A multi-chamber multi-phase low nitrogen combustion treatment device and process

Abstract

The present invention discloses a multi-chamber multiphase low-nitrogen combustion treatment device, comprising: a shell, wherein a plurality of furnaces are formed by dividing the shell; the plurality of furnaces include a combustion furnace, a drying furnace, a pyrolysis furnace, a residue combustion furnace, and a cooling furnace, which are arranged from top to bottom, and the plurality of furnaces are connected in sequence; wherein a feeding mechanism for mixing at least one furnace other than the combustion furnace and feeding the materials to the lower furnace is provided through the center of the shell. The present invention enables solid waste to be directly sent into the furnace for disposal without drying, and can also simultaneously coordinately treat waste gas, waste liquid, and waste water, realize gas-liquid-solid integrated multiphase low-nitrogen combustion, and can especially carry out integrated multiphase low-nitrogen combustion treatment for three wastes with high water content and high raw nitrogen, and can reduce the NOx conversion rate of raw nitrogen to below 5%, and control the oxygen content of flue gas at the furnace outlet to within 1-6%, reduce the flue gas volume and flue gas purification cost, and achieve better social and economic benefits.

Description

Technical Field

[0001] The invention belongs to the technical field of environmental protection, and relates to a multi-chamber multi-phase low-nitrogen combustion treatment device and process. Background Art

[0002] Some large petrochemical enterprises or industrial parks need to treat solid waste, organic waste liquid and organic waste gas at the same time. Some of the solid wastes have very high moisture content and low calorific value, such as sludge, oil sludge, filter cake, etc. The composition of waste liquid and waste gas is also very complex. Some have high nitrogen content, some basically do not contain nitrogen, some have high combustible components and high calorific value, and some have few combustible components and low calorific value. At present, the conventional treatment method is to dry the solid waste with high moisture content and then send it to the rotary kiln for incineration, send the waste liquid or high calorific value waste gas to the solid waste treatment secondary combustion chamber for incineration or build a new waste gas and waste liquid incinerator for incineration, and the low calorific value waste gas is treated by catalytic oxidation or thermal storage oxidation. This leads to a park or a petrochemical enterprise to build several different types of incineration treatment devices for different three wastes, resulting in increased investment, operation and management costs.

[0003] The solid waste, waste liquid and waste gas of petrochemical enterprises often contain very high ammonia nitrogen content. The proportion of ammonia nitrogen in the fuel of the current hazardous waste incineration system converted into NOx is generally between 20% and 50%. For many organic wastes with high ammonia nitrogen content, the conversion rate of 20% to 50% is still too high, and the subsequent flue gas denitrification investment is large, the agent consumption is large, and the operating cost is high.

[0004] Chinese patent document CN2020220148411 discloses a combustion treatment device and process for nitrogen-containing raw materials, which uses a combination of a fixed / rotary pyrolysis furnace and a second combustion chamber to carry out multiphase combustion of nitrogen-containing raw materials. The fixed pyrolysis furnace can only process powdered solid waste, and the rotary pyrolysis furnace generally processes solid waste with a moisture content of ≤60%. When the material is a high-water material (more than 80% water), since the rotary pyrolysis furnace can only be equipped with burners at both ends, the temperature field of the pyrolysis furnace will be uneven, which is easy to cause slagging. It is usually necessary to pre-dry the solid waste to a certain degree before it can be sent to the rotary pyrolysis furnace for treatment.

[0005] Chinese patent document CN202010395972.0 discloses a system for treating solid waste using a multi-chamber furnace, in which a variety of solid wastes are dried separately and then sent into the multi-chamber furnace system, and a traditional multi-chamber furnace is used for treatment. No low-nitrogen treatment process is performed in the furnace, and the waste treated is only solid waste. Therefore, it cannot solve the current gas-liquid-solid integrated multi-phase low-nitrogen combustion. Summary of the invention

[0006] In view of the problems in the above-mentioned prior art, the purpose of the present invention is to provide a multi-chamber multi-phase low-nitrogen combustion treatment device and process, which is optimized and designed on the basis of the traditional multi-chamber furnace, so that solid waste can be directly sent to the furnace for disposal without drying, and can also simultaneously treat waste gas, waste liquid, and waste water, so as to realize gas-liquid-solid integrated multi-phase low-nitrogen combustion. The device and process are especially capable of integrated multi-phase low-nitrogen combustion treatment for three wastes with high water content and high raw nitrogen, which can reduce the NOx conversion rate of raw nitrogen to less than 5%, and control the oxygen content of flue gas at the furnace outlet to within 1% to 6%, reducing the flue gas volume and flue gas purification costs, and achieving better social and economic benefits.

[0007] One of the purposes of the present invention is to provide a multi-chamber multi-phase low nitrogen combustion treatment device, and the technical scheme adopted is as follows:

[0008] A multi-chamber multi-phase low-nitrogen combustion treatment device, comprising:

[0009] A shell, wherein a plurality of furnaces are formed by dividing the shell; the plurality of furnaces include a combustion furnace, a drying furnace, a pyrolysis furnace, a residue combustion furnace, and a cooling furnace, which are arranged from top to bottom, and the plurality of furnaces are connected in sequence;

[0010] Wherein, a feeding mechanism for mixing materials in at least one furnace other than the combustion furnace and feeding the materials to the lower furnace is provided through the center of the shell.

[0011] Preferably, the combustion furnace and the drying furnace are separated by a porous distribution plate, and the surface of the porous distribution plate is evenly distributed with spaced holes.

[0012] Furthermore, a plurality of layers of support members are arranged on the lower side of the porous distribution plate in the shell, and a furnace is formed between two adjacent support members; and any layer of support members forms a blanking portion at the center of the shell or at the inner side wall of the shell.

[0013] Furthermore, the multi-layer support members alternately form blanking portions at the center of the shell and the inner side wall of the shell.

[0014] Furthermore, refractory materials are laid on the support members.

[0015] Furthermore, when the blanking portion is located between the rotating shaft and the support member, the blanking portion is set as a circular hole in the center of the shell; when the blanking portion is located between the inner wall of the shell and the support member, the blanking portion has multiple square holes evenly distributed on the outer peripheral surface of the furnace.

[0016] Furthermore, the feeding mechanism comprises a rotating shaft penetrating through the center of the housing, and a rake arm arranged on the rotating shaft; rake teeth are arranged at intervals on the rake arm, and the rotating shaft is drivingly connected to a power source;

[0017] The rake teeth are arranged above the support member, so that the rake teeth can push the material falling from the support member.

[0018] Furthermore, the rotating shaft is configured as a double-layer hollow rotating shaft including an inner layer shaft and an outer layer shaft, and the double-layer hollow rotating shaft is provided with a cooling air inlet and a cooling air outlet, wherein the cooling air inlet is connected to the inner layer shaft, and the cooling air outlet is connected to the outer layer shaft;

[0019] The rake arm is configured as a double-layer hollow rake arm including an inner rake arm and an outer rake arm, the inner rake arm of the double-layer hollow rake arm is connected to the inner shaft of the double-layer hollow rotating shaft, and the outer rake arm of the double-layer hollow rake arm is connected to the outer shaft of the double-layer hollow rotating shaft;

[0020] Wherein, nozzles are distributed on the inner rake arm of the double-layer hollow rake arm.

[0021] Furthermore, the rake teeth are installed on the rake arm with an adjustable inclination angle. By controlling the inclination angle of the rake arm and the rake teeth, the pushing direction of the rake teeth in the furnace is consistent with the direction of entering the lower furnace.

[0022] Further, when the support member forms a blanking portion at the center of the shell, the blanking portion is located between the rotating shaft and the support member, and the blanking portion is set as a circular hole at the center of the shell; for the rake teeth on the layer of support members, the number of rake teeth pushed toward the center of the furnace is greater than the number of rake teeth pushed toward the periphery of the furnace;

[0023] When the support member forms a blanking portion at the inner wall of the shell, the blanking portion is located between the inner wall of the shell and the support member, and the blanking portion has multiple square holes evenly distributed on the outer peripheral surface of the furnace; for the rake teeth on this layer of the support member, the number of rake teeth pushed toward the periphery of the furnace is greater than the number of rake teeth pushed toward the center of the furnace.

[0024] Preferably, the combustion furnace is provided with a low calorific value waste liquid inlet, a combustion air inlet, and a smoke outlet;

[0025] The drying furnace is provided with a solid waste inlet and a wastewater inlet;

[0026] The pyrolysis furnace and the residue combustion furnace are both provided with combustion air inlets;

[0027] The cooling furnace is provided with a combustion air inlet, a low calorific value waste gas inlet and a slag discharge port;

[0028] Among them, the combustion furnace, drying furnace, pyrolysis furnace and residue combustion furnace are respectively connected to multi-media burners, and the multi-media burners corresponding to the pyrolysis furnace are respectively provided with inlets for combustion-supporting air, nitrogen-containing waste gas, nitrogen-containing waste liquid and auxiliary fuel; the multi-media burners corresponding to the combustion furnace, drying furnace and residue combustion furnace are respectively provided with inlets for combustion-supporting air, high calorific value waste gas, high calorific value waste liquid and auxiliary fuel.

[0029] The second object of the present invention is to provide a multi-chamber multi-phase low nitrogen combustion treatment process, comprising the following steps:

[0030] S1. Low calorific value waste liquid is sent to the combustion furnace of the multi-hearth furnace through the corresponding inlet for treatment; waste water is sent to the drying furnace of the multi-hearth furnace through the corresponding inlet for evaporation treatment; solid waste is sent to the drying furnace of the multi-hearth furnace through the corresponding inlet, and the dried solid waste is sent to the pyrolysis furnace through the feeding mechanism, and nitrogen-containing waste gas and / or nitrogen-containing waste liquid is sent to the pyrolysis furnace through the corresponding inlet for pyrolysis treatment;

[0031] S2. The gaseous pyrolysis products produced in the pyrolysis furnace enter the topmost combustion furnace through the upper drying furnace for combustion. The solid pyrolysis products produced in the pyrolysis furnace enter the lower slag combustion furnace through the feeding mechanism for combustion. The heat generated in the combustion process is used for pyrolysis treatment in the upper pyrolysis furnace. Thus, the pyrolysis products are completely burned and purified through the combustion furnaces and the slag combustion furnaces arranged above and below. The obtained ash is discharged after passing through the feeding mechanism and the cooling furnace for heat exchange with low calorific value exhaust gas.

[0032] Preferably, secondary air is fed into the combustion chamber, and low calorific value waste liquid is sprayed into the combustion chamber. The combustion chamber is also provided with a multi-media burner and a flue gas outlet. The high calorific value waste liquid and waste gas are burned by the multi-media burner, and the combustion chamber temperature is controlled at 850°C ~ 1150°C. By adjusting the amount of secondary air fed in, the oxygen content in the combustion chamber is controlled between 1% and 6%, so that the combustible components in the waste liquid, waste gas and the escaping gas from the lower furnace are completely burned in the combustion chamber, and the flue gas after combustion is discharged from the flue gas outlet 105 of the combustion chamber.

[0033] Preferably, solid waste is fed into the drying furnace, waste water is sprayed into the drying furnace, and the drying furnace is also provided with a multi-media burner and a feeding port; high calorific value waste liquid and waste gas are burned by the multi-media burner to completely dry the solid waste in the drying furnace; the dried solid waste is mixed and fed through a feeding mechanism and then discharged from the feeding port.

[0034] Preferably, the dried solid waste falls into the pyrolysis furnace from the drop port of the upper drying furnace, and secondary air enters the pyrolysis furnace. The pyrolysis furnace is provided with a multi-media burner and a drop port. The nitrogen-containing waste liquid and waste gas are burned in the pyrolysis furnace through the multi-media burner, and the temperature of the pyrolysis furnace is controlled at 900°C ~ 1300°C. By adjusting the amount of secondary air entering, the air-fuel ratio in the pyrolysis furnace is controlled to be maintained between 0.6 and 0.9, so that the nitrogen-containing waste gas and nitrogen-containing waste liquid undergo pyrolysis reaction in a high-temperature oxygen-deficient environment. In a reducing atmosphere, the raw nitrogen in the waste gas and waste liquid is converted into N2, and the NOx in the waste gas itself is also reduced to N2 in a reducing atmosphere; the solid pyrolysis products are mixed and fed through a feeding mechanism and then discharged from the drop port.

[0035] Preferably, the solid pyrolysis products fall into the slag combustion furnace from the drop port of the upper pyrolysis furnace, and the secondary air enters the slag combustion furnace. The slag combustion furnace is provided with a multi-media burner and a drop port. The high calorific value waste liquid and waste gas are burned in the slag combustion furnace through the multi-media burner, and the temperature of the slag combustion furnace is controlled at 850°C ~ 1100°C. By adjusting the amount of air entering through the secondary air inlet, the oxygen content of the slag combustion furnace is controlled between 3% and 6%. The waste liquid, waste gas and solid pyrolysis products are completely burned in the residue combustion furnace; the residue is mixed and fed through the feeding mechanism and then discharged from the drop port.

[0036] Preferably, the ash remaining after combustion in the slag combustion furnace falls into the cooling furnace from the upper slag combustion furnace drop port, and the primary air and low calorific value waste gas are sent into the cooling furnace, and the cooling furnace is also provided with a slag discharge port; the ash is directly contacted with the primary air and low calorific value waste gas in the cooling furnace, and the preheated primary air and low calorific value waste gas flow upward, passing through the slag combustion furnace, pyrolysis furnace, drying furnace, and combustion furnace in turn, and participating in the combustion reaction in the slag combustion furnace, pyrolysis furnace, and combustion furnace; the ash temperature is lowered and discharged through the slag discharge port. By controlling the amount of primary air and low calorific value waste gas, the secondary air of each furnace, and the power of the multi-media burner, it is ensured that the oxygen content and temperature parameters of each furnace meet the requirements.

[0037] The beneficial effects of the present invention are embodied in:

[0038] 1) In the present invention, by adopting a multi-furnace structure, including a combustion furnace, a drying furnace, a pyrolysis furnace, a residue combustion furnace, a cooling furnace and other multiple furnaces, the raw materials can be dried, pyrolyzed and burned step by step, not only can waste gas, waste liquid and waste water of various calorific values ​​and compositions be treated, but also various high-water-content solid wastes can be treated at the same time, and the raw material adaptability is very strong; the gas, liquid and solid three wastes can be treated in an integrated multi-phase combustion state, the solid waste, waste liquid and waste gas treatment process can be shortened, especially the treatment of high-water-content solid waste (water content>80%), and the equipment space and investment can be reduced, which is suitable for industrial promotion.

[0039] 2) The present invention uses a multi-furnace structure to effectively combine the advantages of drying, pyrolysis and combustion processes, and can reduce the NOx conversion rate of the raw nitrogen in the waste gas, waste liquid and solid waste to less than 5%, and the NOx reduction rate in the raw waste gas is above 95%. Therefore, the NOx concentration at the outlet of the incinerator can be greatly reduced, and the subsequent flue gas denitrification treatment equipment and operating costs can be reduced.

[0040] 3) In the present invention, through step-by-step drying, pyrolysis and combustion, the material can be completely burned under low-oxygen combustion, the oxygen content of the flue gas escaping from the top combustion furnace is controlled within 1% to 6%, and the thermal ignition reduction rate of the ash discharged from the bottom is controlled within 1% to 3%, thereby effectively reducing the amount of flue gas and ash, and achieving better social and economic benefits.

[0041] 4) The multi-chamber furnace in the present invention is composed of multiple furnaces such as a combustion furnace, a drying furnace, a pyrolysis furnace, a residue combustion furnace, and a cooling furnace. Organic matter with different characteristics can be fed into furnaces with different functions. For example, organic matter with high moisture content and low calorific value can be fed from the drying furnace. This method is conducive to the complete combustion of organic matter in the material.

[0042] 5) The present invention can select different number of layers for the drying furnace, pyrolysis furnace and residue combustion furnace according to the moisture content, pyrolysis characteristics and combustion characteristics of the processed materials, so as to fully ensure the material treatment effect.

[0043] 6) The present invention adopts a specially designed feeding mechanism. Through the hollow rotating shaft and rake arm structure design, the movement direction of the solid waste in the furnace can be adjusted by adjusting the rake tooth angle, and the solid waste can be turned upside down in the furnace by the distribution of rake teeth at different angles, thereby increasing the residence time of the solid waste in the furnace. In addition, the residence time of the solid waste can be adjusted by adjusting the rotation speed of the rotating shaft. And the cooling air is introduced into the rotating shaft and the rake arm by clever coordination to ensure the safety of the rotating shaft and the rake arm.

[0044] 7) The present invention can accurately control the temperature and oxygen content of each furnace by separately arranging a burner for each furnace and introducing combustion-supporting air through the combustion-supporting air inlet, thereby realizing various different process requirements. BRIEF DESCRIPTION OF THE DRAWINGS

[0045] Figure 1 It is a schematic structural diagram of the multi-chamber multi-phase low nitrogen combustion treatment device of the present invention.

[0046] Figure 2 for Figure 1 Enlarged structural diagram of point A in the middle.

[0047] The meanings of the symbols in the figure are as follows:

[0048] 1-shell, 2-rotating shaft, 21-outer rotating shaft, 22-inner rotating shaft, 23-shaft cooling air inlet, 24-shaft cooling air outlet, 3-rake arm, 31-outer rake arm, 32-inner rake arm, 4-rake teeth, 5-reduction motor; 10-combustion furnace, 101-secondary air inlet, 102-low calorific value waste liquid inlet, 103-multi-media burner, 104-porous distribution plate, 105-smoke outlet; 20-drying furnace, 20 1-solid waste inlet, 202-wastewater inlet, 203-multi-media burner, 204-feeding port; 30-pyrolysis furnace, 301-secondary air inlet, 302-multi-media burner, 303-feeding port; 40-slag combustion furnace, 401-secondary air inlet, 402-multi-media burner, 403-feeding port; 50-cooling furnace, 501-primary air inlet, 502-low calorific value waste gas inlet, 503-slag discharge port. DETAILED DESCRIPTION

[0049] The following will be combined with specific embodiments to clearly and completely describe the technical solutions in the present invention. The following embodiments are only used to more clearly illustrate the technical solutions of the present invention, and cannot be used to limit the protection scope of the present invention.

[0050] According to an embodiment provided by the present invention, a multi-chamber multi-phase low-nitrogen combustion treatment device is provided, comprising:

[0051] A shell 1 is provided, wherein a plurality of furnaces are formed in the shell; the plurality of furnaces include a combustion furnace 10, a drying furnace 20, a pyrolysis furnace 30, a residue combustion furnace 40, and a cooling furnace 50 which are arranged from top to bottom, and the plurality of furnaces are sequentially connected; wherein a feeding mechanism for mixing materials in at least one furnace other than the combustion furnace 10 and feeding the materials to the lower furnace is provided through the center of the shell 1.

[0052] According to the multi-chamber multi-phase low-nitrogen combustion treatment of this embodiment, there are multiple furnaces such as a combustion furnace, a drying furnace, a pyrolysis furnace, a residue combustion furnace, and a cooling furnace, and each furnace is a refractory furnace, which can dry, pyrolyze, and burn the raw materials step by step, shorten the solid waste, waste liquid, and waste gas disposal process, especially the treatment of high-water solid waste (water content>80%), and reduce equipment space and investment. In addition, the setting of the feeding mechanism can promote the effective treatment of related processes in multiple furnaces, and improve the reliability of the device process and the treatment effect.

[0053] As a preferred embodiment, the combustion furnace 10 and the drying furnace 20 are separated by a porous distribution plate 104, and the surface of the porous distribution plate 104 is evenly distributed with spaced holes, and the hole diameter is preferably 50-150 mm, so that the flue gas in the lower furnace enters the combustion furnace 10 through the small holes. In practical applications, the porous distribution plate 104 is formed by a supporting structure and a refractory castable, and the spaced holes evenly distributed on the refractory porous distribution plate 104 separating the combustion furnace 10 from the drying furnace 20 allow the lower flue gas to enter the combustion furnace 10 through the spaced holes. The supporting structure is generally carbon steel, and a refractory material is covered on it.

[0054] The housing 1 is provided with multiple layers of support members 100 at the lower side of the porous distribution plate 104, and each furnace is formed between two adjacent support members 100. Figure 1 , a drying furnace 20, a pyrolysis furnace 30, a residue combustion furnace 40, and a cooling furnace 50 are formed in sequence in the shell through a plurality of support members 100 from top to bottom. Specifically, the drying furnace 20 is formed between the porous distribution plate 104 and the first layer of support members 100, the pyrolysis furnace 30 is formed between the first and second layer of support members 100, the residue combustion furnace 40 is formed between the second and third layer of support members 100, and the cooling furnace 50 is formed between the third and fourth layer of support members 100. It should be noted that different number of layers can be selected for the drying furnace, pyrolysis furnace, and residue combustion furnace according to the moisture content, pyrolysis characteristics, and combustion characteristics of the processed material, so as to fully ensure the material treatment effect.

[0055] Furthermore, any layer of support member 100 forms a blanking portion at the center of the shell 1 or at the inner wall of the shell 1. In order to improve the processing effect, the two ends of the multi-layer support member 100 alternately form blanking portions at the center of the shell 1 and at the inner wall of the shell 1 to extend the blanking processing path. Figure 1 As shown, each layer of support members 100 (refractory material) separating the drying furnace 20, pyrolysis furnace 30, residue combustion furnace 40, and cooling furnace 50 is provided with a blanking opening, and the blanking openings are alternately arranged in the center of the furnace or the outside of the furnace. When the blanking opening of the upper furnace is in the center of the furnace, the blanking opening of the furnace is on the outside of the furnace. Thus, the mass transfer process of the material in the furnace is increased to ensure the full progress of each process. More specifically, when the blanking portion is located between the rotating shaft 2 and the support member 100, the blanking portion is set as a circular hole in the center of the shell 1; when the blanking portion is located between the inner wall of the shell 1 and the support member 2, the blanking portion is evenly distributed with a plurality of, for example, 6-18 square holes on the outer peripheral surface of the furnace, which is conducive to the orderly processing of the material step by step.

[0056] Based on the above, in order to further improve the processing effect of the present invention, the feeding mechanism for achieving the mixing and conveying functions of the drying furnace 20, the pyrolysis furnace 30, the residue combustion furnace 40, and the cooling furnace 50 includes a rotating shaft 2 running through the center of the housing 1, and a rake arm 3 arranged on the rotating shaft 2; rake teeth 4 are arranged at intervals on the rake arm 3, and the rotating shaft 2 is connected to a power source such as a reduction motor 5. In addition, the rake teeth 4 are arranged above the support 100, so that the rake teeth 4 push the falling materials on the support 100, which is conducive to fully mixing and conveying the materials on the support 100.

[0057] The rotating shaft 2 is configured as a double-layer hollow rotating shaft including an inner layer shaft 21 and an outer layer shaft 22, and a cooling air inlet 23 and a cooling air outlet 24 are provided on the double-layer hollow rotating shaft, wherein the cooling air inlet 23 is connected to the inner layer shaft 21, and the cooling air outlet 24 is connected to the outer layer shaft 22;

[0058] The rake arm 3 is configured as a double-layer hollow rake arm including an inner rake arm 31 and an outer rake arm 32, wherein the inner rake arm 31 of the double-layer hollow rake arm is connected to the inner shaft 21 of the double-layer hollow rotating shaft, and the outer rake arm 32 of the double-layer hollow rake arm is connected to the outer shaft 22 of the double-layer hollow rotating shaft; wherein nozzles 310 are distributed on the inner rake arm 31 of the double-layer hollow rake arm 3.

[0059] Through the structural coordination design of the hollow rotating shaft 2 and the rake arm 3, cooling air is introduced into the rotating shaft 2, so that the cooling air flows from the inner layer shaft 21 into the inner layer rake arm 31, then flows from the nozzle 310 of the inner layer rake arm 31 into the outer layer rake arm 32, and finally flows from the outer layer rake arm 32 into the outer layer shaft 22, thereby ensuring the safety of the rotating shaft 2 and the rake arm 3. Preferably, the nozzles are evenly distributed on the inner layer rake arm 31, so that the cooling air evenly enters the outer layer rake arm 32 and the cavity of the rotating shaft 2, thereby ensuring the safety and reliability of the rotating shaft 2 and the rake arm 3.

[0060] As a preferred solution, the rake teeth are installed on the rake arm with an adjustable inclination angle. By controlling the inclination angle of the rake arm and the rake teeth, the pushing direction of the rake teeth in the furnace is consistent with the direction of entering the lower furnace. In this embodiment, the rake teeth 4 are installed at a certain angle to the rake arm 3. By adjusting the inclination angle of the rake teeth 3, the movement direction of the solid waste material in the furnace can be changed. And preferably, when the support member 100 forms a blanking portion at the center of the shell 1, the blanking portion is located between the rotating shaft 2 and the support member 100, and the blanking portion is set as a circular hole in the center of the shell; corresponding to the rake teeth 4 arranged on the upper side of the support member 100 of this layer, the number of rake teeth 4 pushed toward the center of the furnace is greater than the number of rake teeth 4 pushed toward the periphery of the furnace; when the support member 100 forms a blanking portion at the inner wall of the shell 1, the blanking portion is located between the inner wall of the shell and the support member, and the blanking portion has a plurality of square holes evenly distributed on the outer peripheral surface of the furnace; for the rake teeth 4 on the support member 100 of this layer, the number of rake teeth pushed toward the periphery of the furnace is greater than the number of rake teeth pushed toward the center of the furnace. Based on this, when the blanking part of the multi-layer furnace is in the center, the number of rake teeth pushed toward the center of the furnace is greater than that of rake teeth pushed toward the periphery of the furnace, so that the solid waste moves toward the center of the furnace as a whole while flipping back and forth, and finally falls into the lower furnace from the blanking part in the center; when the blanking part of the multi-layer furnace is on the outside, the number of rake teeth pushed toward the periphery of the furnace is greater than that of rake teeth pushed toward the center of the furnace, so that the solid waste moves toward the periphery of the furnace as a whole while flipping back and forth, and finally falls into the lower furnace from the blanking part on the periphery of the furnace, which further improves the step-by-step processing efficiency of the material in the furnace while ensuring the processing effect. Usually, the rake arm 3 and the rake teeth 4 are made of high temperature resistant and wear-resistant castings.

[0061] More specifically, in order to effectively process the multiphase materials in the furnace, Figure 1 As shown:

[0062] The shell 1 corresponding to the combustion furnace 10 is provided with a secondary air inlet 101, a low calorific value waste liquid inlet 102, a multi-media burner 103 and a combustion flue gas outlet 105. The multi-media burner 103 is provided with combustion air, high calorific value waste gas, high calorific value waste liquid, and auxiliary fuel inlets. More specifically, the combustion flue gas outlet 105 is provided at the top of the shell, so that the flue gas is fully burned and utilized in the combustion furnace 10 before being discharged.

[0063] A solid waste inlet 201 and a wastewater inlet 202 are provided on the shell corresponding to the drying furnace 20, and a multi-media burner 203 is connected. A material drop port 204 is provided on the support 100 located between the drying furnace 20 and the lower furnace; the multi-media burner 203 is provided with combustion-supporting air, high calorific value waste gas, high calorific value waste liquid, and auxiliary fuel inlets.

[0064] A secondary air inlet 301 is provided on the shell corresponding to the pyrolysis furnace 30, and a multi-media burner 302 is also connected. A material drop opening 303 is provided on the support 100 between the pyrolysis furnace 30 and the lower furnace. The multi-media burner 302 is provided with inlets for combustion-supporting air, nitrogen-containing waste gas, nitrogen-containing waste liquid, and auxiliary fuel.

[0065] A secondary air inlet 401 is provided on the shell corresponding to the slag combustion furnace 40, and a multi-media burner 402 is also connected. A material drop port 403 is provided on the support 100 between the slag combustion furnace 40 and the lower furnace. The multi-media burner 402 is provided with inlets for combustion-supporting air, high calorific value waste gas, high calorific value waste liquid, and auxiliary fuel.

[0066] It should be noted that the number of multi-media burners installed 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 various waste treatment amounts and the nature of the waste to be treated. Usually, 1 to 4 multi-media burners are installed in each furnace layer.

[0067] The shell corresponding to the cooling furnace 50 is provided with a primary air inlet 501 and a low calorific value exhaust gas inlet 502, and the support member 100 at the bottom of the cooling furnace 50 is provided with a slag discharge port 503 for dropping materials. Figure 1 As shown in FIG. 5 , in order to facilitate the collection of ash, the slag discharge port 503 is located at the outer periphery of the cooling furnace 50 .

[0068] According to the above embodiment, the present invention can also specifically implement a multi-chamber multi-phase low-nitrogen combustion treatment process, including the following steps:

[0069] S1. Low calorific value waste liquid is sent to the combustion furnace 10 of the multi-hearth furnace through the corresponding inlet for treatment; waste water is sent to the drying furnace 20 of the multi-hearth furnace through the corresponding inlet for evaporation treatment; solid waste is sent to the drying furnace 20 of the multi-hearth furnace through the corresponding inlet, and the dried solid waste is sent to the pyrolysis furnace 30 through the feeding mechanism; nitrogen-containing waste gas and / or nitrogen-containing waste liquid is sent to the pyrolysis furnace 30 through the corresponding inlet for treatment; wherein the heat of the pyrolysis furnace 30 is provided by the corresponding multi-media burner 302 and the combustion flue gas of the lower furnace;

[0070] S2. The gaseous pyrolysis products produced in the pyrolysis furnace enter the topmost combustion furnace 10 through the upper drying furnace 20, and the solid pyrolysis products produced in the pyrolysis furnace 30 enter the lower slag combustion furnace 40 for combustion. The heat generated by the combustion process in the slag combustion furnace is used for pyrolysis treatment in the upper pyrolysis furnace 30. Thus, the pyrolysis products are completely burned and purified through the combustion furnace 10 and the slag combustion furnace 40 arranged above and below, and the obtained ash is discharged after being cooled by heat exchange with low calorific value exhaust gas and primary air in the cooling furnace 50.

[0071] The above steps are further optimized to obtain better multiphase material processing effects:

[0072] In step S1, secondary air (i.e., combustion air) is delivered into the combustion furnace 10 through the secondary air inlet 101, and low calorific value waste liquid is sprayed into the combustion furnace 10 through the low calorific value waste liquid inlet 102. The combustion furnace 10 is also provided with a multi-media burner 103 and a flue gas outlet 105. The multi-media burner 103 is provided with interfaces for high calorific value waste liquid, high calorific value waste gas, auxiliary fuel and combustion air. The high calorific value waste liquid and waste gas are burned through the multi-media burner 103 to ensure that the combustion furnace temperature is between 850°C and 1150°C; by adjusting the amount of secondary air entering, the oxygen content of the combustion furnace is ensured to be between 1% and 6%, so that the combustible components in the waste liquid, waste gas and the escaping gas from the lower furnace (the following supplementary instructions) are completely burned in the combustion furnace, and the flue gas after combustion is discharged from the flue gas outlet 105 of the combustion furnace.

[0073] Solid waste is fed into the drying furnace 20 through the solid waste inlet 201, and wastewater is sprayed into the drying furnace 20 through the wastewater inlet 202. The drying furnace is also provided with a multi-media burner 203 and a material drop port 204; the multi-media burner 203 is provided with interfaces for high calorific value waste liquid, high calorific value waste gas, auxiliary fuel and combustion-supporting air; by adjusting the flow of high calorific value waste liquid, high calorific value waste gas and auxiliary fuel, the temperature of the drying furnace 20 is controlled at 150°C to 300°C to ensure that the solid waste is completely dried in the drying furnace 20. More specifically, the feeding mechanism in the drying furnace 20, specifically, the rake teeth 4 in the feeding mechanism, provide a turning and stirring effect on the solid waste, to ensure that the solid waste is fully dried and fed into the lower furnace through the material drop port 204 for further processing.

[0074] Among them, the escaped gas from the lower furnace entering the combustion furnace 10, including the gaseous pyrolysis products of the pyrolysis furnace 30, first enters the drying furnace 20 with the high-temperature flue gas, and the gaseous pyrolysis products and the high-temperature flue gas exchange heat with the solid waste and wastewater in the drying furnace 20 to reduce the temperature, and the water in the solid waste and wastewater is evaporated; the gaseous pyrolysis products, the high-temperature flue gas and the dried and evaporated water pass through the porous distribution plate 104 of the combustion furnace 10 and enter the top combustion furnace 10. In the top combustion furnace 10, a large amount of air is sent into the combustion furnace 10 through the secondary air inlet 101, and the combustion of high calorific value waste gas, high calorific value waste liquid and auxiliary fuel in the multi-media burner 103 can ensure that the temperature required for the combustion reaction is maintained in the combustion furnace 10, and in this way, the gaseous products of pyrolysis can be completely burned.

[0075] The dried solid waste falls into the pyrolysis furnace 30 from the upper drying furnace drop port 204. The pyrolysis furnace 30 is provided with a secondary air inlet 301, a multi-media burner 302 and a drop port 304. The multi-media burner 302 is provided with interfaces for nitrogen-containing waste gas and nitrogen-containing waste liquid, auxiliary fuel and combustion-supporting air. The temperature of the pyrolysis furnace is ensured to be between 900°C and 1300°C by the combustion of nitrogen-containing waste gas, nitrogen-containing waste liquid and auxiliary fuel. The air volume entering the secondary air inlet 301 is adjusted to ensure that the air-fuel ratio in the pyrolysis furnace is maintained between 0.6 and 0.9, so that the nitrogen-containing waste gas and nitrogen-containing waste liquid are burned and pyrolyzed in a high-temperature oxygen-deficient environment, and at the same time, reaction heat is provided, so that the dried solid waste is heated to the temperature required for the reaction and fully pyrolyzed. In a reducing atmosphere, the raw nitrogen in the waste gas and waste liquid is converted into N2, and the NOx in the waste gas itself is also reduced to N2 in a reducing atmosphere. When the raw material contains NH3, the pyrolysis temperature should be basically controlled at 1300°C to ensure that the NH3 with higher activation energy is completely reacted, and at the same time, the temperature in the subsequent residue combustion furnace 40 will not be too high due to excessive temperature, and the thermodynamic NOx generation will not increase. The specific temperature control is adjusted according to the composition of the gas, liquid and solid wastes to be treated, thereby inhibiting the conversion of ammonia nitrogen in the raw material into NOx, and converting the NOx contained in the waste gas into N2. In addition, the rake teeth 4 in the pyrolysis furnace 30 stir the solid waste to ensure that the solid pyrolysis products are fully in contact with the secondary air used for combustion, and the stirring of the rake teeth 4 causes the pyrolyzed solid waste to be discharged downward toward the discharge port 304.

[0076] The solid waste after pyrolysis falls into the slag combustion furnace 40 from the drop port 304 of the upper pyrolysis furnace 30. The slag combustion furnace 40 is provided with a secondary air inlet 401, a multi-media burner 402 and a drop port 403; the multi-media burner 402 is provided with interfaces for high calorific value waste liquid, high calorific value waste gas, auxiliary fuel and combustion-supporting air; by adjusting the flow of high calorific value waste liquid, waste gas and auxiliary fuel, the high calorific value waste liquid and waste gas are fully burned in the slag combustion furnace 40; and the temperature of the slag combustion furnace is ensured to be between 850°C and 1100°C. By adjusting the amount of air entering through the secondary air inlet 401, the oxygen content of the slag combustion furnace 40 is ensured to be between 3% and 6%, so that the waste liquid, waste gas and pyrolysis residue (solid pyrolysis products) are completely burned in the slag combustion furnace. Furthermore, the solid pyrolysis products are stirred and turned by the rake teeth 4 in the residue combustion furnace, thereby ensuring that the solid pyrolysis products are fully in contact with the secondary air, so that the pyrolysis residue is fully and completely burned.

[0077] The ash remaining after combustion in the slag combustion furnace 40 falls into the cooling furnace 50 from the drop port 403 of the upper slag combustion furnace 40. The slag combustion furnace is also provided with a primary air inlet 501, a low calorific value waste gas inlet 502 and a slag discharge port 503. The ash is directly contacted with the primary air and the low calorific value waste gas in the cooling furnace 50 for heat exchange. After the ash temperature is reduced, it is discharged through the slag discharge port 503, and the primary air and the low calorific value waste gas are preheated. This method is helpful for ash heat recovery and reduces the operating cost of waste gas, waste liquid and solid waste disposal. In addition, the rake teeth 4 in the cooling furnace 50 stir the ash to ensure that the ash is fully in contact with the low calorific value waste gas and primary air, and then discharged from the slag discharge port. The ash and slag are directly contacted with the primary air and low calorific value waste gas in the cooling furnace. The preheated primary air and low calorific value waste gas flow upward, passing through the residue combustion furnace 40, the pyrolysis furnace 30, the drying furnace 20, and the combustion furnace 10, and participate in the combustion reaction in the residue combustion furnace 40, the pyrolysis furnace 30, and the combustion furnace 10; the ash and slag temperature is reduced and discharged through the slag discharge port. By controlling the amount of primary air and low calorific value waste gas, the secondary air of each furnace, and the power of the multi-media burner, the oxygen content and temperature parameters of each furnace are guaranteed to meet the requirements.

[0078] In the above embodiment, by combining the drying, pyrolysis and combustion processes, the multiple furnaces are respectively a combustion furnace 10, a drying furnace 20, a pyrolysis furnace 30, a residue combustion furnace 40 and a cooling furnace 50 from top to bottom. The pyrolysis furnace 30 provides the high temperature required for the pyrolysis of the raw materials by burning the auxiliary fuel in the multi-media burner 302 and providing sufficient oxygen for its combustion process. The specific temperature control is adjusted according to the composition of the three wastes of gas, liquid and solid to be processed, so as to achieve sufficient pyrolysis of different phase substances. Since there are dry solid wastes falling from the upper drying furnace 20 and nitrogen-containing waste liquid and nitrogen-containing waste gas sent in through the multi-media burner 302 in the pyrolysis furnace 30, the pyrolysis furnace as a whole is in an oxygen-deficient state. In the oxygen-deficient state, solid wastes, waste liquids and waste gases will pyrolyze to produce a large amount of reducing gases such as CO, H2, hydrocarbons, etc. Inside the pyrolysis furnace, amino groups, nitro groups in nitrogen-containing waste liquids, nitrogen-containing waste gases and solid wastes, as well as NOx and NH3 in nitrogen-containing waste gases, etc., undergo oxidation-reduction reactions with reducing gases such as CO and H2 or with each other, and eventually generate N2 and H2O. The solid residues after the pyrolysis stage treatment enter the residue combustion furnace 40 downward, and the gaseous pyrolysis products pass upward through the drying furnace 20 into the combustion furnace 10 on the top layer, and the heat of the pyrolysis flue gas is used to dry the solid wastes. By adopting a multi-furnace structure, the raw materials can be dried, pyrolyzed and burned step by step. By integrating the advantages of drying, pyrolysis and combustion, combined with process parameter control, the NOx conversion rate of the raw nitrogen in the waste gas, waste liquid and solid waste can be guaranteed to be less than 5%, and the efficiency of reducing NOx in the raw waste gas to N2 is above 95%. This process can greatly reduce the NOx concentration at the outlet of the incinerator, and reduce the subsequent flue gas denitrification treatment equipment and operating costs. It can greatly reduce the NOx conversion rate of the raw nitrogen in the waste gas, waste liquid and solid waste, reduce the NOx concentration at the outlet of the incinerator, and reduce the subsequent flue gas denitrification treatment equipment and operating costs.

[0079] In addition, according to the moisture content, pyrolysis characteristics, and combustion characteristics of the processed materials, different number of setting layers can be selected for the drying furnace, pyrolysis furnace, and residue combustion furnace to fully ensure the material disposal effect. Specifically, according to the moisture content and characteristics of the materials, drying furnaces with different numbers of layers can be designed, and by controlling the heat supply of the multi-media burner in the drying furnace, it can be ensured that solid waste with any moisture content can be completely dried in the drying furnace, thereby further ensuring the complete combustion of the solid waste. According to the characteristics of the materials and the ammonia nitrogen content, pyrolysis furnaces with different numbers of layers can be designed, and by controlling the heat supply of the multi-media burner in the pyrolysis furnace, it can be ensured that the waste gas, waste liquid, and solid waste react completely in the pyrolysis furnace. According to the combustion characteristics of the pyrolysis residue of the material, residue combustion furnaces with different numbers of layers can be designed, and by controlling the heat supply and secondary air volume of the multi-media burner in the residue combustion furnace, it can be ensured that the thermal burn rate of the ash discharged from the bottom layer is controlled below 1% to 3%.

[0080] Several specific embodiments are provided below:

[0081] Example 1 Comprehensive treatment project of gas, liquid and solid wastes in a chemical plant

[0082] Raw materials: The combustion raw materials include 1 solid waste, 3 waste liquids, and 2 waste gases. The total nitrogen content of the raw materials is about 0.73%wt (calculated as N, excluding N2 content).

[0083] Solid waste 1: Chemical sludge (water content 85%)

[0084] Solid waste 2: Oily sludge (water content 85%, oil content ≤ 2%)

[0085] Waste liquid 1: Acrylonitrile waste liquid (containing 5.4%wt C3H5N, the rest is water)

[0086] Waste liquid 2: Fusel alcohol waste liquid (containing 37%wt CH4O, 15.4%wt C2H6O, 5.3%wt C3H8O, 5.3%wtC4H 10 O, 2.7%wt C5H 12 O, 2.3%wt C6H 14 O, the rest is water)

[0087] Wastewater 3: Ethanol tower wastewater (containing 10.88%wt C2H6O2, 4.87%wt C5H 12 O, 0.34%wt C2H6O, 0.26%wt C3H8O, 1.13%wt C4H 10 O, 0.7%wt C3H8O2, the rest is water)

[0088] Waste gas 1: Absorption tower discharges air (containing 58mg / Nm 3 C3H3N, 926mg / Nm 3 NO2, 88.34%wt N2, 1.03%wt CO, the rest are inert gases, oxygen, water)

[0089] Waste gas 2: Recovery tower releases air (containing 30mg / Nm 3 CH4, 100mg / Nm 3 COS, 50mg / Nm 3 CO, 14.32%wtH2S, 27.78%wt H2O, 22.5%wt NH3, 35.4%wt CO2, the rest are inert gases, oxygen, water)

[0090] Exhaust 3: Transport air (containing 30mg / Nm 3 CH4O, the rest is air)

[0091] Combustion treatment device: The device of the present invention is used, and a total of 13 furnaces are arranged (from top to bottom, 1 combustion furnace, 3 drying furnaces, 3 pyrolysis furnaces, 4 residue combustion furnaces, and 2 cooling furnaces are arranged in sequence).

[0092] Feeding: solid waste 1 and solid waste 2 are fed into the drying furnace 20 through the solid waste inlet 201 by the feeder, and then fed into the pyrolysis furnace 30 (rotary pyrolysis furnace) from the blanking part after drying; high nitrogen waste liquid 1 is fed into the pyrolysis furnace 30 through the waste liquid spray gun through the multi-media burner 302; high nitrogen waste gas 1 and 2 are fed into the pyrolysis furnace 30 through the waste gas spray gun through the multi-media burner 302; waste liquid 2 and waste liquid 3 have high calorific value, and are fed into the combustion furnace 10, drying furnace 20, pyrolysis furnace 30, and residue combustion furnace 40 through the waste liquid spray gun through the multi-media burner 103 / 203 / 302 / 402 for fuel use; waste gas 3 has low calorific value and is fed into the cooling furnace through the low calorific value waste gas inlet 502. In addition, the multi-media burner of each furnace is provided with an auxiliary fuel interface and a combustion air interface for adjusting the combustion temperature and oxygen content of each furnace.

[0093] Combustion treatment process: The temperature of the combustion furnace 10 is controlled at 1150°C, and the air-fuel ratio is 1.15; the temperature of the drying furnace 20 is controlled at 300°C±10°C; the temperature of the pyrolysis furnace 30 is controlled at 1250-1280°C, and the air-fuel ratio is 0.85; the temperature of the residue combustion furnace 40 is controlled at 850°C, and the air-fuel ratio is 1.4 (i.e., 6% oxygen content).

[0094] Treatment effect: NOx concentration of flue gas at the incinerator outlet: 200mg / Nm 3 The outlet oxygen concentration is about 3.0%, VOCs cannot be detected, the NOx conversion rate of the entire raw nitrogen is about 1.35%, and the ash thermal burn-off rate is about 2.5%.

[0095] Example 2: Comprehensive treatment project of gas, liquid and solid wastes in a chemical plant

[0096] Raw materials: Same as Example 1.

[0097] Combustion treatment device: The device of the present invention is used, and a total of 13 furnaces are arranged (from top to bottom, 1 combustion furnace, 3 drying furnaces, 4 pyrolysis furnaces, 3 residue combustion furnaces, and 2 cooling furnaces are arranged in sequence).

[0098] Feed: Same as Example 1.

[0099] Combustion treatment process: The temperature of the combustion furnace 10 is controlled at 1150°C, and the air-fuel ratio is 1.1 (i.e., 2% oxygen content); the temperature of the drying furnace 220 is controlled at 300°C±10°C; the temperature of the pyrolysis furnace 30 is controlled at 1200-1250°C, and the air-fuel ratio is 0.80; the temperature of the residue combustion furnace 40 is controlled at 950°C, and the air-fuel ratio is 1.4.

[0100] Treatment effect: NOx concentration of flue gas at the incinerator outlet: 175mg / Nm 3 The outlet oxygen concentration is about 2.1%, VOCs cannot be detected, the NOx conversion rate of the entire raw nitrogen is about 1.2%, and the ash thermal burn-off rate is about 1.5%.

[0101] Example 3: Comprehensive treatment project of gas, liquid and solid wastes in a chemical plant

[0102] Raw materials: Same as Example 1.

[0103] Combustion treatment device: The device of the present invention is used, and a total of 13 furnaces are arranged (from top to bottom, 1 combustion furnace, 3 drying furnaces, 4 pyrolysis furnaces, 4 residue combustion furnaces, and 1 cooling furnace).

[0104] Feed: Same as Example 1.

[0105] Combustion treatment process: The combustion furnace temperature is controlled at 1125°C, and the air-fuel ratio is 1.15; the drying furnace temperature is controlled at 300°C±10°C; the pyrolysis furnace temperature is controlled at 1250-1280°C, and the air-fuel ratio is 0.8; the residue combustion furnace temperature is controlled at 850°C, and the air-fuel ratio is 1.3 (i.e., 4.8% oxygen content).

[0106] Treatment effect: NOx concentration of flue gas at the incinerator outlet: 180mg / Nm 3 The outlet oxygen concentration is about 3.1%, VOCs cannot be detected, the NOx conversion rate of the entire raw nitrogen is about 1.21%, and the ash thermal burn-off rate is about 2.4%.

[0107] Example 4: Comprehensive treatment project of gas, liquid and solid wastes in a chemical plant

[0108] Raw materials: Same as Example 1.

[0109] Combustion treatment device: Same as Example 3.

[0110] Feed: Same as Example 1.

[0111] Combustion treatment process: The combustion furnace temperature is controlled at 1150°C, and the air-fuel ratio is 1.25 (i.e., 4.2% oxygen content); the drying furnace temperature is controlled at 300°C±10°C; the pyrolysis furnace temperature is controlled at 1200-1270°C, and the air-fuel ratio is 0.75; the residue combustion furnace temperature is controlled at 850°C, and the air-fuel ratio is 1.35.

[0112] Treatment effect: NOx concentration of flue gas at the incinerator outlet: 230mg / Nm 3The outlet oxygen concentration is about 4.2%, VOCs cannot be detected, the NOx conversion rate of the entire raw nitrogen is about 1.55%, and the ash thermal burn-off rate is about 2.2%.

[0113] Example 5: Comprehensive treatment project of gas, liquid and solid wastes in a chemical plant

[0114] Raw materials: Contains 2 types of solid wastes, 6 types of waste liquids, and 3 types of waste gases. The total nitrogen content of the raw materials is 3.24%wt (calculated as N, excluding N2 content).

[0115] Solid waste 1: waste activated carbon;

[0116] Solid waste 2: waste catalyst (80% water, 10% catalyst, 10% organic matter);

[0117] Waste liquid 1: Scrubber wastewater (containing about 8% of salts such as Na2SO4 and NaCl, and the rest is water);

[0118] Waste liquid 2: saturated waste brine (containing 20% ​​to 30% Na2SO4, 15% to 20% glycine, and the rest is water);

[0119] Waste liquid 3: ethanol tower wastewater (containing 4.78%wt amyl alcohol, 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, and the rest is water);

[0120] Waste liquid 4: ethylene glycol light component (containing 20.74%wt methyl glycolate, 30.99%wt butanediol, 27.57%wt ethylene glycol, 0.01%wt diethylene glycol, and the rest is water);

[0121] Waste liquid 5: ethylene glycol heavy component (containing 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);

[0122] Waste liquid 6: fusel oil (containing 8%wt methyl formate, 72%wt methanol, and 20%wt ethanol);

[0123] Waste gas 1: MN recovery tower vent air (containing 1.25%wt methyl nitrite, 2.96%wt NO, 1.2%wt N2O, 0.63%wt methylal, 0.83%wt methanol, 12.42%wt CO, and the rest is inert gas N2 and CO2);

[0124] Waste gas 2: conversion stripping tower acid gas components (containing 22.5% wt ammonia, 14.32% wt H2S, 0.01% wt H2, 0.05% wt CO, the rest is CO2 and water vapor);

[0125] Waste gas 3: DMC device waste gas (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, and the rest is N2, CO2 and water vapor).

[0126] Combustion treatment device: The device of the present invention is used, and a total of 15 furnaces are arranged (from top to bottom, 1 combustion furnace, 3 drying furnaces, 4 pyrolysis furnaces, 5 residue combustion furnaces, and 2 cooling furnaces are arranged in sequence).

[0127] Feeding: solid waste 1 and solid waste 2 are fed into the drying furnace 20 through the solid waste inlet 201 by the feeder, and then fed into the pyrolysis furnace 30 (rotary pyrolysis furnace) from the blanking part after drying; high nitrogen waste liquid 2 is fed into the pyrolysis furnace 30 through the waste liquid spray gun via the multi-media burner 302; high nitrogen waste gases 1, 2, and 3 are fed into the pyrolysis furnace 30 through the waste gas spray gun via the multi-media burner 302; waste liquid 3 is fed into the combustion furnace 10 through the low calorific value waste liquid inlet 102; waste liquid 1 is fed into the drying furnace 20 through the wastewater inlet 202; waste liquid 4, waste liquid 5, and waste liquid 6 have higher calorific values, and are fed into the combustion furnace 10, drying furnace 20, pyrolysis furnace 30, and residue combustion furnace 40 through the waste liquid spray gun via the multi-media burners 103 / 203 / 302 / 402 for use as fuel. In addition, the multi-media burner in each furnace is provided with an auxiliary fuel interface and a combustion-supporting air interface for adjusting the combustion temperature and oxygen content of each furnace.

[0128] Combustion treatment process: The combustion furnace temperature is controlled at 1150°C, and the air-fuel ratio is 1.10; the drying furnace temperature is controlled at 300°C±10°C; the pyrolysis furnace temperature is controlled at 1250-1280°C, and the air-fuel ratio is 0.85; the residue combustion furnace temperature is controlled at 850°C, and the air-fuel ratio is 1.4 (i.e., 6% oxygen content).

[0129] Treatment effect: NOx concentration of flue gas at the incinerator outlet: 200mg / Nm 3 The outlet oxygen concentration is about 2.1%, VOCs cannot be detected, the NOx conversion rate of the entire raw nitrogen is about 0.62%, and the ash thermal burn-off rate is about 1.3%.

[0130] Example 6: Comprehensive treatment project of gas, liquid and solid wastes in a chemical plant

[0131] Raw materials: Same as Example 5.

[0132] Combustion treatment device: The device of the present invention is used, and a total of 15 furnaces are arranged (from top to bottom, 1 combustion furnace, 3 drying furnaces, 5 pyrolysis furnaces, 5 residue combustion furnaces, and 1 cooling furnace).

[0133] Feed: Same as Example 5.

[0134] Combustion treatment process: The combustion furnace temperature is controlled at 1150℃, and the air-fuel ratio is 1.15; the drying furnace temperature is controlled at 300℃±10℃; the pyrolysis furnace temperature is controlled at 1250~1280℃, and the air-fuel ratio is 0.65; the residue combustion furnace temperature is controlled at 850℃, and the air-fuel ratio is 1.4.

[0135] Treatment effect: NOx concentration of flue gas at the incinerator outlet: 120mg / Nm 3 The outlet oxygen concentration is about 2.1%, VOCs cannot be detected, the NOx conversion rate of the entire raw nitrogen is about 0.37%, and the ash thermal loss rate is about 1.5%.

[0136] Example 7: Comprehensive treatment project of gas, liquid and solid wastes in a chemical plant

[0137] Raw materials: Same as Example 5.

[0138] Combustion treatment device: The device of the present invention is used, and a total of 13 furnaces are arranged (from top to bottom, 1 combustion furnace, 2 drying furnaces, 5 pyrolysis furnaces, 4 residue combustion furnaces, and 1 cooling furnace).

[0139] Feed: Same as Example 5.

[0140] Combustion treatment process: The combustion furnace temperature is controlled at 1150℃, and the air-fuel ratio is 1.15; the drying furnace temperature is controlled at 350℃±10℃; the pyrolysis furnace temperature is controlled at 1250~1280℃, and the air-fuel ratio is 0.7; the residue combustion furnace temperature is controlled at 850℃, and the air-fuel ratio is 1.4.

[0141] Treatment effect: NOx concentration of flue gas at the incinerator outlet: 150mg / Nm 3 The outlet oxygen concentration is about 2.1%, VOCs cannot be detected, the NOx conversion rate of the entire raw nitrogen is about 0.62%, and the ash thermal burn-off rate is about 1.65%.

[0142] Example 8: Comprehensive treatment project of gas, liquid and solid wastes in a chemical plant

[0143] Raw materials: Same as Example 5.

[0144] Combustion treatment device: Same as Example 7.

[0145] Feed: Same as Example 5.

[0146] Combustion treatment process: The combustion furnace temperature is controlled at 1150℃, and the air-fuel ratio is 1.2; the drying furnace temperature is controlled at 350℃±10℃; the pyrolysis furnace temperature is controlled at 1250~1280℃, and the air-fuel ratio is 0.85; the residue combustion furnace temperature is controlled at 900℃, and the air-fuel ratio is 1.4.

[0147] Treatment effect: NOx concentration of flue gas at the incinerator outlet: 220mg / Nm 3 The outlet oxygen concentration is about 3.5%, VOCs cannot be detected, the NOx conversion rate of the entire raw nitrogen is about 0.68%, and the ash thermal reduction rate is about 1.25%.

[0148] Comparative Example 1: A factory high nitrogen waste gas and waste liquid incineration project

[0149] Raw materials: The combustion raw materials include 4 waste liquids and 2 waste gases, and the total nitrogen content of the raw materials is 2.35%wt (calculated as N, excluding N2 content).

[0150] Waste liquid 1: MMA device waste acid (containing 52.2%wt ammonium bisulfate, 7.4%wt MAA, 17.4%wt sulfuric acid, and the rest is water),

[0151] Waste liquid 2: Waste acid from acrylonitrile plant (containing 39.5%wt ammonium sulfate, 21%wt acrylic acid, 14.5%wt C6H8N2, and the rest is water),

[0152] Waste liquid 3: Alkylation unit waste acid (containing 91%wt sulfuric acid, 8.2%wt N-C5H1 acrylic acid, and the rest is water),

[0153] Waste liquid 4: MMA device wastewater (containing 0.4%wt sulfuric acid, 1%wt MMA, 4.4%wt acetone, and the rest is water).

[0154] Waste gas 1: MMA device waste 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 SO2, the rest are inert gases, oxygen, water)

[0155] Waste gas 2: H2S gas (containing 95%v H2S, 0.08%v C1+C2+C3, and the rest being inert gases, oxygen, and water).

[0156] Combustion treatment device: a two-stage combustion furnace consisting of a vertical pyrolysis furnace and a horizontal oxidation furnace.

[0157] Feeding: waste gases 1 and 2 are fed into the pyrolysis furnace through waste gas spray guns, and waste liquids 1, 2, 3, and 4 are directly fed into the pyrolysis furnace through waste liquid spray guns. The temperature of the combustion device is controlled by the combustion of supplementary fuel.

[0158] Combustion treatment process: The pyrolysis furnace temperature is controlled at 1350°C, and the air-fuel ratio is 0.85; the oxidation furnace temperature is controlled at 1100°C, and the air-fuel ratio is 1.5.

[0159] Treatment effect: NOx concentration of flue gas at the incinerator outlet: 500mg / Nm 3 The outlet oxygen concentration is about 7.0%, VOCs cannot be detected, and the NOx conversion rate of the entire raw nitrogen is about 2.2%.

[0160] Comparative Example 2: Incineration project of high nitrogen content waste gas and waste liquid in a factory

[0161] Raw materials: Same as Example 9.

[0162] Combustion treatment device: a two-stage combustion furnace consisting of a pre-combustion chamber and a burnout chamber.

[0163] Feeding: waste gases 1, 2 and waste liquids 1, 2, 3, 4 are respectively fed into the pre-combustion chamber through waste gas and waste liquid spray guns arranged on the multi-media burner, and the temperature of the combustion device is controlled by the combustion of supplementary fuel.

[0164] Combustion treatment process: Control the combustion temperature of the burnout chamber to 1100-1150℃.

[0165] Treatment effect: NOx concentration of flue gas at the incinerator outlet: 9500mg / Nm 3 The outlet oxygen concentration is about 6.0%, and the non-methane total hydrocarbons occasionally exceed 20 mg / Nm 3 , the NOx conversion rate of the entire raw nitrogen is about 40.4%.

[0166] It should be noted that the above embodiments can be freely combined as needed. The above is only a preferred embodiment of the present invention. It should be pointed out that for ordinary technicians in this technical field, several improvements and modifications can be made without departing from the principle of the present invention, and these improvements and modifications should also be considered as the protection scope of the present invention.

Claims

1. A multi-chamber multi-phase low nitrogen combustion treatment device, characterized in that: include: A shell, wherein a plurality of furnaces are formed by dividing the shell; the plurality of furnaces include a combustion furnace, a drying furnace, a pyrolysis furnace, a residue combustion furnace, and a cooling furnace, which are arranged from top to bottom, and the plurality of furnaces are connected in sequence; Wherein, a feeding mechanism for mixing materials in at least one furnace other than the combustion furnace and feeding the materials to the lower furnace is provided through the center of the shell; The combustion furnace is provided with a low calorific value waste liquid inlet, a combustion air inlet, and a smoke outlet; The drying furnace is provided with a solid waste inlet and a wastewater inlet; The pyrolysis furnace and the residue combustion furnace are both provided with combustion air inlets; The cooling furnace is provided with a combustion air inlet, a low calorific value waste gas inlet and a slag discharge port; The combustion furnace, drying furnace, pyrolysis furnace and residue combustion furnace are respectively connected to multi-media burners, and the multi-media burners corresponding to the pyrolysis furnace are respectively provided with inlets for combustion-supporting air, nitrogen-containing waste gas, nitrogen-containing waste liquid and auxiliary fuel; the multi-media burners corresponding to the combustion furnace, drying furnace and residue combustion furnace are respectively provided with inlets for combustion-supporting air, high calorific value waste gas, high calorific value waste liquid and auxiliary fuel.

2. The multi-chamber multi-phase low nitrogen combustion treatment device according to claim 1 is characterized in that: The combustion furnace and the drying furnace are separated by a porous distribution plate, and the surface of the porous distribution plate is evenly distributed with spaced holes.

3. The multi-chamber multi-phase low nitrogen combustion treatment device according to claim 2 is characterized in that: Multiple layers of support members are arranged on the lower side of the porous distribution plate in the shell, and a furnace is formed between two adjacent support members; any layer of support members alternately forms a blanking portion at the center of the shell or at the inner side wall of the shell.

4. The multi-chamber multi-phase low nitrogen combustion treatment device according to claim 3 is characterized in that: The feeding mechanism comprises a rotating shaft passing through the center of the housing, and a rake arm arranged on the rotating shaft; rake teeth are arranged at intervals on the rake arm, and the rotating shaft is drivingly connected to a power source; The rake teeth are arranged above the support member, so that the rake teeth can push the material falling from the support member.

5. The multi-chamber multi-phase low nitrogen combustion treatment device according to claim 4 is characterized in that: The rotating shaft is configured as a double-layer hollow rotating shaft including an inner layer shaft and an outer layer shaft, and a cooling air inlet and a cooling air outlet are provided on the double-layer hollow rotating shaft, wherein the cooling air inlet is connected to the inner layer shaft, and the cooling air outlet is connected to the outer layer shaft; The rake arm is configured as a double-layer hollow rake arm including an inner rake arm and an outer rake arm, the inner rake arm of the double-layer hollow rake arm is connected to the inner shaft of the double-layer hollow rotating shaft, and the outer rake arm of the double-layer hollow rake arm is connected to the outer shaft of the double-layer hollow rotating shaft; Wherein, nozzles are distributed on the inner rake arm of the double-layer hollow rake arm.

6. The multi-chamber multi-phase low nitrogen combustion treatment device according to claim 4 or 5, characterized in that: The rake teeth are installed on the rake arm with an adjustable inclination angle. By controlling the inclination angle of the rake arm and the rake teeth, the pushing direction of the rake teeth in the furnace is consistent with the direction of entering the lower furnace.

7. The multi-chamber multi-phase low nitrogen combustion treatment device according to claim 6 is characterized in that: When the support member forms a blanking portion at the center of the shell, the blanking portion is located between the rotating shaft and the support member, and the blanking portion is set as a circular hole in the center of the shell; for the rake teeth on the support member of this layer, the number of rake teeth pushed toward the center of the furnace is greater than the number of rake teeth pushed toward the periphery of the furnace; When the support member forms a blanking portion at the inner wall of the shell, the blanking portion is located between the inner wall of the shell and the support member, and the blanking portion has multiple square holes evenly distributed on the outer peripheral surface of the furnace; for the rake teeth on this layer of the support member, the number of rake teeth pushed toward the periphery of the furnace is greater than the number of rake teeth pushed toward the center of the furnace.

8. A multi-chamber multi-phase low nitrogen combustion treatment process, using the multi-chamber multi-phase low nitrogen combustion treatment device according to any one of claims 1 to 7 for treatment, characterized in that: The process includes the following steps: S1. Low calorific value waste liquid is sent to the combustion furnace of the multi-hearth furnace through the corresponding inlet for treatment; waste water is sent to the drying furnace of the multi-hearth furnace through the corresponding inlet for evaporation treatment; solid waste is sent to the drying furnace of the multi-hearth furnace through the corresponding inlet for drying treatment, and the dried solid waste is sent to the pyrolysis furnace through the feeding mechanism, and nitrogen-containing waste gas and / or nitrogen-containing waste liquid is sent to the pyrolysis furnace through the corresponding inlet for pyrolysis treatment; S2. The gaseous pyrolysis products produced in the pyrolysis furnace enter the topmost combustion furnace through the upper drying furnace, and the solid pyrolysis products produced in the pyrolysis furnace enter the lower slag combustion furnace through the feeding mechanism for combustion. The heat generated in the combustion process is used for pyrolysis treatment in the upper pyrolysis furnace. Thus, the pyrolysis products are completely burned and purified through the combustion furnaces and the slag combustion furnaces arranged above and below, and the obtained ash enters the cooling furnace through the feeding mechanism for heat exchange with low calorific value exhaust gas and then discharged.

9. The multiphase low nitrogen combustion treatment process according to claim 8, characterized in that: The high calorific value waste gas, high calorific value waste liquid and auxiliary fuel are burned by a multi-media burner, and the combustion furnace temperature is controlled at 850℃~1150℃; and the oxygen content in the combustion furnace is controlled between 1%~6%, so that the high calorific value waste liquid, high calorific value waste gas, low calorific value waste liquid and the combustible components in the escaped gas from the lower furnace are completely burned in the combustion furnace, and the smoke after combustion is discharged; The nitrogen-containing waste gas, nitrogen-containing waste liquid and auxiliary fuel are burned by a multi-media burner, the temperature of the pyrolysis furnace is controlled at 900℃~1300℃, and the air-fuel ratio in the pyrolysis furnace is controlled to be maintained between 0.6~0.9, so that the dried solid waste is fully pyrolyzed, and the raw nitrogen in the nitrogen-containing waste gas and nitrogen-containing waste liquid is converted into N2; High calorific value waste gas, high calorific value waste liquid and auxiliary fuel are burned through multi-media burners, and the temperature of the residue combustion furnace is controlled at 850℃~1100℃; the oxygen content of the residue combustion furnace is controlled between 3%~6%; and the high calorific value waste liquid, high calorific value waste gas and solid pyrolysis products are completely burned in the residue combustion furnace.

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