Super-enthalpy combustion organic waste gas treatment equipment based on hierarchical porous medium heat accumulator

Abstract

The application discloses a super-enthalpy combustion organic waste gas treatment equipment based on a hierarchical porous medium heat accumulator and relates to the technical field of organic waste gas combustion treatment. The equipment comprises an air inlet mixing unit, a reaction cylinder, a hierarchical porous medium heat accumulator, a temperature detection unit and a controller. The heat accumulator comprises, in sequence along the airflow direction, an explosion suppression fireproof layer, a preheating migration layer, a reaction positioning layer and a heat storage burnout layer. The reaction positioning layer forms a pore diameter sudden increase interface and a pore diameter retraction interface on the two sides respectively, and a target reaction zone is defined between the two interfaces. Three thermocouples are arranged upstream of the pore diameter sudden increase interface, in the target reaction zone and downstream of the pore diameter retraction interface respectively. The controller adjusts the organic waste gas flow and the combustion air amount according to the boundary temperature difference formed by the temperature in the zone and the upstream and downstream temperatures, maintains the reaction zone in the target reaction zone, and thus reduces the risk of backfire, deflagration and incomplete oxidation.

Description

Technical Field

[0001] This invention relates to the field of organic waste gas combustion treatment technology, and in particular to an ultraenthalpic combustion organic waste gas treatment device based on a graded porous media heat storage body. Background Technology

[0002] Volatile organic compounds (VOCs) in waste gas typically originate from production processes such as coating, printing, painting, electronic chemicals, resin processing, pharmaceutical chemicals, and precision cleaning. For organic waste gases containing certain combustible components, common treatment methods include catalytic combustion, regenerative thermal oxidation, direct combustion, and porous media combustion. Among these, porous media combustion utilizes a solid framework for heat storage and radiative heat exchange, preheating the combustible mixture entering the reaction zone. This allows for maintaining a higher combustion temperature even under low-calorific-value or low-concentration waste gas conditions, thus demonstrating its application value in low-concentration organic waste gas treatment scenarios.

[0003] Existing porous media combustion equipment typically fills the combustion chamber with porous media such as ceramic honeycomb, foam ceramics, ceramic particles, or metal foam. The mixture of organic waste gas and combustion air passes through the porous media, where preheating, combustion, and heat storage processes are completed. To improve combustion stability, some equipment divides the porous media into preheating, combustion, and heat storage zones, or sets porous media layers with different pore sizes and porosities along the airflow direction. This type of structure can achieve good heat recovery and combustion maintenance in waste gas treatment scenarios with stable concentrations and airflow rates.

[0004] However, in actual organic waste gas treatment processes, waste gas concentration and air volume often fluctuate due to changes in production cycle, exhaust valve opening and closing, number of workstations, and solvent evaporation intensity. When the concentration of organic waste gas entering the porous media combustion equipment increases or the air volume decreases, the exothermic intensity inside the porous media increases, and the reaction zone is prone to shifting back towards the inlet end. When the reaction zone is too close to the inlet end, the mixed gas near the inlet end may be prematurely heated to a dangerous temperature, leading to a risk of backfire or deflagration. Conversely, when the concentration of organic waste gas decreases or the air volume increases, the exothermic intensity inside the porous media decreases, and the reaction zone may shift downstream, resulting in insufficient preheating or residence time, leading to incomplete oxidation of the organic waste gas.

[0005] While existing technologies can maintain equipment operation by detecting combustion temperature and adjusting the treatment air volume or combustion air volume, the pore structure and the controlled object are usually independent of each other: the layered porous media only passively affect the position of the reaction zone, and the controller uses single-point temperature or outlet temperature as feedback, with the temperature measurement location not corresponding to the pore size change boundary between adjacent porous media layers. Therefore, the controller cannot distinguish between the return state of the reaction zone crossing the upstream boundary and the offset state crossing the downstream boundary, nor can it implement adjustment actions to bring the reaction zone back in both directions separately. When the concentration or air volume of organic waste gas fluctuates, even if the overall temperature is still within the allowable range, the reaction zone may have already approached or crossed the safety boundary.

[0006] In summary, existing organic waste gas regenerative combustion or porous medium superenthalpy combustion equipment still lacks a reaction zone positioning mechanism that correlates the physical boundary of the reaction zone formed by pore size classification, the temperature state on both sides of the boundary, and the air intake adjustment action. It is difficult to simultaneously suppress the upstream migration and downstream shift of the reaction zone under conditions of concentration and air volume fluctuations. Summary of the Invention

[0007] The purpose of this invention is to provide an ultra-enthalpy combustion organic waste gas treatment device based on a graded porous medium heat storage body. The target reaction zone is defined by the interface with sudden increase in pore size and the interface with shrinkage in pore size. The boundary temperature difference corresponding to the two interfaces is used as the control quantity for upstream migration and downstream migration, respectively. This makes the graded pore structure, temperature measurement position and air intake regulation form a closed loop, which solves the problem that existing equipment is difficult to stably limit the reaction zone to a safe and fully oxidized target range when the concentration or air volume of organic waste gas fluctuates.

[0008] To address the aforementioned technical problems, the present invention provides the following technical solution: This invention provides an ultra-enthalpy combustion organic waste gas treatment device based on a staged porous media heat storage body, comprising a reaction cylinder, an air inlet mixing unit, a staged porous media heat storage body, a temperature detection unit, and a controller; the air inlet mixing unit includes an organic waste gas inlet valve, a combustion air regulating valve, and a mixing chamber connected to the reaction cylinder; the staged porous media heat storage body is disposed inside the reaction cylinder and sequentially includes an explosion-proof fireproof layer, a preheating migration layer, a reaction positioning layer, and a heat storage and burnout layer along the airflow direction; a pore size abrupt interface is formed between the preheating migration layer and the reaction positioning layer, wherein the downstream equivalent pore size of the pore size abrupt interface is 1.5 to 4 times the upstream equivalent pore size; a pore size retraction interface is formed between the reaction positioning layer and the heat storage and burnout layer, wherein the downstream equivalent pore size of the pore size retraction interface is smaller than the upstream equivalent pore size, and the target reaction zone is defined between the two interfaces; The temperature detection unit includes first to third thermocouples respectively located upstream of the aperture increase interface, within the target reaction zone, and downstream of the aperture retraction interface, with temperatures of T1, T2, and T3 respectively. The controller connects each valve and each thermocouple, using T2-T1 as the upstream boundary temperature difference of the aperture increase interface and T2-T3 as the downstream boundary temperature difference of the aperture retraction interface. When the upstream boundary temperature difference is lower than the upstream threshold and the rate of increase of T1 is greater than the rate of increase of T2, the flow rate of organic waste gas is reduced and / or the amount of combustion air is increased. When the downstream boundary temperature difference is lower than the downstream threshold and the rate of increase of T3 is greater than the rate of increase of T2, the total intake air velocity is reduced and / or the proportion of organic waste gas in the mixed gas is increased, while ensuring the amount of air required for complete oxidation. Both adjustments continue until the corresponding boundary temperature difference is not lower than the corresponding threshold.

[0009] In one embodiment, the equivalent pore size of the explosion-proof fireproof layer is 0.5 mm to 0.8 mm, the equivalent pore size of the preheating migration layer is 0.8 mm to 2.5 mm, the equivalent pore size of the reaction positioning layer is 2.0 mm to 6.0 mm, and the equivalent pore size of the heat storage burnout layer is 1.0 mm to 4.0 mm.

[0010] In one embodiment, the aperture abrupt increase interface is formed by the outlet end face of the preheated migration layer and the inlet end face of the reaction positioning layer being adjacent to each other, and the equivalent aperture of the inlet end of the reaction positioning layer is 1.5 to 4 times the equivalent aperture of the outlet end of the preheated migration layer.

[0011] In one embodiment, the aperture retraction interface is formed by the outlet end face of the reaction positioning layer and the inlet end face of the heat storage burnout layer being adjacent to each other, and the equivalent aperture of the inlet end of the heat storage burnout layer is smaller than the equivalent aperture of the outlet end of the reaction positioning layer, in order to slow down the continued downstream migration of the high-temperature reaction zone.

[0012] In one embodiment, the temperature detection unit includes a first thermocouple, a second thermocouple, and a third thermocouple. The first thermocouple is arranged on the outlet side of the preheating migration layer, the second thermocouple is arranged in the middle of the reaction positioning layer, and the third thermocouple is arranged on the inlet side of the heat storage burnout layer.

[0013] In one embodiment, the upstream threshold and the downstream threshold are calibrated based on the temperature distribution when the superenthalpy combustion reaction zone is stably in the target reaction zone; when the upstream boundary temperature difference is lower than the upstream threshold, and the rate of increase of T1 is greater than the rate of increase of T2 and continues for a preset determination period, the controller determines that the reaction zone migrates upstream across the aperture increase interface; when the downstream boundary temperature difference is lower than the downstream threshold, and the rate of increase of T3 is greater than the rate of increase of T2 and continues for a preset determination period, the controller determines that the reaction zone migrates downstream across the aperture retraction interface.

[0014] In one embodiment, during the startup phase, the controller controls the auxiliary fuel to enter the mixing chamber and burn and heat up in the reaction positioning layer; when T2 reaches the self-sustaining combustion temperature, and the upstream boundary temperature difference and the downstream boundary temperature difference are not lower than their respective thresholds, the controller reduces or cuts off the auxiliary fuel and gradually increases the flow rate of organic waste gas.

[0015] In one embodiment, the cold end isolation chamber is connected to a reflux cooling branch, through which part of the purified flue gas after being cooled at the outlet end of the reaction cylinder is introduced into the cold end isolation chamber to reduce the wall temperature of the explosion-proof and fireproof layer on the side near the inlet end.

[0016] In one embodiment, the air inlet end of the reaction cylinder is provided with a pressure detection element. When the pressure detection element detects that the pressure fluctuation at the air inlet end exceeds a set threshold, the controller closes the organic waste gas inlet valve and maintains the combustion air purging for a preset time.

[0017] In one embodiment, a waste heat exchange chamber is provided downstream of the heat storage and burnout layer, and an air intake preheating channel is provided between the waste heat exchange chamber and the air intake mixing unit for preheating the organic waste gas and combustion air before entering the reaction cylinder using purified flue gas.

[0018] The beneficial effects of this invention are as follows: This invention does not simply place the graded porous medium heat storage body alongside conventional closed-loop temperature control. Instead, it uses the pore size abrupt increase interface and the pore size shrinkage interface as the two physical boundaries of the target reaction zone, and places the first to third thermocouples outside the upstream boundary, inside the target reaction zone, and outside the downstream boundary, respectively. This allows the temperature difference formed by the three temperature measurement points to characterize the degree to which the reaction zone approaches the two pore size boundaries.

[0019] When the upstream boundary temperature difference decreases, it indicates that the high-temperature reaction zone is approaching or has crossed the aperture abrupt increase interface. The controller reduces the organic waste gas flow rate and / or increases the combustion air volume to reduce the heat release intensity per unit volume of the mixed gas and increase the downstream transport effect of the mixed gas. When the downstream boundary temperature difference decreases, it indicates that the reaction zone is approaching or has crossed the aperture shrinkage interface. The controller reduces the total inlet flow rate and / or increases the proportion of organic waste gas while ensuring the amount of air required for complete oxidation, thereby increasing the residence time of the mixed gas in the target reaction zone or restoring the heat release intensity in the target reaction zone.

[0020] Thus, the intake regulation actions with different temperature measurement positions and directions on both sides of the aperture increase interface, aperture retraction interface, and boundary form an interdependent closed-loop positioning relationship, which changes the controlled object from an isolated single point temperature to the position state of the reaction zone relative to the two aperture boundaries. This can simultaneously suppress the risk of backfire and deflagration caused by the upstream migration of the reaction zone and the risk of incomplete oxidation caused by the downstream shift.

[0021] In addition, by combining the explosion-proof fireproof layer, the cold-end isolation chamber and the recirculation cooling branch, the temperature near the air inlet of the reaction cylinder is kept low, and the high-temperature reaction zone is restricted from spreading to the air inlet mixing unit, thereby reducing the risk of premature combustion, backfire or deflagration of the organic waste gas mixture at the air inlet.

[0022] Furthermore, by combining the heat storage burnout layer and the waste heat exchange chamber, the high-temperature purified flue gas after combustion can be used to preheat the front-end mixed gas and extend the residence path of incompletely oxidized components in the high-temperature region, thereby improving the sufficiency of organic waste gas oxidation and thermal utilization efficiency. Attached Figure Description

[0023] To more clearly illustrate the technical solution of the present invention, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0024] Figure 1 This is a schematic diagram of the overall structure of the superenthalpy combustion organic waste gas treatment equipment in this invention; Figure 2 This is a schematic diagram of the hierarchical structure of the graded porous medium heat storage body in this invention; Figure 3 This is a schematic diagram of the structure of the aperture abrupt increase interface and the aperture retraction interface in this invention; Figure 4 This is a schematic diagram of the temperature measuring point arrangement of the temperature detection unit of the present invention.

[0025] The reference numerals in the attached figures are as follows: 1. Reaction cylinder; 11. Inlet end; 12. Outlet end; 13. Cylinder wall; 2. Air intake mixing unit; 21. Organic waste gas intake valve; 22. Combustion air regulating valve; 23. Mixing chamber; 24. Auxiliary fuel valve; 3. Staged porous medium heat storage body; 31. Cold end isolation cavity; 32. Explosion suppression and fireproof layer; 33. Preheating migration layer; 34. Reaction positioning layer; 35. Heat storage and burnout layer; 36. Pore size sudden increase interface; 37. Pore size shrinkage interface; 4. Temperature detection unit; 41. First thermocouple; 42. Second thermocouple; 43. Third thermocouple; 44. Fourth thermocouple; 5. Controller; 6. Pressure testing components; 7. Recirculation cooling branch; 71. Recirculation regulating valve; 8. Waste heat exchange chamber; 81. Inlet preheating channel; 9. Exhaust pipe. Detailed Implementation

[0026] To further illustrate the technical means and effects adopted by the present invention to achieve its intended purpose, the specific implementation methods, structures, features, and effects of the present invention will be described in detail below with reference to the accompanying drawings and preferred embodiments. It should be understood that the following embodiments are for illustrative purposes only and are not intended to limit the scope of protection of the present invention.

[0027] The specific implementation provides an ultra-enthalpy combustion organic waste gas treatment device based on a graded porous media heat storage body. The pore size abrupt increase interface and the pore size contraction interface define the target reaction zone. First to third thermocouples respectively detect the temperature outside the two pore size interfaces and inside the target reaction zone. The controller uses the boundary temperature difference formed by the temperature inside the target reaction zone and the temperatures outside the two interfaces to determine whether the reaction zone is approaching or crossing the corresponding interface, and implements different directions of air intake adjustment for upstream and downstream migration, so that the graded pore structure, temperature measurement position, and control action form a closed loop for reaction zone positioning.

[0028] The superenthalpy combustion referred to in this invention refers to a staged porous media heat storage body that, through heat storage, conduction, and radiative regeneration via a solid framework, transfers a portion of the heat released by the combustion products to the reaction mixture in the opposite direction of the airflow. This results in the mixture entering the target reaction zone having a higher enthalpy value compared to the unheated inlet state, thereby maintaining the oxidation reaction under conditions of low concentration or low calorific value organic waste gas. The target reaction zone is the area jointly defined by the pore size abrupt increase interface and the pore size contraction interface along the airflow direction. It does not mean that the reaction can only occur in this zone, but rather that the peak temperature and main heat release area are controlled within this zone during stable operation of the equipment.

[0029] Example 1 See Figures 1 to 4 As shown, this embodiment provides an ultraenthalpic combustion organic waste gas treatment device based on a graded porous media heat storage body, including a reaction cylinder 1, an air inlet mixing unit 2, a graded porous media heat storage body 3, a temperature detection unit 4, and a controller 5.

[0030] The reaction cylinder 1 has an inlet end 11 and an outlet end 12. The inlet end 11 is used to receive the mixture of organic waste gas and combustion air, and the outlet end 12 is used to discharge the purified flue gas after combustion. The reaction cylinder 1 is made of heat-resistant steel, and a fire-resistant insulation layer is provided on the inner side of the cylinder wall 13 to reduce heat loss during the reaction. The reaction cylinder 1 can be arranged vertically or horizontally; in this embodiment, for ease of explanation, a vertical reaction cylinder with airflow from bottom to top is used as an example for description. Figure 2 , Figure 3 As shown, the hollow arrow indicates the direction of airflow from bottom to top.

[0031] The air intake mixing unit 2 is located on one side of the air intake end 11 of the reaction cylinder 1, and includes an organic waste gas intake valve 21, a combustion air regulating valve 22, and a mixing chamber 23. The organic waste gas intake valve 21 regulates the flow rate of organic waste gas entering the mixing chamber 23, and the combustion air regulating valve 22 regulates the amount of combustion air entering the mixing chamber 23. The organic waste gas and combustion air are mixed in the mixing chamber 23 before entering the reaction cylinder 1; Figure 1 As shown, the arrow in intake mixing unit 2 indicates the intake direction.

[0032] The mixing chamber 23 employs a cavity structure with guide vanes or swirl vanes to improve the uniformity of gas mixing.

[0033] A staged porous media heat storage body 3 is disposed inside the reaction cylinder 1 and sequentially includes an explosion-proof flame barrier layer 32, a preheating migration layer 33, a reaction positioning layer 34, and a heat storage burnout layer 35 along the airflow direction. The cold-end isolation chamber 31 is located between the air intake mixing unit 2 and the explosion-proof flame barrier layer 32. It is a low-temperature buffer space formed between the air intake mixing unit 2 and the staged porous media heat storage body 3, rather than a layer of the porous media heat storage body. The equivalent pore size of the explosion-proof flame barrier layer 32 is smaller than that of the preheating migration layer 33, and it is used to limit the propagation of flames or high-temperature reaction zones to the air intake end 11.

[0034] It should be noted that the equivalent pore size in this invention refers to the average hydraulic diameter of the main connecting channels within the porous medium through which gas can pass. When the porous medium is honeycomb ceramic, the equivalent pore size can be the hydraulic diameter of the honeycomb channels; when the porous medium is foam ceramic or metal foam, the equivalent pore size can be the average size of the throats of the main connecting pores between the foam cells; when the porous medium is a particle packing layer, the equivalent pore size can be the average hydraulic diameter of the main gas flow pores between the particles. The aforementioned equivalent pore size can be obtained through pore structure detection, image analysis, or similar engineering detection methods.

[0035] The preheating migration layer 33 is located downstream of the explosion-proof and fire-resistant layer 32, and its porosity increases along the airflow direction. Specifically, the preheating migration layer 33 has lower porosity on the side closer to the explosion-proof and fire-resistant layer 32 to accommodate cold-end isolation and initial heat storage; the preheating migration layer 33 has higher porosity on the side closer to the reaction positioning layer 34 to reduce airflow resistance and gradually raise the temperature of the mixed gas. Through this porosity-increasing structure, the mixed gas is preheated step by step before reaching the reaction positioning layer 34, preventing the cold mixed gas from directly entering the reaction positioning layer 34 and causing reaction instability.

[0036] The reaction positioning layer 34 is located between the preheating migration layer 33 and the regenerative burnout layer 35. An aperture amplification interface 36 is provided on the inlet side of the reaction positioning layer 34, formed by the adjacent arrangement of the outlet end face of the preheating migration layer 33 and the inlet end face of the reaction positioning layer 34. An aperture retraction interface 37 is provided on the outlet side of the reaction positioning layer 34, formed by the adjacent arrangement of the outlet end face of the reaction positioning layer 34 and the inlet end face of the regenerative burnout layer 35. The region between the aperture amplification interface 36 and the aperture retraction interface 37 constitutes the target reaction zone.

[0037] During application, the gas mixture passes through the preheating migration layer 33 and reaches the pore size abruptly increased interface 36. Because the equivalent pore size at the inlet of the reaction positioning layer 34 is larger than that at the outlet of the preheating migration layer 33, the local flow space increases after the gas mixture enters the reaction positioning layer 34, altering the gas mixing and heat exchange state and making it easier for the exothermic reaction to form a stable high-temperature zone within the reaction positioning layer 34. Simultaneously, the pore size retraction interface 37 at the outlet of the reaction positioning layer 34 relatively contracts the downstream pore channels, restricting the continued downstream migration of the high-temperature reaction zone. Therefore, the reaction positioning layer 34 is not a simple combustion layer, but rather defines the location of the reaction zone through the combined effect of the inlet-side pore size abruptly increased and the outlet-side pore size retraction.

[0038] The regenerative burnout layer 35 is located downstream of the reaction positioning layer 34 and is used to continue absorbing the heat of reaction and to further burn off any incompletely oxidized organic components. The regenerative burnout layer 35 can be made of honeycomb ceramic, foam ceramic, ceramic particles, or composite ceramic. In an optional embodiment, the heat capacity of the regenerative burnout layer 35 is greater than that of the reaction positioning layer 34 to improve the heat storage capacity on the outlet end 12 side.

[0039] The temperature detection unit 4 includes a first thermocouple 41, a second thermocouple 42, and a third thermocouple 43. The first thermocouple 41 is located on the outlet side of the preheating migration layer 33 and upstream of the aperture increase interface 36, used to characterize whether the reaction zone crosses the upstream boundary of the target reaction zone. The second thermocouple 42 is located within the reaction positioning layer 34 and used to characterize the temperature within the target reaction zone. The third thermocouple 43 is located on the inlet side of the heat storage burnout layer 35 and downstream of the aperture retraction interface 37, used to characterize whether the reaction zone crosses the downstream boundary of the target reaction zone. The first thermocouple 41, the second thermocouple 42, and the third thermocouple 43 are all electrically connected to the controller 5, and their detected temperatures are denoted as T1, T2, and T3, respectively.

[0040] Controller 5 uses T2-T1 as the upstream boundary temperature difference corresponding to the aperture increase interface 36, and T2-T3 as the downstream boundary temperature difference corresponding to the aperture decrease interface 37. These two boundary temperature differences are not ordinary temperature difference monitoring values, but rather state variables representing the reaction zone locations corresponding to the two aperture change interfaces. Under stable operating conditions, T2 is higher than both T1 and T3, the upstream boundary temperature difference is not lower than the upstream threshold, and the downstream boundary temperature difference is not lower than the downstream threshold, indicating that the main heat release region is located between the aperture increase interface 36 and the aperture decrease interface 37.

[0041] When the upstream boundary temperature difference is lower than the upstream threshold, and the rate of increase of T1 is greater than the rate of increase of T2, the controller 5 determines that the reaction zone is approaching or crossing the aperture abrupt increase interface 36 and migrating upstream. It then reduces the opening of the organic waste gas inlet valve 21 and / or increases the opening of the combustion air regulating valve 22 to reduce the heat release intensity per unit volume of the mixed gas and return the main heat release area to the reaction positioning layer 34. When the downstream boundary temperature difference is lower than the downstream threshold, and the rate of increase of T3 is greater than the rate of increase of T2, the controller 5 determines that the reaction zone is approaching or crossing the aperture retraction interface 37 and migrating downstream. While ensuring the amount of air required for complete oxidation, it reduces the total inlet flow rate and / or increases the proportion of organic waste gas in the mixed gas to prolong the residence time of the mixed gas in the reaction positioning layer 34 or restore the heat release intensity in the target reaction zone until the corresponding boundary temperature difference recovers to above its threshold.

[0042] Through the above structure, the aperture abruptly increasing interface 36 and the aperture shrinking interface 37 provide the physical boundaries of the target reaction zone. The first to third thermocouples provide position feedback corresponding one-to-one with the two physical boundaries. The controller 5 implements different directions of air intake adjustment according to the state of the reaction zone crossing different boundaries. Therefore, the hierarchical aperture structure, temperature measuring points, and control actions form an inseparable reaction zone positioning closed loop, rather than a simple superposition of the layered porous medium structure and conventional single-point temperature control.

[0043] Example 2 See Figure 2 and Figure 3As shown in Example 1, in order to further illustrate the pore parameters of the hierarchical porous medium heat storage body 3, this example provides a specific pore size configuration method.

[0044] The explosion-suppressing fireproof layer 32 has an equivalent pore size of 0.5 mm to 0.8 mm, a thickness of 20 mm to 70 mm, and a porosity of 30% to 60%. This layer uses a smaller equivalent pore size to reduce flame propagation and maintain a lower temperature on the side of the mixed gas entering the reaction cylinder 1 near the cold-end isolation chamber 31. The explosion-suppressing fireproof layer 32 is made of small-pore honeycomb ceramic, sintered metal porous sheets, ceramic particle press-fit layers, or porous ceramic plates.

[0045] The preheating migration layer 33 has an equivalent pore size of 0.8 mm to 2.5 mm and a porosity of 45% to 75%. The preheating migration layer 33 is made of open-cell silicon carbide foam ceramic. The open-cell silicon carbide foam ceramic has a continuous open-cell structure, which allows the mixed gas to pass through its pore channels and absorb radiant heat and conductive heat from the reaction positioning layer 34 and the heat storage and burnout layer 35 through the silicon carbide ceramic skeleton, thereby preheating the organic waste gas and combustion air mixture before entering the reaction positioning layer 34 in stages.

[0046] In one specific embodiment, the preheating migration layer 33 is sequentially arranged along the airflow direction, including a first preheating buffer section, a second heat storage transition section, and a third pore-expanding inlet section. The first preheating buffer section is located near the explosion-proof and fire-resistant layer 32 and uses small-pore open-cell silicon carbide foam ceramic with an equivalent pore size of 0.8 mm to 1.2 mm and a porosity of 45% to 55%. The second heat storage transition section is located between the first preheating buffer section and the third pore-expanding inlet section and uses medium-pore open-cell silicon carbide foam ceramic with an equivalent pore size of 1.2 mm to 1.8 mm and a porosity of 55% to 65%. The third pore-expanding inlet section is located near the reaction positioning layer 34 and uses large-pore open-cell silicon carbide foam ceramic with an equivalent pore size of 1.8 mm to 2.5 mm and a porosity of 65% to 75%.

[0047] Therefore, although the preheating migration layer 33 is made entirely of the same type of open-cell silicon carbide foam ceramic, it forms a gradient preheating structure by gradually increasing the equivalent pore size and porosity along the airflow direction. The mixed gas first undergoes initial heating in the first preheating buffer section by utilizing the larger heat transfer area per unit volume provided by the small-pore structure, then continues to absorb heat from the ceramic skeleton in the second heat storage transition section, and finally enters the reaction positioning layer 34 after reducing the pressure drop increment along the path in the third pore expansion inlet section. This structure utilizes the gradient changes in pore size, specific surface area, solid-gas heat transfer, and pressure drop to achieve step-by-step preheating.

[0048] The equivalent pore size of the reaction positioning layer 34 is 2.0 mm to 6.0 mm, and the porosity is 70% to 90%. The reaction positioning layer 34 is made of open-cell foam ceramic or macroporous honeycomb ceramic, which allows the organic waste gas and combustion air to form a sufficient heat exchange and reaction space within the layer. The reaction positioning layer 34 does not simply increase the pore size, but rather, together with the upstream pore size abrupt interface 36 and the downstream pore size contraction interface 37, it defines the reaction location.

[0049] The equivalent pore size of the heat storage burnout layer 35 is 1.0 mm to 4.0 mm, and the porosity is 50% to 80%. The equivalent pore size of the heat storage burnout layer 35 is smaller than or no larger than the equivalent pore size of the reaction positioning layer 34, so that the velocity and heat transfer state of the airflow change after leaving the reaction positioning layer 34, thereby slowing down the excessive migration of the high-temperature reaction zone to the outlet end 12.

[0050] When applied, when the concentration of organic waste gas is low, the preheating migration layer 33 preheats the mixed gas step by step by increasing porosity along the airflow direction, so that the reaction positioning layer 34 can maintain a high base temperature. When the concentration of organic waste gas increases for a short time, the preheating migration layer 33 between the explosion suppression and fireproof layer 32 and the pore size increase interface 36 can form an upstream buffer zone, reducing the possibility of the high-temperature reaction zone directly migrating back to the air inlet 11. When the air volume increases or the concentration decreases, the pore size shrinkage interface 37 and the heat storage and burnout layer 35 can reduce the probability of the reaction zone continuing to shift downstream.

[0051] Example 3 See Figure 3 As shown, based on Example 1, in order to further solve the problem of the lack of a clear positioning boundary between the reaction positioning layer 34 and the upstream and downstream porous media layers, this embodiment further defines the pore size abrupt increase interface 36 and the pore size shrinkage interface 37.

[0052] The aperture abrupt increase interface 36 is formed by the adjacent arrangement of the outlet end face of the preheating migration layer 33 and the inlet end face of the reaction positioning layer 34. The equivalent aperture at the outlet end of the preheating migration layer 33 is 1.0 mm to 2.0 mm, and the equivalent aperture at the inlet end of the reaction positioning layer 34 is 3.0 mm to 5.0 mm, making the equivalent aperture at the inlet end of the reaction positioning layer 34 1.5 to 4 times that of the equivalent aperture at the outlet end of the preheating migration layer 33. This aperture abrupt increase relationship causes a change in the gas flow diffusion space when the mixed gas enters the larger aperture region from the smaller aperture region, and makes heat release more easily concentrated from the inlet side to the middle region of the reaction positioning layer 34.

[0053] The aperture retraction interface 37 is formed by the adjacent arrangement of the outlet end face of the reaction positioning layer 34 and the inlet end face of the regenerative burnout layer 35. The equivalent aperture at the outlet end of the reaction positioning layer 34 is 3.0 mm to 6.0 mm, and the equivalent aperture at the inlet end of the regenerative burnout layer 35 is 1.5 mm to 3.5 mm, making the equivalent aperture at the inlet end of the regenerative burnout layer 35 smaller than the equivalent aperture at the outlet end of the reaction positioning layer 34. This aperture retraction relationship ensures that the high-temperature reaction zone continues to propagate downstream due to changes in pore structure, reducing the possibility of the reaction zone being excessively pushed to the rear section of the regenerative burnout layer 35 under high airflow conditions.

[0054] In application, the aperture abruptly increasing interface 36 creates a boundary for changing propagation conditions between the smaller upstream pore channels and the larger pore channels of the reaction positioning layer 34, inducing the formation of the main exothermic region downstream. The aperture shrinking interface 37, by reducing the downstream equivalent aperture, increasing solid-gas heat exchange and propagation resistance, forms another boundary restricting the further downward movement of the high-temperature core region. The controller 5 uses T2-T1 and T2-T3 to characterize the degree to which the reaction zone approaches the two interfaces, respectively, and implements different directions of air intake regulation for the decrease in the temperature difference between the upstream and downstream boundaries, thereby transforming the passive positioning effect of the two aperture interfaces into a detectable and calibrable closed-loop positioning effect.

[0055] Example 4 See Figure 4 As shown in Embodiment 1, in order to establish a clear correspondence between temperature detection and aperture boundary, this embodiment provides a specific control method for temperature detection unit 4 and controller 5.

[0056] The measuring end of the first thermocouple 41 is located 5mm to 30mm upstream of the aperture abrupt increase interface 36, the measuring end of the second thermocouple 42 is located at 40% to 60% of the axial length of the reaction positioning layer 34, and the measuring end of the third thermocouple 43 is located 5mm to 30mm downstream of the aperture retraction interface 37. These distances allow the first thermocouple 41 and the third thermocouple 43 to respectively sense the temperature rise of the main heat-dissipating region after crossing the two aperture interfaces, while reducing the judgment fluctuations caused by the combined influence of the thermal conductivity of the adjacent two layers when they are directly at the interface.

[0057] The controller 5 acquires T1, T2, and T3 with a sampling period of 0.5s to 5s, and calculates the upstream boundary temperature difference ΔTu = T2 - T1 and the downstream boundary temperature difference ΔTd = T2 - T3. The upstream threshold ΔTu0 and the downstream threshold ΔTd0 are calibrated based on the temperature distribution obtained when the equipment is stably positioned in the reaction positioning layer 34 in the reaction zone; different specifications of equipment may have different thresholds, but both the upstream and downstream thresholds are used to retain the positive temperature difference between the temperature inside the reaction positioning layer 34 and the temperature outside the corresponding boundary.

[0058] When ΔTu is not lower than ΔTu0 and ΔTd is not lower than ΔTd0, the controller 5 determines that the main heat-generating area is in the target reaction zone. To reduce misjudgments caused by instantaneous disturbances, the controller 5 can also calculate the temperature rise rate of each temperature measurement point within a preset time window. When ΔTu is lower than ΔTu0, and the rise rate of T1 is greater than the rise rate of T2 and continues for a preset judgment period, the controller 5 determines that the reaction zone has migrated across the aperture abrupt increase interface 36 to the preheating migration layer 33.

[0059] In response to the upstream migration state, controller 5 reduces the opening of the organic waste gas inlet valve 21 and / or increases the opening of the combustion air regulating valve 22. Reducing the organic waste gas flow rate while maintaining the combustion air volume can reduce the proportion of combustible components in the mixture and the heat release intensity per unit volume; increasing the combustion air volume can dilute the combustible components and increase the downstream transport effect. Controller 5 continues to perform regulation until ΔTu recovers to above ΔTu0; if ΔTu continues to decrease, the cold end protection control described in Example 5 is entered.

[0060] When ΔTd is lower than ΔTd0, and the rate of increase of T3 is greater than the rate of increase of T2 for a preset judgment period, the controller 5 determines that the reaction zone has migrated beyond the aperture retraction interface 37 to the regenerative combustion layer 35. For the downstream migration state, the controller 5 simultaneously reduces the opening of the organic waste gas inlet valve 21 and the combustion air regulating valve 22 to reduce the total inlet gas velocity and prolong the residence time of the mixed gas in the reaction positioning layer 34; or, under the condition of ensuring the amount of air required for complete oxidation and that the organic waste gas concentration is within the allowable range of the equipment, it increases the proportion of organic waste gas in the mixed gas to restore the exothermic intensity in the target reaction zone. The controller 5 continues to perform adjustments until ΔTd recovers to above ΔTd0.

[0061] Therefore, instead of making conventional adjustments based on isolated temperature levels, the controller 5 uses the two aperture interfaces as the upstream and downstream migration boundaries, respectively, to identify the migration direction based on the corresponding boundary temperature difference and temperature change trend, and executes adjustment actions that enable the reaction zone to reverse back to the target reaction zone.

[0062] Example 5 See Figure 1 and Figure 4 As shown, based on Embodiment 1, in order to further reduce the risk of backfire and deflagration on the intake end 11 side, this embodiment provides a cold end isolation cavity 31 and a recirculation cooling branch 7.

[0063] A cold-end isolation chamber 31 is disposed between the air intake mixing unit 2 and the explosion-proof and fire-resistant layer 32. The axial length of the cold-end isolation chamber 31 is 30mm to 150mm, which is used to form a buffer space between the mixing chamber 23 and the high-temperature porous medium. The cold-end isolation chamber 31 is also equipped with a temperature detection point. When the temperature inside the cold-end isolation chamber 31 exceeds the set value, the controller 5 reduces the intake volume of organic waste gas or starts purging.

[0064] One end of the reflux cooling branch 7 is connected to the exhaust pipe 9 downstream of the gas outlet 12 of the reaction cylinder 1, and the other end is connected to the cold end isolation chamber 31. Since the purified flue gas in the exhaust pipe 9 has a low content of combustible components after waste heat exchange or natural cooling, it can be introduced into the cold end isolation chamber 31 as a dilution and cooling gas to reduce the volume fraction of combustible components in the mixture within the cold end isolation chamber 31 and the temperature on the inlet side of the explosion-proof fireproof layer 32. A reflux regulating valve 71 is installed on the reflux cooling branch 7, and the reflux regulating valve 71 is electrically connected to the controller 5.

[0065] In application, when the upstream boundary temperature difference is lower than the upstream threshold, indicating that the reaction zone is approaching the upstream side of the aperture abrupt increase interface 36, the controller 5 first reduces the organic waste gas intake and / or increases the combustion air intake. When the fourth thermocouple 44 detects that the temperature inside the cold end isolation chamber 31 simultaneously reaches the cold end safety threshold, the controller 5 opens the reflux regulating valve 71, allowing part of the cooled purified flue gas to enter the cold end isolation chamber 31 to dilute and cool the intake side of the explosion-proof and fireproof layer 32. Therefore, the reflux cooling branch 7 is not an independent cooling structure, but a second-level protection structure triggered when the upstream boundary temperature difference continues to decrease.

[0066] In a further embodiment, the temperature detection unit 4 further includes a fourth thermocouple 44, which is disposed in the cold end isolation chamber 31 or on the side of the explosion-proof and fire-resistant layer 32 near the air inlet 11, for detecting the temperature inside the cold end isolation chamber 31. When the fourth thermocouple 44 detects that the temperature inside the cold end isolation chamber 31 exceeds a set safety threshold, the controller 5 closes the organic waste gas inlet valve 21 and opens the combustion air regulating valve 22 for purging; simultaneously, the controller 5 opens the reflux regulating valve 71, allowing some of the cooled purified flue gas to enter the cold end isolation chamber 31 through the reflux cooling branch 7, thereby reducing the wall temperature of the explosion-proof and fire-resistant layer 32 on the side near the air inlet 11. Thus, the fourth thermocouple 44 can serve as a cold end safety monitoring point, forming a linkage detection structure with the first thermocouple 41, the second thermocouple 42, and the third thermocouple 43 for reaction zone position control and cold end backfire protection.

[0067] Furthermore, the cold-end isolation chamber 31 in this embodiment is not simply an increase in chamber space, but rather, together with the explosion-proof and fire-resistant layer 32, the first thermocouple 41, and the recirculation cooling branch 7, it constitutes a backfire prevention and explosion-proof protection structure. When the reaction zone shows an upstream migration trend, the controller 5 corrects the position of the reaction zone by reducing the amount of organic waste gas entering and increasing the amount of combustion air, and also reduces the cold-end temperature through the recirculation cooling branch 7, thereby forming a safety protection method that combines active control and passive fire isolation.

[0068] Example 6 See Figure 1 and Figure 4 As shown, based on Embodiment 1, in order to further address the safety risks caused by pressure fluctuations or abnormal combustion at the intake end, this embodiment provides a pressure detection element 6 and a safety purging control method.

[0069] The pressure detection element 6 is located at the air inlet 11 of the reaction cylinder 1 or the mixing chamber 23, and is used to detect pressure fluctuations near the air inlet 11. The pressure detection element 6 is a pressure sensor, a differential pressure sensor, or a pressure switch. The pressure detection element 6 is electrically connected to the controller 5.

[0070] The steady-state pressure reference is the average pressure detected by the pressure detection element 6 within a preset time window when the equipment is stably in the target reaction zone. The pressure threshold is the allowable fluctuation amount relative to this steady-state pressure reference.

[0071] During application, the controller 5 receives pressure signals from the pressure detection element 6 in real time. When the pressure detection element 6 detects that the pressure fluctuation at the air inlet 11 exceeds the set threshold, or that the pressure rises abnormally within a short period of time, the controller 5 determines that there is a risk of backfire, blockage, or abnormal combustion. At this time, the controller 5 closes the organic waste gas inlet valve 21 and keeps the combustion air regulating valve 22 open, so that the combustion air purges the air inlet 11 of the reaction cylinder 1, the cold end isolation chamber 31, and the explosion-proof fireproof layer 32. The preset purging time is 10s to 180s.

[0072] During the purging process, the controller 5 continues to collect the detection signals from the pressure sensor 6 and the first to fourth thermocouples. When the pressure stabilizes, the detection temperature of the fourth thermocouple 44 is below the cold junction safety threshold, and the upstream boundary temperature difference recovers to above the upstream threshold, the controller 5 allows the organic waste gas inlet valve 21 to reopen at a lower opening degree and gradually restores the organic waste gas intake volume; if any recovery condition is not met, the organic waste gas inlet valve 21 remains closed and an alarm signal is output.

[0073] In this embodiment, the pressure detection element 6 is linked with the temperature detection unit 4, so that the equipment can not only control the position of the reaction zone relative to the aperture increase interface 36 and aperture retraction interface 37 according to the upstream boundary temperature difference, the downstream boundary temperature difference and the temperature rise rate of the corresponding temperature measurement point, but also cut off the supply of organic waste gas and purge it in time when abnormal pressure fluctuations occur, thereby improving the operational safety of the equipment under the condition of fluctuation in organic waste gas concentration.

[0074] Example 7 See Figure 1 As shown, based on Embodiment 1, in order to further improve heat utilization efficiency and reduce the difficulty of self-sustaining combustion of the equipment, this embodiment provides a waste heat exchange chamber 8 and an air intake preheating channel 81.

[0075] The waste heat exchange chamber 8 is located downstream of the heat storage and combustion layer 35, and is connected to the exhaust pipe 9. The intake preheating channel 81 is located between the waste heat exchange chamber 8 and the intake mixing unit 2, used to exchange heat between the organic waste gas, combustion air, or both entering the mixing chamber 23 and the purified flue gas. The intake preheating channel 81 adopts a sleeve-type heat exchange structure, a plate-type heat exchange structure, or a jacketed heat exchange structure. One end of the intake preheating channel 81 extends into the waste heat exchange chamber 8, and the other end extends into the mixing chamber 23. The waste heat of the purified flue gas introduced into the exhaust pipe 9 through the waste heat exchange chamber 8 is indirectly transferred to the organic waste gas and / or combustion air in the mixing chamber 23 via the intake preheating channel 81 to preheat the gas entering the mixing chamber 23. The purified flue gas after heat exchange is discharged through the waste heat exchange chamber 8. Figure 1 The arrow in the residual heat exchange chamber 8 indicates the direction of flue gas exhaust.

[0076] During application, the purified flue gas, after combustion in the regenerative combustion chamber 35, still retains a relatively high temperature. This purified flue gas enters the waste heat exchange chamber 8 and indirectly exchanges heat with the organic waste gas and / or combustion air in the inlet preheating channel 81, raising the temperature of the mixed gas before entering the reaction cylinder 1. This preheating method reduces the external heat required to maintain superenthalpy combustion after startup.

[0077] It should be noted that the main function of the waste heat exchange chamber 8 and the inlet preheating channel 81 is to enhance the thermal efficiency of the reaction zone positioning and migration control scheme in Example 1. This allows the waste heat exchange chamber 8 to increase the temperature of the mixed gas before it enters the preheating migration layer 33 in low-concentration organic waste gas treatment scenarios, making it easier for the reaction positioning layer 34 to maintain the target reaction temperature, thereby reducing the probability of the reaction zone shifting downstream due to insufficient heat.

[0078] Example 8 See Figure 1 and Figure 4As shown, based on Embodiment 1, this embodiment provides a start-up control method to further illustrate the device start-up and self-sustaining combustion process.

[0079] The intake mixing unit 2 also includes an auxiliary fuel valve 24, which is used to supply auxiliary fuel to the mixing chamber 23 or the vicinity of the reaction positioning layer 34. The auxiliary fuel is natural gas, liquefied petroleum gas, hydrogen, or other combustible gas. The auxiliary fuel valve 24 is electrically connected to the controller 5.

[0080] During startup, controller 5 opens combustion air regulating valve 22 and introduces combustion air into reaction cylinder 1 at a low flow rate. Subsequently, controller 5 controls auxiliary fuel valve 24 to open, causing auxiliary fuel to burn and heat up near reaction positioning layer 34. Temperature detection unit 4 continuously monitors the temperatures of first thermocouple 41, second thermocouple 42, and third thermocouple 43. Controller 5 determines whether self-sustaining operation conditions are met based on T2, upstream boundary temperature difference, and downstream boundary temperature difference, and controls organic waste gas inlet valve 21 and auxiliary fuel valve 24 according to the following criteria.

[0081] In one possible implementation, the self-sustaining combustion temperature is set to 650℃~850℃. When T2 reaches the self-sustaining combustion temperature, and the upstream boundary temperature difference ΔTu is not lower than the upstream threshold ΔTu0 and the downstream boundary temperature difference ΔTd is not lower than the downstream threshold ΔTd0, the controller 5 determines that the main exothermic zone has stabilized in the target reaction zone and meets the self-sustaining operation conditions. Subsequently, the controller 5 gradually reduces or cuts off the auxiliary fuel, and maintains the reaction positioning layer 34 within the target temperature range of 750℃~950℃ by adjusting the organic waste gas inlet valve 21 and the combustion air regulating valve 22.

[0082] During operation, controller 5 prioritizes reaction zone position control according to the upstream boundary temperature difference ΔTu, downstream boundary temperature difference ΔTd, and corresponding temperature rise rate as described in Example 4. Provided that ΔTu and ΔTd are not lower than their respective thresholds, if T2 is higher than the target temperature upper limit, the organic waste gas intake volume is reduced and / or the combustion air volume is increased; if T2 is lower than the target temperature lower limit, the total intake gas flow rate is reduced while ensuring the air volume required for complete oxidation, and the auxiliary fuel valve 24 is briefly opened for supplementary heating if necessary. Therefore, the upper and lower temperature limits of T2 are used for fine-tuning the temperature within the target reaction zone and do not replace reaction zone position control based on the two boundary temperature differences.

[0083] This embodiment combines auxiliary fuel start-up, self-sustaining combustion determination, and reaction zone position control to enable the equipment to stably enter the operating state in low-concentration organic waste gas scenarios and reduce the continuous consumption of auxiliary fuel during operation.

[0084] Example 9 To further illustrate the application of this invention in typical organic waste gas treatment scenarios, this embodiment provides feasible operating parameters. These operating parameters are used to illustrate the feasibility of the equipment and do not constitute a limitation on the scope of protection of this invention.

[0085] In one application scenario, the organic waste gas is a low-concentration organic waste gas containing ethyl acetate, toluene, isopropanol, or mixtures thereof. Before entering the equipment, the organic waste gas is first filtered or dusted to reduce the clogging of the staged porous media heat storage body 3 by particulate matter. The concentration of organic waste gas entering the air inlet mixing unit 2 is 200 mg / m³ to 3000 mg / m³, the processing air volume is 500 Nm³ / h to 10000 Nm³ / h, and the combustion air volume is adjusted by the controller 5 according to the preset excess air coefficient and the correspondence between the organic waste gas flow rate and the combustion air volume.

[0086] Under stable operating conditions, the temperature detected by the first thermocouple 41 is maintained between 350℃ and 650℃, the temperature detected by the second thermocouple 42 is maintained between 750℃ and 950℃, and the temperature detected by the third thermocouple 43 is maintained between 600℃ and 850℃. The controller 5 calculates the upstream boundary temperature difference ΔTu = T2 - T1 and the downstream boundary temperature difference ΔTd = T2 - T3; when ΔTu is not lower than the upstream threshold ΔTu0 and ΔTd is not lower than the downstream threshold ΔTd0, it is determined that the main heat release area is maintained within the reaction positioning layer 34.

[0087] When the number of production stations opened increases, causing the concentration of organic waste gas to rise, or when the total volume of organic waste gas decreases, the heat release intensity per unit volume in the target reaction zone increases, and the reaction zone tends to migrate upstream. When ΔTu is lower than ΔTu0, and the rate of increase of T1 is greater than the rate of increase of T2 and continues for a preset judgment period, the controller 5 reduces the opening of the organic waste gas inlet valve 21 and / or increases the opening of the combustion air regulating valve 22; if the temperature detected by the fourth thermocouple 44 reaches the cold end safety threshold, the return regulating valve 71 is also opened to introduce part of the cooled purified flue gas into the cold end isolation chamber 31 until ΔTu recovers to above ΔTu0.

[0088] When the number of production stations shut down increases, causing a decrease in the concentration of organic waste gas, or when the treatment air volume increases, the reaction zone tends to migrate downstream. When ΔTd is lower than ΔTd0, and the rate of increase of T3 is greater than the rate of increase of T2 and continues for the preset judgment period, the controller 5 reduces the total intake airflow rate and / or increases the proportion of organic waste gas in the mixed gas while ensuring the amount of air required for complete oxidation; when the temperature of the target reaction zone is still lower than the set value for maintaining self-sustaining combustion, the auxiliary fuel valve 24 is opened briefly for supplemental heating until ΔTd recovers to above ΔTd0.

[0089] Through the above-described operating mode, the present invention can maintain the super-enthalpy combustion reaction zone within the target reaction zone under conditions of low concentration, concentration fluctuation, and air volume fluctuation, thereby taking into account the operating performance of preventing backfire, stabilizing combustion, and ensuring sufficient oxidation.

[0090] The above description is merely a preferred embodiment of the present invention and is not intended to limit the present invention in any way. Although the present invention has been disclosed above with reference to preferred embodiments, it is not intended to limit the present invention. Any person skilled in the art can make some modifications or alterations to the above-disclosed technical content to create equivalent embodiments without departing from the scope of the present invention. Any simple modifications, equivalent changes, and alterations made to the above embodiments based on the technical essence of the present invention without departing from the scope of the present invention shall still fall within the scope of the present invention.

Claims

1. A superenthalpy combustion organic waste gas treatment device based on a staged porous media heat storage medium, characterized in that, The system includes a reaction cylinder, an air intake mixing unit, a staged porous media heat storage body, a temperature detection unit, and a controller. The air intake mixing unit includes an organic waste gas intake valve, a combustion air regulating valve, and a mixing chamber connected to the reaction cylinder. The staged porous media heat storage body is disposed within the reaction cylinder and sequentially includes an explosion-proof fireproof layer, a preheating migration layer, a reaction positioning layer, and a heat storage and burnout layer along the airflow direction. A pore size abrupt interface is formed between the preheating migration layer and the reaction positioning layer, with the downstream equivalent pore size of the abrupt interface being 1.5 to 4 times the upstream equivalent pore size. A pore size retraction interface is formed between the reaction positioning layer and the heat storage and burnout layer, with the downstream equivalent pore size of the retraction interface being smaller than the upstream equivalent pore size, defining a target reaction zone between the two interfaces. The temperature detection unit includes components respectively disposed within the reaction cylinder. The first to third thermocouples located upstream of the aperture increase interface, within the target reaction zone, and downstream of the aperture decrease interface have temperatures of T1, T2, and T3, respectively. The controller connects each valve and each thermocouple, using T2-T1 as the upstream boundary temperature difference of the aperture increase interface and T2-T3 as the downstream boundary temperature difference of the aperture decrease interface. When the upstream boundary temperature difference is lower than the upstream threshold and the rate of increase of T1 is greater than the rate of increase of T2, the flow rate of organic waste gas is reduced and / or the combustion air volume is increased. When the downstream boundary temperature difference is lower than the downstream threshold and the rate of increase of T3 is greater than the rate of increase of T2, the total intake air velocity is reduced and / or the proportion of organic waste gas in the mixed gas is increased, while ensuring the amount of air required for complete oxidation. Both adjustments continue until the corresponding boundary temperature difference is not lower than the corresponding threshold.

2. The superenthalpy combustion organic waste gas treatment equipment according to claim 1, characterized in that, The equivalent pore size of the explosion-suppressing and fire-resistant layer is 0.5 mm to 0.8 mm; the equivalent pore size of the preheating and migration layer is 0.8 mm to 2.5 mm and the porosity is 45% to 75%, and its equivalent pore size and porosity increase along the airflow direction; the equivalent pore size of the reaction positioning layer is 2.0 mm to 6.0 mm and the porosity is 70% to 90%; the equivalent pore size of the heat storage and burnout layer is 1.0 mm to 4.0 mm and the porosity is 50% to 80%.

3. The superenthalpy combustion organic waste gas treatment equipment according to claim 2, characterized in that, The preheating migration layer includes, in sequence along the airflow direction, a first preheating buffer section, a second heat storage transition section, and a third pore-expanding inlet section; the first preheating buffer section has an equivalent pore size of 0.8 mm to 1.2 mm and a porosity of 45% to 55%, the second heat storage transition section has an equivalent pore size of 1.2 mm to 1.8 mm and a porosity of 55% to 65%, and the third pore-expanding inlet section has an equivalent pore size of 1.8 mm to 2.5 mm and a porosity of 65% to 75%.

4. The superenthalpy combustion organic waste gas treatment equipment according to claim 1, characterized in that, The first thermocouple is located 5mm to 30mm upstream of the aperture abrupt increase interface, the second thermocouple is located at 40% to 60% of the axial length of the reaction positioning layer, and the third thermocouple is located 5mm to 30mm downstream of the aperture retraction interface; the controller acquires T1, T2, and T3 with an acquisition period of 0.5s to 5s.

5. The superenthalpy combustion organic waste gas treatment equipment according to claim 4, characterized in that, The upstream and downstream thresholds are calibrated based on the temperature distribution when the superenthalpy combustion reaction zone is stably located in the target reaction zone. When T2 is higher than T1 and T3, and the upstream boundary temperature difference and the downstream boundary temperature difference are not lower than their respective thresholds, the controller determines that the superenthalpy combustion reaction zone is in the target reaction zone. When the upstream boundary temperature difference is lower than the upstream threshold and the rate of increase of T1 is greater than the rate of increase of T2 and continues for a preset determination period, the controller reduces the organic waste gas flow rate and / or increases the combustion air volume. When the downstream boundary temperature difference is lower than the downstream threshold and the rate of increase of T3 is greater than the rate of increase of T2 and continues for the preset determination period, the controller reduces the total intake air velocity and / or increases the proportion of organic waste gas in the mixed gas while ensuring the amount of air required for complete oxidation.

6. The superenthalpy combustion organic waste gas treatment equipment according to claim 1, characterized in that, A cold-end isolation chamber is formed between the explosion-proof and fire-resistant layer and the air intake mixing unit. The cold-end isolation chamber is connected to the exhaust pipe downstream of the gas outlet of the reaction cylinder through a reflux cooling branch equipped with a reflux regulating valve. The temperature detection unit also includes a fourth thermocouple located in the cold-end isolation chamber or on the air intake side of the explosion-proof and fire-resistant layer. When the upstream boundary temperature difference is lower than the upstream threshold and the detection temperature of the fourth thermocouple reaches the cold-end safety threshold, the controller reduces the organic waste gas flow rate, increases the combustion air volume, and opens the reflux regulating valve.

7. The superenthalpy combustion organic waste gas treatment equipment according to claim 6, characterized in that, The inlet end of the reaction cylinder or the mixing chamber is equipped with a pressure detection device; when the pressure detected by the pressure detection device fluctuates more than the pressure threshold relative to the steady-state pressure reference, the controller closes the organic waste gas inlet valve, maintains the combustion air regulating valve open for 10s to 180s, and allows the organic waste gas inlet valve to reopen after the pressure stabilizes, the detection temperature of the fourth thermocouple is lower than the cold junction safety threshold, and the upstream boundary temperature difference recovers to above the upstream threshold.

8. The superenthalpy combustion organic waste gas treatment equipment according to claim 1, characterized in that, The intake mixing unit also includes an auxiliary fuel valve; during the start-up phase, the controller supplies auxiliary fuel to the mixing chamber through the auxiliary fuel valve, causing the auxiliary fuel to burn and heat up in the reaction positioning layer; when T2 reaches the self-sustaining combustion temperature, and the upstream boundary temperature difference and the downstream boundary temperature difference are not lower than their respective thresholds, the auxiliary fuel is reduced or cut off and the organic waste gas flow rate is gradually increased.

9. The superenthalpy combustion organic waste gas treatment equipment according to claim 1, characterized in that, Downstream of the heat storage and burnout layer is a waste heat exchange chamber, and an air intake preheating channel is provided between the waste heat exchange chamber and the air intake mixing unit. The air intake preheating channel is used to indirectly exchange heat between the organic waste gas and / or combustion air and the purified flue gas after combustion.

10. The superenthalpy combustion organic waste gas treatment equipment according to claim 1, characterized in that, The reaction positioning layer is an open-cell foam ceramic or a large-pore honeycomb ceramic, and the heat capacity of the heat storage and burnout layer is greater than that of the reaction positioning layer.

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