Waste liquid and waste gas incinerator combustion air distribution system and air distribution method

Abstract

The invention belongs to the technical field of incinerators, and particularly relates to a combustion air distribution system and method of a waste liquid and waste gas incinerator. Comprising an incinerator, an SNCR denitration device and a heat distribution box, and air inlet bins and air outlet bins which are alternately arranged are arranged in the heat distribution box; a pipe network is arranged in the steam generating device, and is respectively connected with the upper, middle and lower air inlet bins and air outlet bins of the heat distribution box through closed loops; a top air outlet of the steam generating device is sequentially connected with a steam turbine and an SOEC device, an outlet of the SOEC device is connected with a hydrogen temporary storage tank and an oxygen temporary storage tank, and an outlet of the hydrogen temporary storage tank and an outlet of the oxygen temporary storage tank are connected with the incinerator. According to the air distribution system, the treatment efficiency is remarkably improved, pollutant emission is reduced, meanwhile, efficient utilization of energy is achieved through the heat energy recovery system, stable operation of the whole device is guaranteed through intelligent control, steam is converted into clean energy hydrogen and oxygen, and the resource utilization rate is increased.

Description

Technical Field

[0001] The invention belongs to the technical field of incinerators, and in particular relates to a combustion air distribution system and an air distribution method of a waste liquid and waste gas incinerator. Background Art

[0002] In the process of industrial production, a large amount of waste liquid and waste gas will be generated, which contain a variety of harmful substances, such as waste hydrocyanic acid, ammonium sulfate waste water, waste gas containing hydrocyanic acid and waste hydrogen. If these waste liquids and waste gases are directly discharged without proper treatment, they will cause serious harm to the environment and human health. Therefore, how to efficiently and environmentally friendly treat these waste liquids and waste gases has become a problem that needs to be solved urgently.

[0003] Most traditional methods of treating waste liquid and waste gas have problems such as low treatment efficiency, high energy consumption, and serious secondary pollution. For example, when treating waste liquid and waste gas, some incinerators have an unreasonable air distribution system, which leads to incomplete combustion and produces a large amount of black smoke and harmful gases; at the same time, the heat generated during the incineration process is not fully utilized, resulting in energy waste. In addition, traditional denitrification technology also has problems such as low denitrification efficiency and large ammonia escape, which further aggravates environmental pollution.

[0004] In view of the above problems, it is urgent to develop a new type of waste liquid and waste gas incinerator combustion air distribution system and air distribution method to improve the treatment efficiency of waste liquid and waste gas, reduce energy consumption and secondary pollution, and maximize the utilization of resources. Summary of the invention

[0005] In view of the shortcomings of the prior art, the purpose of the present invention is to provide a waste liquid and waste gas incinerator combustion air distribution system, which significantly improves the processing efficiency and reduces pollution emissions. At the same time, the heat recovery system is used to achieve efficient energy utilization, and the stable operation of the entire device is ensured through intelligent control. Steam is converted into clean energy hydrogen and oxygen, thereby improving resource utilization.

[0006] Another object of the present invention is to provide a combustion air distribution method for a waste liquid and waste gas incinerator.

[0007] The technical solution adopted by the present invention is as follows: The waste liquid and waste gas incinerator combustion air distribution system comprises an incinerator, an SNCR denitrification device and a heat distribution box connected in sequence, and the upper, middle and lower sections of the heat distribution box are provided with alternately arranged air inlet bins and air outlet bins; it also comprises a steam generating device, and the steam generating device is provided with upper, middle and lower sections of pipe networks, which are respectively connected to the upper, middle and lower air inlet bins and air outlet bins of the heat distribution box through a closed loop; wherein, the closed loop of the lower pipe network and the lower air inlet bin and the air outlet bin is also provided with a first water heating box and a second water heating box and a water heating tank arranged in parallel in sequence, the outlet of the lower air inlet bin is connected to the lower pipe network through a pipeline, the air outlet of the lower pipe network is connected to the inlet of the internal pipe network of the first water heating box and the second water heating box arranged in parallel, the outlet of the internal pipe network of the first water heating box and the second water heating box is connected to the internal pipe network of the water heating tank through a pipeline, the outlet of the internal pipe network of the water heating tank is connected to the lower air outlet bin through a pipeline, and the outlet of the lower air outlet bin is connected to an electrostatic precipitator and an SCR denitrification reactor in sequence through a pipeline; A steam injection device is provided at the bottom of the steam generating device, the outlet of the water heating tank is connected to the inlet of the first water heating tank and the inlet of the second water heating tank respectively, and the outlet of the first water heating tank and the second water heating tank are connected to the steam injection device respectively; The top gas outlet of the steam generating device is connected to a steam turbine through a pipeline, the steam turbine is connected to a SOEC device and a molecular sieve oxygen generating device respectively, the outlet of the SOEC device is connected to a hydrogen temporary storage tank, the outlet of the molecular sieve oxygen generating device is connected to an oxygen temporary storage tank, and the outlets of the hydrogen temporary storage tank and the oxygen temporary storage tank are connected to an incinerator through pipelines respectively.

[0008] The incinerator is also respectively connected with a natural gas pipeline, an organic waste liquid pipeline and an organic waste gas pipeline.

[0009] The SNCR denitration device is connected with an ammonia pipeline.

[0010] The incinerator and the SNCR denitration device are both provided with temperature monitoring devices, and the incinerator is also provided with an oxygen content monitoring device.

[0011] The waste liquid and waste gas incinerator combustion air distribution system also includes a spare hydrogen tank arranged in parallel with the hydrogen temporary storage tank, and a spare oxygen tank arranged in parallel with the oxygen temporary storage tank.

[0012] The gas temporary storage tank, the spare hydrogen tank, the oxygen temporary storage tank and the spare oxygen tank are respectively connected with vacuum pipelines.

[0013] The waste liquid and waste gas incinerator combustion air distribution method is realized based on the above-mentioned waste liquid and waste gas incinerator combustion air distribution system.

[0014] The waste liquid and waste gas incinerator combustion air distribution method comprises the following steps: Step 1: introducing natural gas, organic waste liquid and organic waste gas into an incinerator for combustion and oxidation reaction; Step 2: The waste gas generated after combustion then enters the SNCR denitrification section of the incinerator and is mixed with precisely measured ammonia water. The NO in the waste gas is removed by SNCR technology at a temperature range of 1050-1300°C. x Perform reduction removal; Step 3: The exhaust gas after SNCR denitrification treatment is introduced into the upper air inlet bin from the top inlet of the heat distribution box. The exhaust gas then enters the upper pipe network through the pipeline for heat exchange, then enters the upper air outlet bin, and continues to flow to the middle air inlet bin; Step 4: In the middle air inlet bin, the exhaust gas is heat exchanged again through the middle pipe network, and then enters the middle air outlet bin; thereafter, the exhaust gas enters the lower air inlet bin, and heat exchange is performed with the pipe networks in the first water heating box and the second water heating box through the lower pipe network; the water in the two water heating boxes transfers heat energy with the exhaust gas, and the exhaust gas continues to flow to the pipe network in the water heating tank, and further heat exchange is performed with the water in the water heating tank; Step 5: The exhaust gas that has completed the heat exchange returns to the lower air outlet bin of the heat distribution box, and then enters the electrostatic precipitator from the lower air outlet bin for dust removal. The exhaust gas after dust removal enters the SCR denitration reactor for further purification treatment; Step 6: The heated water in the water heating tank is introduced into the first water heating tank and the second water heating tank for further heating treatment. The two water heating tanks are operated in a standby mode, that is, one is in a water supply state and the other is in a heating state; Step 7: The water after heat exchange by the first water heating box or the second water heating box enters the bottom of the steam generating device and forms a scattered water flow through the steam injection device. The scattered water flow has a small amount of water. When it contacts the lower pipe network at 345-355°C, it will evaporate instantly to form wet steam. When the wet steam contacts the surface of the middle pipe network at 645-655°C, the wet steam will be further evaporated instantly to form dry steam. The dry steam continues to flow upward and performs the final heat exchange on the surface of the upper pipe network at 845-855°C to ensure that the output steam is dry steam. Step 8: After the dry steam enters the steam turbine, it drives the steam turbine to rotate. Under the power of the dry steam, the steam turbine drives the generator to generate electricity, and after the electric energy is stabilized and transformed, it is supplied to the SOEC device. Under the action of electric energy and thermal energy, the SOEC device decomposes the dry steam to generate hydrogen; Step 9: The generated hydrogen (mixed with oxygen) is pumped into a hydrogen temporary storage tank in a vacuum state, and a positive pressure state is maintained in the hydrogen temporary storage tank. Both the hydrogen temporary storage tank and the backup hydrogen tank operate in a backup mode; Step 10: The electric energy generated by the generator is simultaneously supplied to the molecular sieve oxygen generator, and the oxygen generated by the molecular sieve oxygen generator is stored in an oxygen temporary storage tank or a backup oxygen tank, and both the oxygen temporary storage tank and the backup oxygen tank are operated in a backup mode; Step 11: monitor the temperature in the incinerator and the SNCR denitration device in real time through the temperature monitoring device, and accurately adjust the intake volume of natural gas, organic waste liquid and organic waste gas through the control system to keep the temperature in the incinerator stable between 850-1050°C, and ensure that the temperature in the SNCR denitration device is within the range of 1050-3000°C; when it is detected that the temperature in the SNCR denitration device is lower than 1050°C, spray the oxygen in the oxygen temporary storage tank into the incinerator to increase the oxygen content of the combustion-supporting wind, thereby improving the combustion effect of natural gas and the heat release of combustion. After monitoring for 1 minute, if the temperature does not reach 1050°C, spray the hydrogen in the hydrogen temporary storage tank into the incinerator, and use the characteristic that hydrogen can be ignited at a very low temperature to add hydrogen to achieve a low-temperature deflagration heating effect, thereby initiating the combustion of the organic waste liquid and organic waste gas; The oxygen content in the incinerator is monitored in real time through the oxygen content monitoring device, and oxygen is added to the incinerator through the oxygen temporary storage tank when necessary to ensure that the oxygen content in the incinerator remains within the range of 6-10%.

[0015] The organic waste liquid includes waste hydrocyanic acid and ammonium sulfate waste water.

[0016] The organic waste gas includes waste gas containing hydrocyanic acid and waste hydrogen.

[0017] The control system adopts conventional PID control technology to realize the above-mentioned regulating function. This technology has been widely used in the field of automatic control and is not an innovation point of the present invention, so it will not be described in detail here.

[0018] Compared with the prior art, the present invention has the following beneficial effects: (1) The present invention optimizes the air distribution system to make the combustion in the incinerator more complete, reducing the generation of black smoke and harmful gases. At the same time, the use of SNCR and SCR denitrification technology effectively reduces the NO in the exhaust gas. x content, thus improving the treatment efficiency of waste liquid and waste gas; the waste gas is further purified by electrostatic precipitator and SCR denitration reactor, effectively removing particulate matter and harmful gases in the waste gas and reducing secondary pollution; (2) The present invention makes full use of the heat generated during the incineration process through a heat recovery system consisting of a steam generating device, a water heating box and a steam injection device, converts the heat energy in the exhaust gas into steam, which is then used for power generation and hydrogen production, thereby realizing the cascade utilization of energy and greatly reducing energy consumption; the SOEC device is used to decompose dry steam into hydrogen and oxygen, which can be used as clean energy and combustion aids, thereby maximizing the utilization of resources; (3) The present invention monitors the temperature and oxygen content in the incinerator and the SNCR denitrification device in real time through a temperature monitoring device and an oxygen content monitoring device, and accurately adjusts the air intake volume through a control system, thereby realizing intelligent control of the incineration process and improving the stability and reliability of the system. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] Figure 1 It is a structural schematic diagram of the combustion air distribution system of the waste liquid and waste gas incinerator of the present invention; Figure 2 It is a structural schematic diagram of the heat distribution box and the steam generating device of the present invention; Figure 3 It is a schematic diagram of the structure of the steam turbine, SOEC device, molecular sieve oxygen production device, hydrogen temporary storage tank and oxygen temporary storage tank of the present invention; In the figure: 1. Incinerator; 2. SNCR denitration device; 3. Heat distribution box; 4. Steam generating device; 5. First water heating box; 6. Second water heating box; 7. Water heating tank; 8. Electrostatic precipitator; 9. SCR denitration reactor; 10. Steam injection device; 11. Steam turbine; 12. SOEC device; 13. Hydrogen temporary storage tank; 14. Oxygen temporary storage tank; 15. Natural gas pipeline; 16. Organic waste liquid pipeline; 17. Organic waste gas pipeline; 18. Ammonia pipeline; 19. Temperature monitoring device; 20. Oxygen content monitoring device; 21. Spare hydrogen tank; 22. Spare oxygen tank; 23. Vacuum pipeline; 24. Molecular sieve oxygen production device. DETAILED DESCRIPTION

[0020] The present invention is further described below with reference to the embodiments, but they do not limit the implementation of the present invention.

[0021] The raw materials used in the examples are all conventional commercially available raw materials unless otherwise specified, and the process methods used in the examples are all conventional methods in the art unless otherwise specified.

[0022] Some of the raw materials used in the examples are described as follows: Waste hydrocyanic acid: from acrylonitrile unit, the main component is 98wt.% hydrocyanic acid; Ammonium sulfate wastewater: comes from the ammonium sulfate unit, and its main components are 30wt.% ammonium sulfate, 60wt.% water and 10wt.% polymer; Waste gas containing hydrocyanic acid: from dinitrile unit, the main components are 95vol% nitrogen and 5vol% hydrocyanic acid gas; Waste hydrogen: comes from the diamine unit, the main components are 50vol% hydrogen and 50vol% nitrogen.

[0023] Example 1 like Figure 1-3As shown, the waste liquid and waste gas incinerator combustion air distribution system comprises an incinerator 1, an SNCR denitrification device 2 and a heat distribution box 3 connected in sequence, and the upper, middle and lower sections of the heat distribution box 3 are provided with alternately arranged air inlet bins and air outlet bins; it also comprises a steam generating device 4, and the steam generating device 4 is provided with upper, middle and lower sections of pipe networks, which are respectively connected to the upper, middle and lower air inlet bins and air outlet bins of the heat distribution box 3 through a closed loop; wherein, the closed loop of the lower pipe network and the lower air inlet bin and air outlet bin is also provided with a first water heater arranged in parallel in sequence. The heat box 5 and the second water heating box 6 and the water heating tank 7, the outlet of the lower air inlet bin is connected to the lower pipe network through a pipeline, the air outlet of the lower pipe network is connected to the inlet of the internal pipe network of the first water heating box 5 and the second water heating box 6 arranged in parallel, the outlet of the internal pipe network of the first water heating box 5 and the second water heating box 6 is connected to the internal pipe network of the water heating tank 7 through a pipeline, the outlet of the internal pipe network of the water heating tank 7 is connected to the lower air outlet bin through a pipeline, and the outlet of the lower air outlet bin is sequentially connected to the electrostatic precipitator 8 and the SCR denitration reactor 9 through a pipeline; A steam injection device 10 is provided at the bottom of the steam generating device 4, and the outlet of the water heating tank 7 is connected to the inlet of the first water heating tank 5 and the second water heating tank 6 respectively, and the outlets of the first water heating tank 5 and the second water heating tank 6 are connected to the steam injection device 10 respectively; The top gas outlet of the steam generating device 4 is connected to the steam turbine 11 through a pipeline, and the steam turbine 11 is connected to the SOEC device 12 and the molecular sieve oxygen generating device 24 respectively. The outlet of the SOEC device 12 is connected to the hydrogen temporary storage tank 13, and the outlet of the molecular sieve oxygen generating device 24 is connected to the oxygen temporary storage tank 14. The outlets of the hydrogen temporary storage tank 13 and the oxygen temporary storage tank 14 are connected to the incinerator 1 through pipelines respectively.

[0024] The incinerator 1 is also connected to a natural gas pipeline 15, an organic waste liquid pipeline 16 and an organic waste gas pipeline 17 respectively.

[0025] The SNCR denitration device 2 is connected to an ammonia water pipeline 18 .

[0026] The incinerator 1 and the SNCR denitration device 2 are both provided with a temperature monitoring device 19 , and the incinerator 1 is also provided with an oxygen content monitoring device 20 .

[0027] The combustion air distribution system of the waste liquid and waste gas incinerator 1 also includes a spare hydrogen tank 21 arranged in parallel with the hydrogen temporary storage tank 13 , and a spare oxygen tank 22 arranged in parallel with the oxygen temporary storage tank 14 .

[0028] The hydrogen temporary storage tank 13, the backup hydrogen tank 21, the oxygen temporary storage tank 14 and the backup oxygen tank 22 are respectively connected with vacuum pipelines 23.

[0029] The combustion air distribution method of the waste liquid and waste gas incinerator comprises the following steps: Step 1: Introduce natural gas, organic waste liquid and organic waste gas into the incinerator 1, and preliminarily adjust the supply of natural gas, waste liquid and waste gas through the PID control system according to the preset combustion parameters; in the incinerator 1, the natural gas and waste liquid and waste gas are quickly mixed and ignited, and the temperature in the furnace quickly rises to 950±100℃. Under high temperature, the hydrocarbons in the waste liquid and waste gas are fully burned to generate harmless gases such as CO2 and H2O, while releasing a large amount of heat energy. In addition, some incompletely burned organic matter is further decomposed under the high temperature and sufficient oxygen conditions in the furnace to ensure combustion efficiency and emission quality; Step 2: The exhaust gas after combustion enters the SNCR denitrification device 2, and reacts with precisely measured ammonia water at a high temperature of 1200±100℃. The SNCR technology is used to remove NO in the exhaust gas. x Reducing to N2, effectively reducing nitrogen oxide emissions. In this step, the PID control system automatically adjusts the supply of ammonia water according to the real-time monitored temperature in the SNCR denitrification device 2 to ensure denitrification efficiency; Step 3: The exhaust gas after SNCR denitration treatment is introduced into the upper air inlet bin from the top inlet of the heat distribution box 3. The exhaust gas then enters the upper pipe network through the pipeline for heat exchange, then enters the upper air outlet bin, and continues to flow to the middle air inlet bin; Step 4: In the middle air inlet bin, the exhaust gas is heat exchanged again through the middle pipe network, and then enters the middle air outlet bin; thereafter, the exhaust gas enters the lower air inlet bin, and heat exchange is performed with the pipe networks in the first water heating box 5 and the second water heating box 6 through the lower pipe network; the water in the two water heating boxes transfers heat energy with the exhaust gas, and the exhaust gas continues to flow to the pipe network in the water heating tank 7, and further heat exchange is performed with the water in the water heating tank 7; Step 5: The exhaust gas that has completed the heat exchange returns to the lower air outlet bin of the heat distribution box 3, and then enters the electrostatic precipitator 8 from the lower air outlet bin for dust removal to remove particulate matter in the exhaust gas. Subsequently, the exhaust gas enters the SCR denitration reactor 9 for further purification to ensure the cleanliness of the exhaust gas; Step 6. The heated water in the water heating tank 7 is introduced into the first water heating tank 5 and the second water heating tank 6 for further heating treatment. The PID control system will automatically switch the working state of the first water heating tank 5 and the second water heating tank 6 according to the real-time monitored water temperature and exhaust gas temperature. When the water temperature in the first water heating tank 5 reaches the preset value, the PID control system will automatically close the water inlet valve of the first water heating tank 5 and open the water inlet valve of the second water heating tank 6 to heat the second water heating tank 6. When the water temperature in the second water heating tank 6 also reaches the preset value, the PID control system will automatically switch back to the first water heating tank 5 to work. This one-backup-one-use working mode ensures the reliability and continuity of the system. Step 7: The water after heat exchange by the first water heating box 5 or the second water heating box 6 enters the bottom of the steam generating device 4 and forms a scattered water flow through the steam injection device 10. The scattered water flow has a small amount of water. When it contacts the lower pipe network at 350±5°C, it will evaporate instantly to form wet steam. When the wet steam contacts the surface of the middle pipe network at 650±5°C, the wet steam will be further evaporated instantly to form dry steam. The dry steam continues to flow upward and performs the final heat exchange on the surface of the upper pipe network at 850±5°C to ensure that the output steam is dry steam. Step 8: After the dry steam enters the steam turbine 11, it drives the steam turbine 11 to rotate. Under the power of the dry steam, the steam turbine 11 drives the generator to generate electricity, and after the electric energy is stabilized and transformed, it is supplied to the SOEC device 12. Under the action of electric energy and thermal energy, the SOEC device 12 decomposes the dry steam to generate hydrogen; Step 9: The generated hydrogen (mixed with oxygen) is introduced into the hydrogen temporary storage tank 13 in a vacuum state, and the positive pressure state in the hydrogen temporary storage tank 13 is maintained. When the hydrogen temporary storage tank 13 reaches the storage upper limit, the PID control system automatically switches to the spare hydrogen tank 21 to ensure continuous and stable operation of the system; Step 10: The electric energy generated by the generator is simultaneously supplied to the molecular sieve oxygen generator 24; the oxygen generated by the molecular sieve oxygen generator 24 is stored in the oxygen temporary storage tank 14 or the backup oxygen tank 22; both the oxygen temporary storage tank 14 and the backup oxygen tank 22 are operated in the backup mode; the vacuum degree and storage volume of each gas temporary storage tank are monitored by the PID control system to ensure the gas quality and safety; Step 11: monitor the temperature in the incinerator (1) and the SNCR denitration device (2) in real time through the temperature monitoring device (19), and accurately adjust the intake amount of natural gas, organic waste liquid and organic waste gas through the control system to keep the temperature in the incinerator 1 stable between 850-1050°C, and ensure that the temperature in the SNCR denitration device 2 is within the range of 1050-3000°C; when it is detected that the temperature in the SNCR denitration device 2 is lower than 1050°C, spray the oxygen in the oxygen temporary storage tank into the incinerator 1 to increase the oxygen content of the combustion-supporting wind, thereby improving the combustion effect of the natural gas and the heat release of the combustion. After monitoring for 1 minute, if the temperature does not reach 1050°C, spray the hydrogen in the hydrogen temporary storage tank 13 into the incinerator. By utilizing the characteristic that hydrogen can be ignited at a very low temperature, hydrogen is added to achieve a low-temperature deflagration heating effect, thereby initiating the combustion of the organic waste liquid and the organic waste gas; The oxygen content in the incinerator 1 is monitored in real time by the oxygen content monitoring device 20. When the oxygen content is lower than 6%, oxygen is added to the incinerator 1 through the oxygen temporary storage tank 14 to ensure that the oxygen content in the incinerator 1 remains within the range of 6-10%.

[0030] The material after combustion contains 21 vol% water, 17 vol% oxygen, 60 vol% nitrogen, nitrogen oxides <1 vol%, sulfur dioxide less than 0.5 vol%, and others <0.5 vol%.

Claims

1. A combustion air distribution system for a waste liquid and waste gas incinerator, characterized in that: The invention comprises an incinerator (1), an SNCR denitration device (2) and a heat distribution box (3) which are connected in sequence, wherein the upper, middle and lower sections of the heat distribution box (3) are provided with air inlet bins and air outlet bins which are arranged alternately; and a steam generating device (4) is further provided with an upper, middle and lower section of a pipe network which is respectively connected to the upper, middle and lower air inlet bins and air outlet bins of the heat distribution box (3) through a closed loop; wherein a first water heating box (5) and a second water heating box (6) which are arranged in parallel are sequentially provided on the closed loop between the lower pipe network and the lower air inlet bin and air outlet bin. ) and a water heating tank (7), the outlet of the lower air inlet bin is connected to the lower pipe network through a pipeline, the air outlet of the lower pipe network is connected to the inlet of the internal pipe network of the first water heating box (5) and the second water heating box (6) arranged in parallel, the outlet of the internal pipe network of the first water heating box (5) and the second water heating box (6) is connected to the internal pipe network of the water heating tank (7) through a pipeline, the outlet of the internal pipe network of the water heating tank (7) is connected to the lower air outlet bin through a pipeline, and the outlet of the lower air outlet bin is connected to the electrostatic precipitator (8) and the SCR denitration reactor (9) in sequence through a pipeline; A steam injection device (10) is provided at the bottom of the steam generating device (4); the outlet of the water heating tank (7) is respectively connected to the inlets of the first water heating tank (5) and the second water heating tank (6); and the outlets of the first water heating tank (5) and the second water heating tank (6) are respectively connected to the steam injection device (10); The top gas outlet of the steam generating device (4) is connected to a steam turbine (11) via a pipeline. The steam turbine (11) is connected to a SOEC device (12) and a molecular sieve oxygen generating device (24) respectively. The outlet of the SOEC device (12) is connected to a hydrogen temporary storage tank (13). The outlet of the molecular sieve oxygen generating device (24) is connected to an oxygen temporary storage tank (14). The outlets of the hydrogen temporary storage tank (13) and the oxygen temporary storage tank (14) are connected to an incinerator (1) via pipelines respectively.

2. The waste liquid and waste gas incinerator combustion air distribution system according to claim 1, characterized in that: The incinerator (1) is also respectively connected to a natural gas pipeline (15), an organic waste liquid pipeline (16) and an organic waste gas pipeline (17).

3. The waste liquid and waste gas incinerator combustion air distribution system according to claim 1, characterized in that: The SNCR denitrification device (2) is connected to an ammonia water pipeline (18).

4. The combustion air distribution system for the waste liquid and waste gas incinerator according to claim 1 is characterized in that: The incinerator (1) and the SNCR denitration device (2) are both provided with a temperature monitoring device (19), and the incinerator (1) is also provided with an oxygen content monitoring device (20).

5. The combustion air distribution system for the waste liquid and waste gas incinerator according to claim 1 is characterized in that: It also includes a spare hydrogen tank (21) arranged in parallel with the hydrogen temporary storage tank (13), and a spare oxygen tank (22) arranged in parallel with the oxygen temporary storage tank (14).

6. The combustion air distribution system for the waste liquid and waste gas incinerator according to claim 5 is characterized in that: The hydrogen temporary storage tank (13), the backup hydrogen tank (21), the oxygen temporary storage tank (14) and the backup oxygen tank (22) are respectively connected to vacuum pipelines (23).

7. A method for distributing air for combustion of waste liquid and waste gas incinerator, characterized in that: It uses the waste liquid and waste gas incinerator combustion air distribution system described in any one of claims 1-6.

8. The method for combustion air distribution of a waste liquid and waste gas incinerator according to claim 7, characterized in that: The following steps are involved: Step 1: introducing natural gas, organic waste liquid and organic waste gas into an incinerator (1) to carry out a combustion oxidation reaction; Step 2: The waste gas generated after combustion then enters the SNCR denitrification section of the incinerator (1) and is mixed with precisely measured ammonia water. The NO in the waste gas is removed by SNCR technology at a temperature range of 1050-1300°C. x Perform reduction removal; Step 3: The exhaust gas after SNCR denitration treatment is introduced into the upper air inlet bin from the top inlet of the heat distribution box (3), and then enters the upper pipe network through the pipeline for heat exchange, and then enters the upper air outlet bin, and continues to flow to the middle air inlet bin; Step 4: In the middle air inlet bin, the exhaust gas is again heat exchanged through the middle pipe network, and then enters the middle air outlet bin; thereafter, the exhaust gas enters the lower air inlet bin, and is heat exchanged with the pipe networks in the first water heating box (5) and the second water heating box (6) through the lower pipe network; the water in the two water heating boxes transfers heat energy with the exhaust gas, and the exhaust gas continues to flow to the pipe network in the water heating tank (7), and is further heat exchanged with the water in the water heating tank (7); Step 5: The exhaust gas that has completed the heat exchange returns to the lower air outlet bin of the heat distribution box (3), and then enters the electrostatic precipitator (8) from the lower air outlet bin for dust removal. The exhaust gas after dust removal enters the SCR denitration reactor (9) for further purification. Step 6: The heated water in the water heating tank (7) is introduced into the first water heating tank (5) and the second water heating tank (6) for further heating treatment. The two water heating tanks are operated in a standby mode, that is, one is in a water supply state and the other is in a heating state; Step 7: The water after heat exchange in the first water heating box (5) or the second water heating box (6) enters the bottom of the steam generating device (4) and forms a scattered water flow through the steam injection device (10). The scattered water flow evaporates instantly to form wet steam when it contacts the lower pipe network at 345-355°C. The wet steam further evaporates instantly to form dry steam when it contacts the surface of the middle pipe network at 645-655°C. The dry steam continues to flow upward and undergoes final heat exchange on the surface of the upper pipe network at 845-855°C, thereby ensuring that the output steam is dry steam. Step 8, the dry steam enters the steam turbine (11) and drives the steam turbine (11) to rotate. The steam turbine (11) drives the generator to generate electricity under the power of the dry steam, and supplies the electricity to the SOEC device (12) after voltage stabilization and voltage transformation. The SOEC device (12) decomposes the dry steam to generate hydrogen under the action of electrical energy and thermal energy; Step 9: The generated hydrogen is pumped into a hydrogen temporary storage tank (13) in a vacuum state, and a positive pressure state is maintained in the hydrogen temporary storage tank (13). Both the hydrogen temporary storage tank (13) and the backup hydrogen tank (21) operate in a backup mode; Step 10: The electric energy generated by the generator is simultaneously supplied to the molecular sieve oxygen generator (24); the oxygen generated by the molecular sieve oxygen generator (24) is stored in the oxygen temporary storage tank (14) or the backup oxygen tank (22); both the oxygen temporary storage tank (14) and the backup oxygen tank (22) are operated in a backup mode; Step 11: monitor the temperature in the incinerator (1) and the SNCR denitration device (2) in real time through the temperature monitoring device (19), and accurately adjust the intake amount of natural gas, organic waste liquid and organic waste gas through the control system to keep the temperature in the incinerator (1) stable between 850-1050°C, and ensure that the temperature in the SNCR denitration device (2) is within the range of 1050-3000°C; when it is detected that the temperature in the SNCR denitration device (2) is lower than 1050°C, inject oxygen in the oxygen temporary storage tank into the incinerator (1) to increase the oxygen content of the combustion-supporting wind, thereby improving the combustion effect of the natural gas and increasing the heat release of combustion. After monitoring for 1 minute, if the temperature does not reach 1050°C, inject hydrogen in the hydrogen temporary storage tank (13) into the incinerator to achieve a low-temperature deflagration heating effect; The oxygen content in the incinerator (1) is monitored in real time by an oxygen content monitoring device (20), and oxygen is added to the incinerator (1) through an oxygen temporary storage tank (14) to ensure that the oxygen content in the incinerator (1) is maintained within a range of 6-10%.

9. The method for combustion air distribution of a waste liquid and waste gas incinerator according to claim 8, characterized in that: The organic waste liquid includes waste hydrocyanic acid and ammonium sulfate waste water.

10. The method for combustion air distribution of a waste liquid and waste gas incinerator according to claim 8, characterized in that: The organic waste gas includes waste gas containing hydrocyanic acid and waste hydrogen.

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