Oxygen-enriched incineration device for hazardous wastes

Abstract

The utility model relates to a hazardous waste oxygen-enriched incineration device which comprises a rotary kiln, a secondary combustion chamber and oxygen production equipment, a feeding port is formed in one side of the rotary kiln, and a first oxygen-enriched mixer is fixedly arranged at the position, close to the feeding port, in the rotary kiln; the other side of the rotary kiln fixedly communicates with the secondary combustion chamber, and a second oxygen-enriched mixer is installed in the middle of the interior of the secondary combustion chamber. The hazardous waste incineration system has the advantages that the oxygen-enriched incineration technology is applied to incineration treatment of hazardous waste, the hazardous waste incineration system is clean and efficient, meanwhile, the hazardous waste incineration system has the remarkable advantages of being high in incineration efficiency and low in pollutant emission, the problems that the hazardous waste incineration flue gas amount is large, nitric oxide is generated, the CO concentration is large, incineration is not thorough, operation is not stable, and equipment investment is large are effectively solved, and the hazardous waste incineration system is suitable for industrial production. And sustainable development of the environmental governance industry in China is facilitated.

Description

Technical Field

[0001] The utility model relates to the field of auxiliary components for incineration treatment of hazardous wastes, and particularly relates to an oxygen-enriched incineration device for hazardous wastes. Background Art

[0002] At present, due to the remarkable characteristics of high moisture content, high ash content, low calorific value, complex composition and unclear classification of hazardous wastes in China, the hazardous wastes in China face main problems such as unstable incineration and complex pollutants.

[0003] Specifically in the prior art, the existing incineration technologies for hazardous wastes mainly include: rotary kiln incineration technology, landfill technology, comprehensive utilization, etc. In practice, at present, the air rotary kiln incineration technology is basically adopted for the incineration of hazardous wastes. However, this technology not only has incomplete incineration and low combustion efficiency, but also has high CO concentration, complex gaseous pollutants such as NOx and dioxins, and high carbon emissions, which is not conducive to the sustainable development of the environmental governance industry in China. Content of the Utility Model

[0004] The purpose of the utility model is to provide an oxygen-enriched incineration device for hazardous wastes to solve the above problems. The oxygen-enriched incineration technology is applied to the incineration treatment of hazardous wastes, which is clean and efficient, and has the remarkable advantages of high incineration efficiency and low pollutant emissions. It effectively solves the problems such as large flue gas volume, generation of nitrogen oxides, high CO concentration, incomplete incineration, unstable operation and large equipment investment in the incineration of hazardous wastes, and is conducive to the sustainable development of the environmental governance industry in China. Details are described below.

[0005] To achieve the above purpose, the utility model provides the following technical solutions:

[0006] An oxygen-enriched incineration device for hazardous wastes provided by the utility model comprises a rotary kiln, a secondary combustion chamber and an oxygen generation device. An inlet is arranged on one side of the rotary kiln. A first oxygen-enriched mixer is fixedly arranged inside the rotary kiln near the inlet. The other side of the rotary kiln is fixedly connected to the secondary combustion chamber, and a second oxygen-enriched mixer is installed in the middle of the secondary combustion chamber;

[0007] The first oxygen-enriched mixer is respectively connected to a first oxygen pipeline for inputting oxygen and a first air pipeline for inputting air, and the first oxygen pipeline is connected to the oxygen generation device, so as to mix oxygen and air through the first oxygen-enriched mixer to obtain air with high-concentration oxygen and introduce it into the rotary kiln;

[0008] The second oxygen-enriched mixer is respectively connected with a second oxygen pipeline for inputting oxygen and a second gas pipeline for inputting gas, and the second oxygen pipeline is connected with the oxygen production equipment, so as to mix oxygen and air through the second oxygen-enriched mixer to obtain air with high-concentration oxygen and introduce it into the secondary combustion chamber.

[0009] Preferably, the oxygen production equipment is connected with a buffer tank through pipelines, and the first oxygen pipeline and the second oxygen pipeline are respectively connected with the oxygen production equipment through the buffer tank. The outer ends of the first gas pipeline and the second gas pipeline are respectively connected with a primary fan and a secondary fan for air supply.

[0010] Preferably, an observation port and a furnace drying burner port are arranged at the side of the rotary kiln at the position between the feeding port and the first oxygen-enriched mixer. An air outlet and a slag discharge port are respectively arranged at the top and bottom of the secondary combustion chamber.

[0011] Preferably, the air outlet of the secondary combustion chamber is connected with a waste heat boiler through a pipeline, and a denitration system for denitrating the discharged flue gas is connected to the pipeline between the air outlet and the waste heat boiler.

[0012] Preferably, the waste heat boiler is connected with a quench tower through a pipeline, and the quench tower is connected with a dry deacidification tower through a pipeline.

[0013] Preferably, the dry deacidification tower is connected with a bag filter through a pipeline, and the bag filter is connected with an alkali washing tower through a pipeline.

[0014] Preferably, the alkali washing tower is connected with an exhaust fan through a pipeline, and the exhaust fan is connected with a chimney through a pipeline.

[0015] Preferably, the oxygen concentration range of the first oxygen-enriched mixer and the second oxygen-enriched mixer is 21%-50%.

[0016] Preferably, the first oxygen-enriched mixer and the second oxygen-enriched mixer are provided with an annular air flow channel and a central oxygen flow channel. At the same time, the air outlet angle range at the tail end of the annular air flow channel is 0-25°, and the oxygen outlet angle at the tail end of the central oxygen flow channel is 0°.

[0017] A use method of a hazardous waste oxygen-enriched incineration device includes the following steps:

[0018] S1: Oxygen is generated by an oxygen generation device and is transported through a first oxygen transmission pipeline to a first oxygen-enriched mixer. At the same time, a primary fan sucks and transports air through a first air transmission pipeline to the first oxygen-enriched mixer. The first oxygen-enriched mixer mixes the oxygen and air to obtain air with high-concentration oxygen and introduces it into a rotary kiln to incinerate hazardous waste. The remaining residue after incineration reaches the slag discharge port at the bottom of the secondary combustion chamber through the tail of the rotary kiln and is discharged. The crude flue gas generated after incineration directly rises to the secondary combustion chamber;

[0019] S2: Oxygen generated by the oxygen generation device is transported through a second oxygen transmission pipeline to a second oxygen-enriched mixer. At the same time, a secondary fan sucks and transports air through a second air transmission pipeline to the second oxygen-enriched mixer. The second oxygen-enriched mixer mixes the oxygen and air to obtain air with high-concentration oxygen and introduces it into the secondary combustion chamber to mix with the combustible gas in the crude flue gas and perform high-temperature incineration in the secondary combustion chamber;

[0020] S3: The flue gas after incineration in the secondary combustion chamber successively passes through a denitrification system, a waste heat boiler, a quench tower, a dry acid scrubber, a bag filter, and an alkali scrubber, so that the flue gas after incineration is successively denitrified, waste heat utilized, quenched, dry acid removed, dust removed, and wet acid removed and purified. The flue gas after reaching the standard is then discharged outward through an induced draft fan and a chimney.

[0021] The beneficial effects are as follows: 1. The utility model applies the oxygen-enriched incineration technology to the incineration treatment of hazardous waste, which is clean and efficient, and at the same time has the significant advantages of high incineration efficiency and low pollutant emissions, effectively solving the problems such as large flue gas volume, generation of nitrogen oxides, high CO concentration, incomplete incineration, unstable operation, and large equipment investment in hazardous waste incineration, which is conducive to the sustainable development of the environmental governance industry in China;

[0022] 2. Oxygen is prepared by an oxygen generation device, and then the oxygen and air are mixed by means of connecting both the first oxygen transmission pipeline and the first air transmission pipeline to the first oxygen-enriched mixer to obtain air with high-concentration oxygen through the first oxygen-enriched mixer. Then, by introducing air with high-concentration oxygen into the rotary kiln, the direct air supply method is replaced, reducing the large proportion of nitrogen content in the air, ensuring the oxygen supply during the incineration of hazardous waste, being conducive to reducing the flue gas volume, and then the selection of the subsequent flue gas purification equipment can also be reduced, thereby reducing the project equipment investment. At the same time, since no auxiliary fuel needs to be added, the ignition conditions are also improved, and the incineration stability is increased;

[0023] 3. The second oxygen-enriched mixer is connected to both the second oxygen supply pipeline and the second gas supply pipeline. By this means, oxygen and air are mixed by the second oxygen-enriched mixer to obtain air with a high oxygen concentration. Then, instead of directly supplying air, air with a high oxygen concentration is introduced into the secondary combustion chamber, reducing the large proportion of nitrogen in the air, ensuring the oxygen supply during the incineration of hazardous waste, further facilitating the reduction of flue gas volume. At the same time, dust burns sufficiently, residue burns thoroughly, reducing the generation amount of secondary hazardous waste. Dioxin and combustible gas CO burn efficiently, reducing the generation of nitrogen oxides.

[0024] 4. The oxygen concentration range of the air mixed by the first oxygen-enriched mixer and the second oxygen-enriched mixer can be controlled within 21% - 50%. The selectable range is large, enhancing the flexibility of use of the first oxygen-enriched mixer and the second oxygen-enriched mixer. At the same time, since the first oxygen-enriched mixer and the second oxygen-enriched mixer can precisely control the oxygen concentration, the amount of excess oxygen air is reduced, ensuring more stable incineration control.

[0025] 5. The first oxygen-enriched mixer and the second oxygen-enriched mixer are provided with an annular air flow channel and a central oxygen flow channel. At the same time, the air outlet angle range at the end of the annular air flow channel is 0 - 25°, and the oxygen outlet angle at the end of the central oxygen flow channel is 0°. In this way, the first oxygen-enriched mixer and the second oxygen-enriched mixer can be used to mix oxygen and air in layers and in proportion, which is beneficial to improving the incineration efficiency. Brief Description of the Drawings

[0026] In order to more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the following will briefly introduce the drawings required for use in the description of the embodiments or the prior art. Obviously, the drawings in the following description are only some embodiments of the present invention. For those of ordinary skill in the art, without creative efforts, other drawings can also be obtained based on these drawings.

[0027] Figure 1 is the overall composition schematic diagram of the present invention;

[0028] Figure 2 is the present invention Figure 1 structural schematic diagram of the first oxygen-enriched mixer and the second oxygen-enriched mixer.

[0029] The description of the reference numerals is as follows:

[0030] 1. Second oxygen-rich mixer; 2. Second gas transmission pipeline; 201. Secondary air blower; 3. Rotary kiln; 301. Feed inlet; 302. Observation port; 303. Furnace drying burner port; 4. Oxygen generation equipment; 401. Second oxygen transmission pipeline; 402. Buffer tank; 403. First oxygen transmission pipeline; 5. Primary air blower; 501. First gas transmission pipeline; 6. First oxygen-rich mixer; 7. Secondary combustion chamber; 701. Slag discharge port; 702. Gas outlet; 8. Waste heat boiler; 9. Quenching tower; 10. Dry deacidification tower; 11. Bag filter; 12. Alkali washing tower; 13. Exhaust fan; 14. Chimney; 15. Denitration system; 16. Annular air flow channel; 17. Central oxygen flow channel. Detailed implementation mode

[0031] To make the objectives, technical solutions and advantages of the present utility model clearer, the technical solutions of the present utility model will be described in detail below. Apparently, the described embodiments are only a part of the embodiments of the present utility model, rather than all of them. Based on the embodiments of the present utility model, all other implementation manners obtained by those of ordinary skill in the art without creative efforts fall within the scope protected by the present utility model.

[0032] Embodiment 1:

[0033] Refer to Figure 1 - Figure 2As shown in the figure, the utility model provides a hazardous waste oxy-fuel incineration device, which includes a rotary kiln 3, a secondary combustion chamber 7 and an oxygen production device 4. A feed inlet 301 is arranged at one side of the rotary kiln 3. A first oxygen-enriched mixer 6 is fixedly arranged inside the rotary kiln 3 near the feed inlet 301. The other side of the rotary kiln 3 is fixedly connected to the secondary combustion chamber 7, and a second oxygen-enriched mixer 1 is installed in the middle of the secondary combustion chamber 7. The first oxygen-enriched mixer 6 is respectively connected to a first oxygen pipeline 403 for inputting oxygen and a first air pipeline 501 for inputting air, and the first oxygen pipeline 403 is connected to the oxygen production device 4. Thus, the first oxygen-enriched mixer 6 is used to mix oxygen and air to obtain air with high-concentration oxygen and introduce it into the rotary kiln 3. The second oxygen-enriched mixer 1 is respectively connected to a second oxygen pipeline 401 for inputting oxygen and a second air pipeline 2 for inputting air, and the second oxygen pipeline 401 is connected to the oxygen production device 4. Thus, the second oxygen-enriched mixer 1 is used to mix oxygen and air to obtain air with high-concentration oxygen and introduce it into the secondary combustion chamber 7. The purpose of this setting is that, firstly, the first oxygen pipeline 403 and the first air pipeline 501 are both connected to the first oxygen-enriched mixer 6 to mix oxygen and air through the first oxygen-enriched mixer 6 to obtain air with high-concentration oxygen, and then the air supply method of directly introducing air is replaced by introducing air with high-concentration oxygen into the rotary kiln 3, reducing the large proportion of nitrogen content in the air, ensuring the oxygen supply during the incineration of hazardous waste. At the same time, the second oxygen pipeline 401 and the second air pipeline 2 are both connected to the second oxygen-enriched mixer 1 to mix oxygen and air through the second oxygen-enriched mixer 1 to obtain air with high-concentration oxygen, and then the air supply method of directly introducing air is replaced by introducing air with high-concentration oxygen into the secondary combustion chamber 7, reducing the large proportion of nitrogen content in the air, ensuring the oxygen supply during the incineration of hazardous waste, and further facilitating the reduction of flue gas volume.

[0034] See Figure 1As shown, more specifically for the first oxygen-enriched mixer 6 and the second oxygen-enriched mixer 1, optionally, the oxygen concentration range of the first oxygen-enriched mixer 6 and the second oxygen-enriched mixer 1 is 21% - 50%. The advantage of this setting is that, firstly, there is a larger selection range when inputting oxygen-enriched air into the rotary kiln 3 and the secondary combustion chamber 7, which improves the flexibility of use of the first oxygen-enriched mixer 6 and the second oxygen-enriched mixer 1. At the same time, since the first oxygen-enriched mixer 6 and the second oxygen-enriched mixer 1 can precisely control the oxygen concentration, the amount of excess oxygen air is reduced. More specifically, the first oxygen-enriched mixer 6 and the second oxygen-enriched mixer 1 are provided with an annular air flow channel 16 and a central oxygen flow channel 17. At the same time, the air outlet angle range at the end of the annular air flow channel 16 is 0 - 25°, and the oxygen outlet angle at the end of the central oxygen flow channel 17 is 0°. The function of this setting is to be able to mix oxygen and air in layers and in proportion by means of the self-structure of the first oxygen-enriched mixer 6 and the second oxygen-enriched mixer 1.

[0035] See Figure 1 As shown, the following optimizations are respectively carried out on the oxygen production equipment 4, the rotary kiln 3 and the secondary combustion chamber 7. Specifically for the oxygen production equipment 4, the oxygen production equipment 4 is connected with a buffer tank 402 through pipelines, and the first oxygen pipeline 403 and the second oxygen pipeline 401 are respectively connected with the oxygen production equipment 4 through the buffer tank 402. The outer ends of the first air pipeline 501 and the second air pipeline 2 are respectively connected with a primary fan 5 and a secondary fan 201 for air supply, so as to buffer and temporarily store the oxygen produced by the oxygen production equipment 4 by means of the buffer tank 402, ensuring that the first oxygen pipeline 403 and the second oxygen pipeline 401 can be supplied with gas more stably. And specifically for the rotary kiln 3 and the secondary combustion chamber 7, an observation port 302 and a furnace drying burner port 303 are provided at the position between the feed inlet 301 and the first oxygen-enriched mixer 6 on the side of the rotary kiln 3. An air outlet 702 and a slag discharge port 701 are respectively provided at the top and bottom of the secondary combustion chamber 7. In this way, it is convenient to observe the incineration situation of the rotary kiln 3 through the observation port 302, and at the same time, it is convenient to install and use the burner smoothly in the rotary kiln 3 through the furnace drying burner port 303. Moreover, through the settings of the air outlet 702 and the slag discharge port 701, the flue gas after secondary combustion in the secondary combustion chamber 7 can be discharged upward and the waste slag generated by incineration can be discharged downward respectively.

[0036] See Figure 1As shown, further, specifically when the flue gas discharged from the secondary combustion chamber 7 is subjected to subsequent purification treatment, optionally, the gas outlet 702 of the secondary combustion chamber 7 is connected to the waste heat boiler 8 through a pipeline, and the pipeline between the gas outlet 702 and the waste heat boiler 8 is connected to a denitrification system 15 for denitrifying the discharged flue gas, the waste heat boiler 8 is connected to a quenching tower 9 through a pipeline, and the quenching tower 9 is connected to a dry deacidification tower 10 through a pipeline, and the dry deacidification tower 15 is connected to the waste heat boiler 8 through a pipeline. 0 is connected to a bag filter 11 through a pipeline, and the bag filter 11 is connected to an alkali washing tower 12 through a pipeline, the alkali washing tower 12 is connected to an exhaust fan 13 through a pipeline, and the exhaust fan 13 is connected to a chimney 14 through a pipeline. This arrangement facilitates the flue gas after incineration to be purified in sequence through denitrification, waste heat utilization, rapid cooling, dry deacidification, dust removal and wet deacidification, and the flue gas that meets the purification standards is then discharged to the outside through the exhaust fan 13 and the chimney 14.

[0037] See also Figure 1 - Figure 2 As shown, when applying the above-mentioned hazardous waste oxygen-enriched incineration device, its specific method of use includes the following steps:

[0038] S1: Oxygen is generated by the oxygen production equipment 4 and transported to the first oxygen-enriched mixer 6 via the first oxygen supply pipeline 403. At the same time, the primary fan 5 sucks and transports air to the first oxygen-enriched mixer 6 via the first air supply pipeline 501. The first oxygen-enriched mixer 6 mixes the oxygen with air to obtain air with a high oxygen concentration, which is then passed into the rotary kiln 3 to incinerate the hazardous waste. The remaining residue from the incineration is discharged from the slag discharge port 701 at the bottom of the secondary combustion chamber 7 through the tail of the rotary kiln 3. The crude flue gas generated after the incineration rises directly into the secondary combustion chamber 7.

[0039] S2: The oxygen generated by the oxygen production equipment 4 is transported to the second oxygen-enriched mixer 1 via the second oxygen supply pipeline 401. At the same time, the secondary fan 201 sucks and delivers air to the second oxygen-enriched mixer 1 via the second air supply pipeline 2. The second oxygen-enriched mixer 1 mixes the oxygen with the air to obtain air with a high oxygen concentration, which is then introduced into the secondary combustion chamber 7 to mix with the combustible gas in the raw flue gas and is burned at high temperature in the secondary combustion chamber 7.

[0040] S3: The flue gas after incineration in the secondary combustion chamber 7 passes through the denitrification system 15, the waste heat boiler 8, the quenching tower 9, the dry deacidification tower 10, the bag dust collector 11 and the alkali washing tower 12 in sequence, so that the flue gas after incineration is purified in sequence by denitrification, waste heat utilization, quenching, dry deacidification, dust removal and wet deacidification. The flue gas that meets the purification standards is then discharged to the outside through the exhaust fan 13 and the chimney 14.

[0041] When the above structure is specifically used for actual operation verification, oxygen with a purity of 99% is produced by the oxygen production equipment 4, stored in the buffer tank 402, and then transported to the first oxygen-enriched mixer 6 through the first oxygen pipeline 403. At the same time, the primary fan 5 sucks and transports air to the first oxygen-enriched mixer 6 through the first air pipeline 501. Thus, the oxygen and air are mixed by the first oxygen-enriched mixer 6 to obtain air with an oxygen concentration of 30% and input it into the rotary kiln 3. The oxygen is transported to the second oxygen-enriched mixer 1 through the second oxygen pipeline 401. At the same time, the secondary fan 201 sucks and transports air to the second oxygen-enriched mixer 1 through the second air pipeline 2. Thus, the oxygen and air are mixed by the second oxygen-enriched mixer 1 to obtain air with an oxygen concentration of 30% and input it into the secondary combustion chamber 7.

[0042] Then, the hazardous waste is first incinerated in the rotary kiln 3 at an incineration temperature of 850 - 950°C. The incineration residue is discharged through the slag discharge port 701. The crude gas enters the secondary combustion chamber 7 for secondary high-temperature incineration. H2, CO, dust, dioxins, etc. in the crude gas are mixed with 30% oxygen and incinerated at 1100°C. The generated flue gas is denitrified by the denitrification system 15 and then enters and exits the waste heat boiler 8, the quench tower 9, the dry acid scrubber 10, the bag filter 11, the caustic scrubber 12, the exhaust fan 13, and the chimney 14 in sequence. After denitrification, quenching, dry acid removal, dust removal, and wet acid removal purification, it meets the discharge standards. Other process parameters remain unchanged and are compared with the data of the original air incineration. The inspection of the heat loss rate of the incineration residue and the online inspection data of the flue gas show that the heat loss rate of the incineration residue has dropped from the original 6% to 3%; CO has dropped from 70 mg / m3 to 45 mg / m3; dust has dropped from 25 mg / m3 to 18 mg / m3; nitrogen oxides (NOX) have dropped from 220 mg / m3 to 110 mg / m3; dioxins have dropped from 0.1 ng TEQ / m3 to 0.05 ng TEQ / m3. The flue gas volume has dropped from 23000 m3 to 18000 m3, and the power consumption of the exhaust fan 13 has decreased by 20%.

[0043] Example 2:

[0044] See Figure 1 - Figure 2As shown in the figure, when the above structure is specifically applied to actual operation verification, oxygen with a purity of 99% is produced by the oxygen production equipment 4, stored in the buffer tank 402, and then transported to the first oxygen-enriched mixer 6 through the first oxygen delivery pipeline 403. At the same time, the primary air blower 5 sucks and transports air to the first oxygen-enriched mixer 6 through the first air delivery pipeline 501. In this way, the oxygen and air are mixed by the first oxygen-enriched mixer 6 to obtain air with an oxygen concentration of 45% and input it into the rotary kiln 3. The oxygen is transported to the second oxygen-enriched mixer 1 through the second oxygen delivery pipeline 401. At the same time, the secondary air blower 201 sucks and transports air to the second oxygen-enriched mixer 1 through the second air delivery pipeline 2. In this way, the oxygen and air are mixed by the second oxygen-enriched mixer 1 to obtain air with an oxygen concentration of 45% and input it into the secondary combustion chamber 7.

[0045] Then, the hazardous waste is first incinerated in the rotary kiln 3 at an incineration temperature of 850 - 950°C. The incineration residue is discharged through the slag discharge port 701. The crude gas enters the secondary combustion chamber 7 for secondary high-temperature incineration. The H2, CO, dust, dioxins, etc. in the crude gas are mixed with 30% concentration of oxygen and incinerated at 1100°C. The generated flue gas is denitrified by the denitrification system 15 and then enters the waste heat boiler 8, the quench tower 9, the dry deacidification tower 10, the bag filter 11, the alkali wash tower 12, the exhaust fan 13, and the chimney 14 in sequence. After denitrification, quenching, dry deacidification, dust removal, and wet deacidification purification, it meets the discharge standards. Other process parameters remain unchanged and are compared with the original data of air incineration. The inspection data of the thermal burnout rate of the incineration residue and the online inspection of the flue gas show that the thermal burnout rate of the incineration residue has dropped from 6% to 1%; CO has dropped from 70 mg / m3 to 25 mg / m3; dust has dropped from 25 mg / m3 to 9 mg / m3; nitrogen oxides (NOX) have dropped from 220 mg / m3 to 80 mg / m3; dioxins have dropped from 0.1 ng TEQ / m3 to 0.01 ng TEQ / m3. The flue gas volume has dropped from 23000 m3 to 15000 m3. The power consumption of the exhaust fan 13 has been reduced by 35%.

[0046] From the practical applications of the above-mentioned First Embodiment and Second Embodiment, it can be seen that through the oxygen-enriched incineration technology that increases the oxygen content, a large proportion of nitrogen (N2) in the air is reduced, and high-concentration oxygen (O2) is used to replace pure air, which can reduce the flue gas volume. At the same time, no auxiliary fuel needs to be added, which improves the ignition conditions, increases the incineration temperature, and enhances the incineration stability. The dust burns more fully, the residue burns more thoroughly, reducing the generation amount of secondary hazardous waste. Dioxins and combustible gas CO burn more efficiently, and the generated nitrogen oxides are also greatly reduced. At the same time, the power consumption is saved by about 35%, reducing carbon dioxide emissions. Due to the reduction of the flue gas volume, the selection of the subsequent flue gas purification equipment can also be downsized, thereby reducing the project equipment investment, effectively solving the problems of large flue gas volume in hazardous waste incineration, generation of nitrogen oxides, high CO concentration, incomplete incineration, unstable operation, and large equipment investment. Due to the precise control of the oxygen concentration, the amount of excess air is reduced, and the control is more stable.

[0047] The above is only the specific implementation manner of the present utility model, but the protection scope of the present utility model is not limited thereto. Any person skilled in the art within the technical scope disclosed by the present utility model can easily think of changes or substitutions, which should all be covered within the protection scope of the present utility model. Therefore, the protection scope of the present utility model shall be subject to the protection scope of the claims.

Claims

1. A hazardous waste oxygen-enriched incineration device, comprising a rotary kiln (3), a secondary combustion chamber (7) and an oxygen production device (4), characterized in that: A feed port (301) is provided on one side of the rotary kiln (3); a first oxygen-enriched mixer (6) is fixedly provided inside the rotary kiln (3) at a position close to the feed port (301); the second combustion chamber (7) is fixedly connected to the other side of the rotary kiln (3); and a second oxygen-enriched mixer (1) is installed in the middle of the second combustion chamber (7); The first oxygen-enriched mixer (6) is connected to a first oxygen supply pipeline (403) for inputting oxygen and a first air supply pipeline (501) for inputting air, and the first oxygen supply pipeline (403) is connected to the oxygen production equipment (4), so that oxygen and air are mixed by means of the first oxygen-enriched mixer (6) to obtain air with a high oxygen concentration and pass it into the rotary kiln (3); The second oxygen-enriched mixer (1) is connected to a second oxygen supply pipeline (401) for inputting oxygen and a second gas supply pipeline (2) for inputting gas, and the second oxygen supply pipeline (401) is connected to the oxygen production equipment (4), so that oxygen and air are mixed with the help of the second oxygen-enriched mixer (1) to obtain air with a high oxygen concentration and pass it into the secondary combustion chamber (7).

2. The hazardous waste oxygen-enriched incineration device according to claim 1, characterized in that: The oxygen production equipment (4) is connected to a buffer tank (402) through a pipeline, and the first oxygen supply pipeline (403) and the second oxygen supply pipeline (401) are respectively connected to the oxygen production equipment (4) via the buffer tank (402), and the outer ends of the first gas supply pipeline (501) and the second gas supply pipeline (2) are respectively connected to a primary fan (5) and a secondary fan (201) for induced air supply.

3. The hazardous waste oxygen-enriched incineration device according to claim 1, characterized in that: An observation port (302) and a kiln burner port (303) are provided on the side of the rotary kiln (3) between the feed port (301) and the first oxygen-enriched mixer (6), and an air outlet (702) and a slag discharge port (701) are provided at the top and bottom of the secondary combustion chamber (7), respectively.

4. The hazardous waste oxygen-enriched incineration device according to claim 3, characterized in that: The gas outlet (702) of the secondary combustion chamber (7) is connected to a waste heat boiler (8) via a pipeline, and the pipeline between the gas outlet (702) and the waste heat boiler (8) is connected to a denitrification system (15) for denitrifying the exhaust flue gas.

5. The hazardous waste oxygen-enriched incineration device according to claim 4, characterized in that: The waste heat boiler (8) is connected to a quenching tower (9) via a pipeline, and the quenching tower (9) is connected to a dry deacidification tower (10) via a pipeline.

6. The hazardous waste oxygen-enriched incineration device according to claim 5, characterized in that: The dry deacidification tower (10) is connected to a bag dust collector (11) via a pipeline, and the bag dust collector (11) is connected to an alkali washing tower (12) via a pipeline.

7. The hazardous waste oxygen-enriched incineration device according to claim 6, characterized in that: The alkali washing tower (12) is connected to an exhaust fan (13) through a pipeline, and the exhaust fan (13) is connected to a chimney (14) through a pipeline.

8. The hazardous waste oxygen-enriched incineration device according to any one of claims 1 to 7, characterized in that: The oxygen concentration of the first oxygen-enriched mixer (6) and the second oxygen-enriched mixer (1) ranges from 21% to 50%.

9. The hazardous waste oxygen-enriched incineration device according to claim 8, characterized in that: The first oxygen-enriched mixer (6) and the second oxygen-enriched mixer (1) are provided with an annular air flow channel (16) and a central oxygen flow channel (17). The air outlet angle at the tail end of the annular air flow channel (16) is in the range of 0-25 degrees, and the oxygen outlet angle at the tail end of the central oxygen flow channel (17) is 0 degrees.

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