlling the temperature of a drying hearth 20 to be 300 +/-10 ℃; the temperature of the pyrolysis furnace chamber 30 is controlled to be 1250-1280 ℃, and the air-fuel ratio is 0.85; the temperature of the residue-burning furnace 40 is controlled at 850 ℃, and the air-fuel ratio is 1.4 (namely, 6 percent of oxygen content).
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 200mg/Nm3The concentration of outlet oxygen is about 3.0 percent, VOCs can not be detected, and the NOx conversion rate of the whole raw material nitrogen is about1.35% and the ash scorching rate is about 2.5%.
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: by adopting the device, 13 layers of hearths (1 layer of combustion hearths, 3 layers of drying hearths, 4 layers of pyrolysis hearths, 3 layers of residue combustion hearths and 2 layers of cooling hearths are arranged from top to bottom in sequence) are arranged.
Feeding: same as in example 1.
The combustion treatment process comprises the following steps: the temperature of the combustion hearth 10 is controlled at 1150 ℃, and the air-fuel ratio is 1.1 (namely 2 percent of oxygen content); controlling the temperature of a drying hearth 220 to be 300 +/-10 ℃; the temperature of the pyrolysis hearth 30 is controlled to be 1200-1250 ℃, and the air-fuel ratio is 0.80; the temperature of the residue burning hearth 40 is controlled to be 950 ℃, and the air-fuel ratio is 1.4.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 175mg/Nm3The outlet oxygen concentration is about 2.1 percent, VOCs cannot be detected, the NOx conversion rate of the whole raw material nitrogen is about 1.2 percent, and the ash scorching and reducing rate is about 1.5 percent.
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: by adopting the device, 13 layers of hearths (1 layer of combustion hearths, 3 layers of drying hearths, 4 layers of pyrolysis hearths, 4 layers of residue combustion hearths and 1 layer of cooling hearths are arranged from top to bottom in sequence) are arranged.
Feeding: same as in example 1.
The combustion treatment process comprises the following steps: the temperature of a combustion furnace hearth is controlled to be 1125 ℃, and the air-fuel ratio is 1.15; controlling the temperature of a drying hearth to be 300 +/-10 ℃; the temperature of a pyrolysis furnace hearth is controlled to be 1250-1280 ℃, and the air-fuel ratio is 0.8; the temperature of the residue combustion furnace was controlled at 850 deg.C and the air-fuel ratio was 1.3 (i.e., 4.8% oxygen content).
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 180mg/Nm3The outlet oxygen concentration is about 3.1 percent, VOCs cannot be detected, the NOx conversion rate of the whole raw material nitrogen is about 1.21 percent, and the ash thermal ignition loss rate is about 2.4 percent.
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 3.
Feeding: same as in example 1.
The combustion treatment process comprises the following steps: the temperature of a combustion hearth is controlled to 1150 ℃, and the air-fuel ratio is 1.25; controlling the temperature of a drying hearth to be 300 +/-10 ℃; controlling the temperature of a pyrolysis furnace hearth to be 1200-1270 ℃, and controlling the air-fuel ratio to be 0.75; the temperature of the residue burning hearth is controlled at 850 ℃, and the air-fuel ratio is 1.35.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 230mg/Nm3The outlet oxygen concentration is about 4.2 percent, VOCs cannot be detected, the NOx conversion rate of the whole raw material nitrogen is about 1.55 percent, and the ash thermal ignition loss rate is about 2.2 percent.
Example 5: comprehensive disposal project for gas, liquid and solid three wastes of certain chemical plant
Raw materials: comprises 2 kinds of solid waste, 6 kinds of waste liquid and 3 kinds of waste gas, and the total nitrogen content of the raw materials is 3.24 percent wt (calculated by N, N is not included)2Content(s).
Solid waste 1: waste activated carbon;
solid waste 2: spent catalyst (80% water, 10% catalyst, 10% organics);
waste liquid 1: washing tower waste water (containing Na)2SO4About 8% of salt such as NaCl, and the balance of water);
waste liquid 2: saturated waste brine (containing 20-30% of Na)2SO415% -20% of glycine and the balance of water);
waste liquid 3: 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);
waste liquid 4: ethylene glycol lights (20.74% wt methyl glycolate, 30.99% wt butanediol, 27.57% wt ethylene glycol, 0.01% wt diethylene glycol, the remainder being water);
waste liquid 5: 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 6: fusel oil (containing 8% wt of methyl formate, 72% wt of methanol and 20% wt of ethanol);
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 of methylal, 0.83% wt of methanol, 12.42% wt of CO, the remainder being inert gas N2And CO2)；
Exhaust gas 2: shift stripper acid gas component (containing 22.5 wt% ammonia gas and 14.32 wt% H)2S、0.01％wt H20.05% wt CO, the remainder being CO2And water vapor);
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 dimethyl ether, 7.52% wt methylal, the remainder being N2、CO2And water vapor).
A combustion processing device: by adopting the device, 15 layers of hearths (1 layer of combustion hearths, 3 layers of drying hearths, 4 layers of pyrolysis hearths, 5 layers of residue combustion hearths and 2 layers of cooling hearths are arranged from top to bottom in sequence) are arranged.
Feeding: after the solid waste 1 and the solid waste 2 are fed into the drying hearth 20 through the solid waste inlet 201 by the feeder, the dried solid waste falls into the pyrolysis hearth 30 (a rotary pyrolysis furnace) from the blanking part; the high-nitrogen waste liquid 2 is sent into the pyrolysis hearth 30 through a waste liquid spray gun through a multi-medium burner 302; high-nitrogen waste gas 1, 2 and 3 is fed into the pyrolysis hearth 30 through a waste gas spray gun through a multi-medium burner 302; the waste liquid 3 is sent into the combustion furnace 10 through a low-heat value waste liquid inlet 102; the waste liquid 1 is sent into the drying hearth 20 through a waste water inlet 202; the waste liquid 4, the waste liquid 5 and the waste liquid 6 have higher heat value and are respectively sent into the combustion hearth 10, the drying hearth 20, the pyrolysis hearth 30 and the residue combustion hearth 40 through the multi-medium burner 103/203/302/402 by a waste liquid spray gun to be used as fuels. In addition, the multi-medium burner of each hearth is provided with an auxiliary fuel interface and a combustion-supporting air interface for adjusting the combustion temperature and the oxygen content of each hearth.
The combustion treatment process comprises the following steps: the temperature of a combustion hearth is controlled to 1150 ℃, and the air-fuel ratio is 1.10; controlling the temperature of a drying hearth to be 300 +/-10 ℃; the temperature of a pyrolysis furnace hearth is controlled to be 1250-1280 ℃, and the air-fuel ratio is 0.85; the temperature of the residue combustion furnace is controlled at 850 ℃, and the air-fuel ratio is 1.4 (namely 6 percent of oxygen content).
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 200mg/Nm3The outlet oxygen concentration is about 2.1 percent, VOCs cannot be detected, the NOx conversion rate of the whole raw material nitrogen is about 0.62 percent, and the ash thermal ignition loss rate is about 1.3 percent.
Example 6: comprehensive disposal project for gas, liquid and solid three wastes of certain chemical plant
Raw materials: same as in example 5.
A combustion processing device: by adopting the device, 15 layers of hearths (1 layer of combustion hearths, 3 layers of drying hearths, 5 layers of pyrolysis hearths, 5 layers of residue combustion hearths and 1 layer of cooling hearths are arranged from top to bottom in sequence) are arranged.
Feeding: same as in example 5.
The combustion treatment process comprises the following steps: the temperature of a combustion hearth is controlled to 1150 ℃, and the air-fuel ratio is 1.15; controlling the temperature of a drying hearth to be 300 +/-10 ℃; the temperature of a pyrolysis furnace hearth is controlled to be 1250-1280 ℃, and the air-fuel ratio is 0.65; the temperature of the residue combustion hearth is controlled to be 850 ℃, and the air-fuel ratio is 1.4.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 120mg/Nm3The outlet oxygen concentration is about 2.1 percent, VOCs cannot be detected, the NOx conversion rate of the whole raw material nitrogen is about 0.37 percent, and the ash thermal ignition loss rate is about 1.5 percent.
Example 7: comprehensive disposal project for gas, liquid and solid three wastes of certain chemical plant
Raw materials: same as in example 5.
A combustion processing device: by adopting the device, 13 layers of hearths (1 layer of combustion hearths, 2 layers of drying hearths, 5 layers of pyrolysis hearths, 4 layers of residue combustion hearths and 1 layer of cooling hearths are arranged from top to bottom in sequence) are arranged.
Feeding: same as in example 5.
The combustion treatment process comprises the following steps: the temperature of a combustion hearth is controlled to 1150 ℃, and the air-fuel ratio is 1.15; controlling the temperature of a drying hearth to be 350 +/-10 ℃; the temperature of a pyrolysis furnace hearth is controlled to be 1250-1280 ℃, and the air-fuel ratio is 0.7; the temperature of the residue combustion hearth is controlled to be 850 ℃, and the air-fuel ratio is 1.4.
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 2.1 percent, VOCs cannot be detected, the NOx conversion rate of the whole raw material nitrogen is about 0.62 percent, and the ash thermal ignition loss rate is about 1.65 percent.
Example 8: comprehensive disposal project for gas, liquid and solid three wastes of certain chemical plant
Raw materials: same as in example 5.
A combustion processing device: same as in example 7.
Feeding: same as in example 5.
The combustion treatment process comprises the following steps: the temperature of a combustion hearth is controlled to 1150 ℃, and the air-fuel ratio is 1.2; controlling the temperature of a drying hearth to be 350 +/-10 ℃; the temperature of a pyrolysis furnace hearth is controlled to be 1250-1280 ℃, and the air-fuel ratio is 0.85; the temperature of the residue combustion hearth is controlled at 900 ℃, and the air-fuel ratio is 1.4.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 220mg/Nm3The outlet oxygen concentration is about 3.5%, VOCs cannot be detected, the NOx conversion rate of the whole raw material nitrogen is about 0.68%, and the ash scorching rate is about 1.25%.
Comparative example 1: incineration project for high-nitrogen-content waste gas and waste liquid of certain factory
Raw materials: the combustion feed contained 4 streams of waste liquor, 2 streams of waste gas, and a total nitrogen content of the feed of 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 apparatus exhaust 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% v C1+ C2+ C3, balance inert gas, oxygen, water).
A combustion processing device: comprises a two-section type combustion furnace with a vertical pyrolysis furnace chamber and a horizontal oxidation furnace chamber.
Feeding: waste gas 1, 2 send into the pyrolysis furnace through the waste gas spray gun in, waste liquid 1, 2, 3, 4 directly let in the pyrolysis furnace through the waste liquid spray gun in, burner's temperature is through afterburning fuel combustion control.
The combustion treatment process comprises the following steps: the temperature of the pyrolysis furnace is controlled to 1350, and the air-fuel ratio is 0.85; the temperature of the oxidation furnace hearth is controlled at 1100 ℃, and the air-fuel ratio is 1.5.
The treatment effect is as follows: concentration of NOx in flue gas at an outlet of the incinerator: 500mg/Nm3And the concentration of outlet oxygen is about 7.0%, VOCs cannot be detected, and the NOx conversion rate of the whole raw material nitrogen is about 2.2%.
Comparative example 2: incineration project for high-nitrogen-content waste gas and waste liquid of certain factory
Raw materials: same as in example 9.
A combustion processing device: a two-stage furnace comprising a precombustion chamber and a burnout chamber.
Feeding: the waste gas 1, 2 and the waste liquid 1, 2, 3, 4 are respectively sent into the precombustion chamber through a waste gas spray gun and a waste liquid spray gun which are arranged on the multimedia burner, and the temperature of the combustion device is controlled by burning the afterburning fuel.
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: 9500mg/Nm3With an outlet oxygen concentration of about 6.0%, the non-methane total hydrocarbon operation may occasionally exceed 20mg/Nm3The overall feed nitrogen NOx conversion was about 40.4%.
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. A multi-chamber multiphase low-nitrogen combustion treatment device is characterized by comprising:
the shell is internally divided into a plurality of hearths; the multiple hearths comprise a combustion hearth, a drying hearth, a pyrolysis hearth, a residue combustion hearth and a cooling hearth which are respectively arranged from top to bottom, and the multiple hearths are sequentially communicated;
the center of the shell is provided with a feeding mechanism which is used for mixing materials of at least one hearth except the combustion hearth and feeding the materials to the lower hearth in a penetrating mode.
2. The multi-bore multi-phase low-nitrogen combustion processing device according to claim 1, wherein:
the combustion furnace hearth and the drying furnace hearth are separated by a porous distribution plate, and the surface of the porous distribution plate is uniformly distributed with spaced holes.
3. The multi-bore multi-phase low-nitrogen combustion processing device according to claim 2, wherein:
the multi-layer support piece is arranged on the lower side of the porous distribution plate in the shell, a hearth is formed between every two adjacent support pieces, and the blanking portion is formed in the center of the shell or on the inner side wall of the shell by any layer of support piece.
4. The multi-bore multiphase low nitrogen combustion processing device according to claim 3, wherein:
the multilayer supporting piece alternately forms blanking parts at the center of the shell and on the inner side wall of the shell.
5. The multi-bore multiphase low nitrogen combustion processing device according to claim 3, wherein:
the feeding mechanism comprises a rotating shaft penetrating through the center of the shell and a rake arm arranged on the rotating shaft; rake teeth are arranged on the rake arm at intervals, and the rotating shaft is in driving connection with a power source;
the rake teeth are arranged above the supporting piece, so that the rake teeth can push blanking on the supporting piece.
6. The multi-bore multi-phase low-nitrogen combustion processing device according to claim 5, wherein:
the rotating shaft is a double-layer hollow rotating shaft comprising an inner layer shaft and an outer layer shaft, a cooling air inlet and a cooling air outlet are arranged on the double-layer hollow rotating shaft, the cooling air inlet is connected with the inner layer shaft, and the cooling air outlet is connected with the outer layer shaft;
the double-layer hollow rake arm comprises an inner layer rake arm and an outer layer rake arm, the inner layer rake arm of the double-layer hollow rake arm is communicated with an inner layer shaft of the double-layer hollow rotating shaft, and the outer layer rake arm of the double-layer hollow rake arm is communicated with an outer layer shaft of the double-layer hollow rotating shaft;
wherein, spouts are distributed on the inner layer harrow arm of the double-layer hollow harrow arm.
7. The multi-bore multiphase low nitrogen combustion processing device according to claim 5 or 6, characterized in that:
the rake teeth are arranged on the rake arm in an adjustable inclination angle, and the inclination angles of the rake arm and the rake teeth are controlled, so that the material pushing direction of the rake teeth in the hearth is consistent with the direction of the rake teeth entering the lower hearth.
8. The multi-bore multi-phase low-nitrogen combustion processing device according to claim 7, wherein:
when the support piece forms a blanking part at the center of the shell, the blanking part is positioned between the rotating shaft and the support piece and is a circular hole at the center of the shell; for the rake teeth on the layer of supporting piece, the number of the rake teeth pushing towards the center of the hearth is more than that of the rake teeth pushing towards the periphery of the hearth;
when the support piece forms a blanking part on the inner side wall of the shell, the blanking part is positioned between the inner wall of the shell and the support piece, and a plurality of square holes are uniformly distributed on the outer peripheral surface of the hearth by the blanking part; for the rake teeth on the layer of supporting piece, the number of the rake teeth pushing towards the periphery of the hearth is more than that of the rake teeth pushing towards the center of the hearth.
9. The multi-bore multi-phase low-nitrogen combustion processing device according to claim 1, wherein:
a low-heat-value waste liquid inlet, a combustion-supporting air inlet and a flue gas outlet are formed in the combustion hearth;
a solid waste inlet and a waste water inlet are arranged on the drying hearth;
combustion-supporting air inlets are formed in the pyrolysis hearth and the residue combustion hearth;
a combustion-supporting air inlet, a low-calorific-value waste gas inlet and a slag discharge port are formed in the cooling hearth;
wherein, the combustion hearth, the drying hearth, the pyrolysis hearth and the residue combustion hearth are respectively connected with a multi-medium burner, and the multi-medium burners corresponding to the pyrolysis hearth are respectively provided with combustion-supporting air, nitrogen-containing waste gas, nitrogen-containing waste liquid and auxiliary fuel inlets; the multi-medium burner corresponding to the combustion hearth, the drying hearth and the residue combustion hearth is respectively provided with a combustion-supporting air inlet, a high-heat-value waste gas inlet, a high-heat-value waste liquid inlet and an auxiliary fuel inlet.
10. The multi-bore multi-phase low-nitrogen combustion processing device according to claim 1, wherein:
controlling the temperature of a combustion hearth to be 850-1150 ℃; and controlling the oxygen content in the combustion hearth to be between 1 and 6 percent; and/or;
controlling the temperature of the pyrolysis furnace hearth to be 900-1300 ℃, and controlling the air-fuel ratio in the pyrolysis furnace hearth to be 0.6-0.9; and/or;
controlling the temperature of a residue combustion hearth to be 850-1100 ℃; controlling the oxygen content of the residue combustion furnace to be between 3 and 6 percent.
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| CN202122598517.3U CN216448160U (en) | 2021-10-27 | 2021-10-27 | Multi-chamber type multiphase low-nitrogen combustion treatment device |
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