PDR-RTO equipment for treating high-concentration VOCs waste gas

Abstract

The invention provides PDR-RTO equipment for treating high-concentration VOCs waste gas, and belongs to the technical field of waste gas treatment. According to the PDR-RTO equipment for treating the high-concentration VOCs waste gas, the low-concentration VOCs waste gas and the high-concentration VOCs waste gas are introduced into the PDR-RTO equipment in a split-flow mode, the low-concentration VOCs waste gas is introduced into the PDR-RTO equipment through a gas inlet of an RTO (regenerative thermal oxidizer), and the high-concentration VOCs waste gas is introduced into the PDR-RTO equipment through a PDR (high-temperature pulse wave reactor); the low-concentration VOCs waste gas is subjected to preheating and high-temperature oxidation treatment through a heat storage bed of the RTO, and energy generated by combustion is recycled through the heat storage bed, so that the VOCs waste gas can be thoroughly destroyed and treated; high-concentration VOCs waste gas is guided into a high-temperature oxidation reaction chamber of the RTO through the PDR, the VOCs waste gas is subjected to detonation damage and then is subjected to high-temperature thorough oxidation, and part of high-temperature waste gas is recycled through a waste heat recycling boiler arranged on the side to generate steam.

Description

Technical Field

[0001] The present invention belongs to the technical field of waste gas treatment, and in particular relates to a PDR-RTO device for treating high-concentration VOCs waste gas. Background Art

[0002] Volatile organic compounds (VOCs) are common air pollutants in the industrial sector. Their primary sources are chemical plants, the petrochemical industry, the printing and coating industries, the adhesive tape industry, the circuit board industry, and, more recently, the emerging high-tech semiconductor integrated circuit manufacturing and optoelectronic liquid crystal display industries. Because VOCs are toxic and can easily damage the ozone layer, they must be controlled to prevent harm to the global environment.

[0003] In recent years, fires accounted for approximately 83% of accidents and disasters in industrial areas, chemical leaks for approximately 7%, and explosions for approximately 5%. All three categories of accidents are partially related to VOC chemical leaks. VOC waste gas from chemical plants is generally a multi-component mixture with complex composition, often flammable, explosive, toxic, and odorous. Furthermore, it often exhibits rapid fluctuations in concentration and flow, making it difficult to handle and easily causing damage and loss to property and personnel, as well as pollution to the surrounding environment. Environmental protection authorities and the industry proposed the concept of "zero emissions" many years ago, requiring the collection and treatment of VOC waste gas in the hope of effectively reducing pollution and minimizing the chance of accidents and disasters.

[0004] Currently developed and commercialized VOCs waste gas pollution control equipment technologies include incineration, adsorption, absorption, and condensation methods, which can be basically divided into two types: destructive and non-destructive. Destructive methods include incineration, high temperature, and catalytic oxidation. Under these mechanisms, VOCs are converted into less polluting substances such as CO2 and water or other inert substances. Non-destructive methods, on the other hand, use physical methods such as adsorption, absorption, and condensation to physically remove VOCs from exhaust gases, converting them into clean gas.

[0005] Currently, the commercialized VOCs waste gas treatment technologies are generally classified into the following categories: (1) Low-concentration VOCs waste gas (<10-20 mg / Nm 3 ) Low hazard, easy to handle, most of them are treated by activated carbon adsorption method; (2) Low and medium concentration VOCs waste gas (50-1000 mg / Nm 3 ) Due to the low concentration, the treatment consumes energy, so adsorption concentration / desorption plus RTO or RCO incineration is often used for treatment; (3) Medium concentration VOCs waste gas (500-3,000 mg / Nm 3) are usually treated by thermal incineration or thermal oxidation (RTO); (4) medium to high concentration VOCs waste gas (2,000-5,000 mg / Nm 3 ) are mostly treated by catalytic incineration (RCO) or regenerative thermal oxidation (RTO); (5) high concentration VOCs exhaust gas (>5,000-10,000 mg / Nm 3 ) are treated by post-dilution treatment, flame incineration, condensation, or activated carbon adsorption recovery; (6) High-concentration VOCs waste gas (including instantaneous abnormal emissions) is burned in the air using a high-altitude torch that is easy to cause pollution; (7) If the odor contains medium or low concentrations of sulfur or nitrogen components, it can be treated by chemical washing method.

[0006] Each of the above commonly used treatment methods has its advantages, disadvantages and applicable occasions. In particular, for situations with high VOCs concentrations and high-concentration VOCs waste gas emitted abnormally in an instant, the current commercial treatment methods all adopt a dilution post-treatment method. Therefore, they all have to face the problems of high treatment operation costs and the risk of explosion or fire. Therefore, over the past 100 years, the industry has been accustomed to using high-altitude flares to burn in the air to solve the problem of high-concentration VOCs waste gas.

[0007] Windhorst (2004) reviewed numerous chemical plant accidents and found that many explosions were caused by thermal processing equipment. The underlying cause is typically the accumulation of a flammable VOC waste gas mixture within the equipment, followed by a spark igniting within the confined space. In VOC waste gas treatment equipment, an ignition source is often present to maintain effective combustion temperatures. The three elements of fire—oxygen, flammable gases, and an ignition source—are always present within VOC waste gas treatment systems. Therefore, when designing industrial VOC waste gas treatment equipment, avoiding ignition sources within the equipment is not a reliable safety design principle (Wasileski, 2005 / 2007; Ennis 2004).

[0008] High-temperature oxidation or incineration technologies for VOC waste gas are generally categorized into thermal incineration and catalytic incineration. Based on their energy recovery methods, VOC high-temperature oxidation or incineration facilities can be further divided into two main technologies: recuperative thermal oxidizers (RTOs) and regenerative thermal oxidizers (RTOs). Recuperative thermal oxidizers use a heat exchanger to exchange heat between VOC-containing gases and high-temperature combustion products, recovering the heat generated by the high-temperature combustion products. These oxidizers typically utilize plate heat exchangers for energy recovery, resulting in heat recovery rates typically less than 70%. RTOs, on the other hand, utilize ceramic thermal storage materials to store and recover heat from the high-temperature combustion product exhaust, which is then used alternately to heat the VOC-containing waste gas. RTOs can achieve heat recovery rates exceeding 90% to 95%.

[0009] In thermal incineration of VOCs waste gas, the combustion chamber's flame temperature can reach 1,350-1,500°C. However, the combustion temperature of the mixed gas within the combustion chamber is typically controlled at 800-850°C. The gas residence time is typically 0.3-0.5 seconds, with some equipment designed for residence times exceeding 1.0 seconds. The airflow velocity within the combustion chamber is typically 3-15 m / s. Under these conditions, the removal rate of general odorous substances and VOCs waste gas can typically reach 90-95%, effectively suppressing odor emission and meeting regulatory emission standards. However, for particularly difficult-to-treat VOCs waste gases, such as those from the rubber and resin industries, trace amounts of combustion by-products can create an unpleasant odor. For example, for VOCs organic waste gases from the rubber industry and the petrochemical industry, the operating temperature of the combustion chamber sometimes needs to be adjusted to as high as 1000°C, and the gas residence time is designed to be 1.0 to 2.0 seconds as needed. The airflow velocity must reach 8 to 10 m / s to completely resolve the odor problem.

[0010] A typical regenerative thermal oxidation (RTO) system consists of at least two regenerative beds, air intake control equipment, and heating and temperature control equipment. The regenerative beds are filled with stone or ceramic thermal storage material. The gas to be treated first enters the first regenerative bed (Bed A) to be preheated to a certain temperature. Afterwards, a reaction occurs within the high-temperature oxidation reaction chamber to remove VOCs. The hot gas, after the oxidation reaction, passes through the second regenerative bed (Bed), transferring its heat energy to the previously cooled regenerative material for storage, storing the sensible heat of the hot gas and allowing it to be discharged at a lower temperature. After a certain period of time, a valve is switched, allowing the gas to be directed to the hot bed (Bed) for preheating. The hot gas energy after the reaction is stored in Bed A, completing the operation cycle. However, two-bed regenerative thermal oxidation or incineration systems can suffer from transiently high VOC emission concentrations when switching between regenerative beds, resulting in poor destruction and removal efficiency. Therefore, the RTO equipment is developed into an RTO system containing more than three heat storage beds to suppress the escape of VOCs waste gas generated instantly when the furnace beds are switched.

[0011] The heat recovery rate of a regenerative high-temperature oxidation system (RTO) is generally defined as:

[0012] R=(T c -T o ) / (T c -T i )×100%(1);

[0013] Where T c is the gas oxidation temperature or operating temperature (i.e., maximum oxidation temperature) of the high-temperature oxidation reaction chamber of the thermal regenerative high-temperature oxidation system (i.e., RTO), T o is the outlet temperature of the thermal storage regeneration high temperature oxidation system, T i is the inlet temperature of the VOCs waste gas to be treated. c 、T o 、T i are 800℃, 85℃, and 50℃ respectively, then

[0014] R=(800-85) / (800-50)×100%=95.3%.

[0015] The above calculation example shows that the energy recovery efficiency of RTO itself is 95.3%, which means that the VOCs waste gas to be treated only needs to be heated from the inlet temperature of 50℃ to 35℃ (T o -T i =85-50=35℃) can oxidize the VOCs in the gas. Generally speaking, the thermal regenerative high temperature oxidation system is used to treat waste gas containing VOCs with a concentration greater than 1,500mg / Nm 3The exhaust gas is of a VOCs concentration of about 500ppmv (equivalent to the general VOCs exhaust gas concentration of about 500ppmv). Except for the auxiliary fuel required during startup, no auxiliary fuel or auxiliary electric heating energy supply is required during normal operation.

[0016] The advantage of the thermal regenerative high-temperature oxidation (RTO) system is its high energy recovery efficiency. However, for high-concentration VOCs-containing exhaust gas, traditional thermal regenerative high-temperature oxidation systems are unable to effectively recover and utilize the excess energy released by the oxidation and combustion of VOCs. Therefore, if the VOCs concentration is high, the excess energy cannot be effectively discharged from the thermal regenerative high-temperature oxidation system, which means that there is a risk of temperature runaway causing the RTO to burn or explode.

[0017] In recent years, there have been numerous cases of explosions or incineration in thermal regenerative high-temperature oxidation systems internationally. The primary cause is the inadvertent introduction of high-VOC exhaust gases into the RTO. Improper air supply regulation can lead to deflagration or detonation, or damage caused by overheating. Furthermore, during system shutdown and startup, dilution operations can cause mixed gases to pass through the explosion zone, often resulting in explosion accidents. Therefore, HSE recommends that the VOC exhaust concentration at the RTO inlet be controlled to below 25% of the gas's lower explosion limit (LEL). Based on this HSE recommendation, many existing VOC exhaust gas treatment systems use air to dilute the source VOC exhaust, reducing its concentration to below 25% of the LEL, before treating it as low-concentration VOC exhaust using the RTO. However, since the concentration detection of VOCs waste gas takes about 30 seconds to 2 minutes from extraction, purification, to inspection and data generation, in petrochemical industry applications, an instantaneous change in VOCs waste gas concentration, coupled with a spark, may cause an immediate explosion disaster; and VOCs waste gas concentration detection equipment can usually only tell the operator why the accident occurred after the incident, but cannot remind the operator to take appropriate measures in advance before the disaster occurs, or automatically initiate emergency response measures to avoid the disaster. Therefore, when the industry is faced with high-concentration VOCs waste gas treatment, the method of diluting VOCs waste gas is adopted according to HSE specifications, which almost makes users without exception suffer from backfire, combustion, and even explosion accidents. The present invention is based on solving this difficult problem in the industry and invents a technology without explosion risk, which thoroughly improves the existing VOCs waste gas heat treatment technology and can effectively recover and utilize the energy released by the oxidation and combustion of VOCs waste gas, which is one of the purposes of the present invention.

[0018] The technology adopted by the present invention is the concept of "fighting explosion with explosion". Since the VOCs waste gas is a flammable and explosive substance, the technical concept adopted by the present invention is to use its flammable and explosive characteristics to create a condition that can easily allow this flammable and explosive substance to be detonated in a controllable space. First, the explosive characteristics and power of the VOCs waste gas are eliminated through explosion behavior, and then traditional RTO technology is used to provide conditions for complete oxidation to completely oxidize and destroy the VOCs waste gas. Finally, it is combined with energy recovery equipment to recover its excess energy for use in generating steam recovery, and only the energy required to provide the RTO to meet its heat exchange is retained to ensure that the RTO can operate stably, safely and energy-savingly. This "fighting explosion with explosion" concept utilizes pulse detonation technology (Zhang Rongxing, Taiwan Invention Patent I448657, China Invention Patent ZL 2012 1 0143533.6). Zhang Rongxing has also applied this patented technology to the treatment of flammable and explosive flare gases and high-concentration organic VOC waste gas (Taiwan Patent I504844, China Invention Patent ZL2012 1 0548700.5). However, the implementation of Zhang Rongxing's Taiwan Patent I448657 invention technology is plagued by limited operating range and high-frequency noise generated by subcooling of the surface cooling. Furthermore, Taiwan Patent I448657 poses risks when used on high-concentration organic waste gas containing oxygen within high-concentration VOC waste gas. In addition, Taiwan Patent I448657 uses a metal static stirring turbulence device to create turbulent mixing in the detonation tube. However, this static stirring turbulence device is easily damaged under the repeated impact of the high-temperature detonation shock wave.In order to solve the use risk of Taiwan Patent I448657, Zhang Rongxing proposed an invention patent application for a countercurrent detonation pulse wave reactor without valve control in 2024 (Taiwan, China, application number 113130710), using multiple serially connected reduced diameter pipe sections, expanded diameter pipe sections and straight pipe sections to form a detonation pulse wave reactor tube, and using the change of flow space to create turbulent mixing conditions; then, using multiple gas feeding pipes that can provide gas mixing and terminate the countercurrent detonation pulse wave, and the gas feeding pipe has a flame prevention device inside to optimize the mixing conditions of combustible gas and air or oxygen, and make the gas feeding pipe itself The flame prevention function reduces operational constraints and can stably generate high-temperature detonation pulse waves under various operating conditions, allowing high-concentration VOCs waste gas to undergo oxidation reactions. Furthermore, the outer surface of the detonation pulse wave reactor tube is machined into a porous structure, which enhances surface boiling. Once a detonation shock wave is generated, it instantly causes the reactor tube to rapidly heat up. This porous structure can be used to instantly and comprehensively generate bubbles, causing surface boiling, thereby eliminating the high-frequency noise generated by the instantaneous high-temperature sub-cold boiling of the detonation shock wave reactor tube. Taiwan Patent No. 1504844 places a water-tube boiler within the RTO combustion chamber to recover the RTO's excess energy. However, when VOC concentrations are low, the placement of a water-tube boiler within the RTO combustion chamber can cause the combustion chamber's temperature to drop locally, affecting the effective destruction of VOCs. The present invention proposes a PDR-RTO device and develops an intelligent control technology that combines PDR-RTO with a waste heat recovery boiler to effectively recover energy, so that the PDR-RTO device can simultaneously solve the treatment of high-concentration VOCs waste gas and low-concentration VOCs waste gas.

[0019] Based on the above description, the present invention proposes a treatment device that can simultaneously solve the problems of high-concentration VOCs waste gas and low-concentration VOCs waste gas. The treatment of high-concentration VOCs waste gas is to use its flammable and explosive properties to eliminate its flammable and explosive properties using PDR detonation technology; the treatment of low-concentration VOCs waste gas is to directly use the RTO's air intake pipe to introduce it into the RTO; then, the detonation technology is combined with the RTO and the waste heat recovery boiler to invent a PDR-RTO device for treating high-concentration VOCs waste gas.

[0020] The innovative PDR-RTO equipment proposed in this invention treats high-concentration VOCs waste gas. The PDR utilizes "detonation" technology, which involves igniting a gas mixture of combustible gas and an appropriate amount of air or oxygen within a container. This mixture undergoes rapid flame formation, known as deflagration, which combines with a compression wave ahead of it to generate a shock wave. This sudden increase in the combustion propagation speed, exceeding the speed of sound and stabilizing, is known as detonation. The localized reaction area where the compression generates the shock wave is called the detonation shock wave. After the detonation shock wave passes through, the chemical composition of the gas mixture rapidly changes. If this detonation shock wave impacts material, it not only imparts intense pressure and high temperatures within a very short period of time, but also produces mechanical damage.

[0021] To address the safety and energy recovery challenges associated with treating high-concentration VOCs waste gas, this invention proposes a PDR-RTO device for treating high-concentration VOCs waste gas. This device utilizes high-temperature pulse wave reactor technology (Taiwan Invention Patent Application No. 113130701), thermal oxidation technology, and waste heat recovery technology. Furthermore, it incorporates integrated control technology for safe operation to provide an integrated, innovative, and cost-effective device capable of treating both high- and low-concentration VOCs waste gas and recovering energy. This device addresses long-standing safety concerns in industries such as petrochemicals, refining, plastics, and rubber, while achieving energy conservation, carbon reduction, and environmentally friendly governance (ESG) goals. Summary of the Invention

[0022] The main purpose of the present invention is to provide a PDR-RTO device for treating high-concentration VOCs waste gas, comprising: diverting low-concentration VOCs waste gas and high-concentration VOCs waste gas into the PDR-RTO device; the low-concentration VOCs waste gas is introduced into the RTO device for treating the PDR-RTO device for treating high-concentration VOCs waste gas through the air inlet pipe of the RTO; the high-concentration VOCs waste gas is introduced into the PDR-RTO device for treating high-concentration VOCs waste gas through the PDR; the low-concentration VOCs waste gas is preheated and subjected to high-temperature oxidation treatment through the regenerative bed of the RTO, and the energy generated by combustion is recovered by the regenerative bed, so that the VOCs waste gas can be completely destroyed and treated; the high-concentration VOCs waste gas is introduced into the high-temperature oxidation reaction chamber of the RTO through the PDR (high-temperature pulse wave reactor), the VOCs waste gas is destroyed by detonation, and then completely oxidized at high temperature; the high-temperature waste gas generated by the high-temperature oxidation is regulated and controlled by using the control strategy successfully developed by the present invention to introduce part of the high-temperature waste gas into the waste heat recovery boiler to recover energy and generate steam.

[0023] Because the PDR used in the PDR-RTO equipment of the present invention for treating high-concentration VOCs waste gas utilizes high-temperature detonation technology, its energy density is over 100 million times that of traditional combustion technology, and the velocity within the PDR's detonation tube is as high as over one thousand meters per second (1000m / s), the PDR can withstand instantaneous flow rate changes (typical pipeline flow rate is approximately 10 to 30m / s) and instantaneous concentration changes (0% to 100%) of VOCs waste gas without affecting its safe operation.

[0024] The PDR-RTO equipment for treating high-concentration VOCs waste gas comprises: (1) separating low-concentration VOCs waste gas and high-concentration VOCs waste gas and introducing them into the PDR-RTO equipment, wherein the low-concentration VOCs waste gas is introduced into the PDR-RTO equipment by using the air inlet of the RTO, and the high-concentration VOCs waste gas is introduced into the PDR-RTO equipment by using the PDR; (2) after the low-concentration VOCs waste gas enters the PDR-RTO equipment, it will first be preheated and subjected to high-temperature oxidation treatment by the heat storage bed of the RTO, and the energy generated by combustion will be recovered by another heat storage bed, so that the VOCs waste gas can be completely destroyed and treated; (3) the high-concentration VOCs waste gas is preheated and subjected to high-temperature oxidation treatment by the heat storage bed of the RTO, and the energy generated by combustion will be recovered by using the heat storage bed of the RTO, so that the VOCs waste gas can be completely destroyed and treated; The PDR uses detonation technology to release the explosive energy of VOCs and then introduces it into the high-temperature oxidation reaction chamber of the RTO; the high-concentration VOCs exhaust gas is destroyed by detonation and then completely oxidized by the high-temperature oxidation reaction chamber of the RTO. Part of the high-temperature exhaust gas generated by the high-temperature oxidation reaction chamber is used to recover energy and generate steam using the waste heat recovery boiler. Part of the high-temperature exhaust gas generated by the high-temperature oxidation reaction chamber is used to heat the aforementioned other heat storage bed to recover the energy generated by combustion; (4) The RTO contains at least three or more heat storage beds, and each heat storage bed has a ceramic heat storage bed formed by stacking ceramic heat storage materials, and a VOCs exhaust gas inlet valve and a valve are provided under each ceramic heat storage bed. Cleaning exhaust valve and a combustion exhaust valve; (5) a high-temperature oxidation reaction chamber, located above the heat storage bed and combined with each heat storage bed; multiple groups of PDR high-temperature pulse wave reactors are provided on the wall of the high-temperature oxidation reaction chamber to provide high-concentration VOCs waste gas destruction treatment, and multiple groups of burners; (6) the waste heat recovery boiler is provided with a lower header, an upper header and a group of waste heat recovery boiler pipe rows, which are placed sideways next to the high-temperature oxidation reaction chamber, and the waste heat recovery boiler outlet control valve is used to adjust the gas flow entering the waste heat recovery boiler for energy recovery and steam generation; (7) a steam drum is provided above the waste heat recovery boiler, which is connected to the upper header of the waste heat recovery boiler, and steam is generated. The steam drum is provided with a vapor-liquid separation device for collecting steam generated by the waste heat recovery boiler tube bank and supplying steam; (8) The RTO heat storage bed utilizes the switching of the VOCs waste gas inlet valve, the cleaning exhaust valve and the combustion waste gas exhaust valve to alternately serve as an air inlet heating tank, a purification tank and an exhaust energy recovery tank; and at least one of the heat storage beds is used as a purification tank, and the others are used as VOCs waste gas inlet heating tank and combustion waste gas exhaust energy recovery tank respectively; (9) In the RTO, the VOCs waste gas first flows through the VOCs waste gas inlet heating tank, and is heated by the heated ceramic heat storage bed to raise the temperature to above its autoignition temperature (Auto Ignition Temperature), and then enters the high-temperature oxidation reaction chamber for oxidation reaction; after use, the VOCs waste gas inlet heating tank is converted into a purification tank, and the clean gas after combustion in the high-temperature oxidation reaction chamber is extracted by the cleaning windmill and backwashed into the ceramic heat storage bed used as the purification tank; after cleaning, the purification tank is switched to the combustion waste gas exhaust energy recovery tank;(10) Before the cleaning of the purification tank, it is used as a VOCs waste gas feed tank. Therefore, the gas backwashed to clean the purification tank will contain diluted low-concentration VOCs waste gas, which is transported to the PDR through the cleaning windmill and used as the detonation batching air of the PDR or / and the secondary air of the PDR; (11) The low-concentration VOCs waste gas introduced into the PDR-RTO equipment through the RTO and the high-concentration VOCs waste gas introduced into the PDR-RTO equipment through the PDR undergo oxidation reaction in the high-temperature oxidation reaction chamber of the RTO, and the high-temperature waste gas generated is partially directed to the waste heat recovery boiler The high-temperature exhaust gas discharged from the high-temperature oxidation reaction chamber is subjected to energy recovery in the exhaust energy recovery tank, and the heat is stored in the ceramic heat storage bed of the exhaust energy recovery tank, and then discharged from the combustion exhaust gas exhaust valve, and extracted by the induced fan and sent to the chimney for discharge; (12) The high-temperature exhaust gas directed to the waste heat recovery boiler for energy recovery to generate steam is regulated by the flow control valve at the outlet of the waste heat recovery boiler; the opening ratio of the flow control valve is dynamically adjusted by the outlet temperature change potential of the RTO combustion exhaust gas exhaust valve.

[0025] In order to provide a better understanding of the present invention, a preferred embodiment of the present invention is described below with reference to the following drawings as examples. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 Schematic diagram of the mixing of high-concentration VOCs waste gas and low-concentration VOCs waste gas in the present invention;

[0027] Figure 2 This is a schematic diagram of an embodiment of a PDR-RTO device for treating high-concentration VOCs waste gas in the present invention;

[0028] Figure 3 Schematic diagram of the operation cycle of the PDR-RTO equipment for treating high-concentration VOCs waste gas in the present invention;

[0029] Figure 4 Schematic diagram of the operation cycle of the PDR-RTO equipment for treating high-concentration VOCs waste gas in the present invention;

[0030] Figure 5 Schematic diagram of the operation cycle of the PDR-RTO equipment for treating high-concentration VOCs waste gas in the present invention;

[0031] Figure 6 Schematic diagram of the PDR high-temperature pulse wave reactor used in the PDR-RTO equipment for treating high-concentration VOCs waste gas in the present invention;

[0032] Figure 7 This is a schematic diagram of the working principle of the PDR high-temperature pulse wave reactor used in the PDR-RTO equipment for treating high-concentration VOCs waste gas in the present invention;

[0033] Figure 8 Schematic diagram of temperature changes of the PDR-RTO equipment for treating high-concentration VOCs waste gas in the present invention;

[0034] Description of reference numerals:

[0035] 1. PDR-RTO equipment for treating high-concentration VOCs waste gas;

[0036] 2RTO equipment;

[0037] 3. Waste heat recovery boiler;

[0038] 10 first heat storage bed;

[0039] 11. Air inlet chamber of the first heat storage bed;

[0040] 12 a ceramic heat storage bed of the first heat storage bed;

[0041] 13. Gas mixing chamber of the first regenerator bed;

[0042] 14 refractory furnace wall of the first regenerator bed;

[0043] 15. Flame arrester at the entrance of the first regenerator bed;

[0044] 20 second heat storage bed;

[0045] 21 air inlet chamber of the second heat storage bed;

[0046] 22 ceramic heat storage bed of the second heat storage bed;

[0047] 23 gas mixing chamber of the second regenerator bed;

[0048] 24 refractory furnace wall of the second regenerator bed;

[0049] 25. Flame arrester at the entrance of the second regenerator bed;

[0050] 30 third heat storage bed;

[0051] 31 the air inlet chamber of the third heat storage bed;

[0052] 32 ceramic heat storage bed of the third heat storage bed;

[0053] 33 gas mixing chamber of the third regenerative bed;

[0054] 34 refractory furnace wall of the third regenerator bed;

[0055] 35: flame arrester at the entrance of the third regenerator bed;

[0056] 40 high temperature oxidation reaction chamber;

[0057] 41 refractory furnace wall of high temperature oxidation reaction chamber;

[0058] 42 the interior of the high temperature oxidation reaction chamber;

[0059] 43 high temperature oxidation reaction chamber temperature controller;

[0060] 44 high temperature oxidation reaction chamber bypass pipe;

[0061] 50 auxiliary fuel;

[0062] 51 fuel supply lines;

[0063] 52 fuel control valve;

[0064] 53 fuel flow controller;

[0065] 54 Combustion air-fuel ratio calculation;

[0066] 56 burners;

[0067] 60 combustion air;

[0068] 61 Combustion air windmill;

[0069] 62 combustion air control valve;

[0070] 63 combustion air pipeline;

[0071] 64 combustion air flow controller;

[0072] 70 high concentration VOCs exhaust gas;

[0073] 71 High-concentration VOCs exhaust gas variable frequency booster fan;

[0074] 72 Detonation-proof flame arrester;

[0075] 73 High concentration VOCs exhaust gas flow controller;

[0076] 74 high-concentration VOCs exhaust pipeline;

[0077] 75 high concentration VOCs exhaust gas pressure controller;

[0078] 76 High concentration VOCs exhaust gas proportioning air flow controller;

[0079] 77 Proportional Air Flow Calculator;

[0080] 78 proportioning air line;

[0081] 79 proportioning air flow regulating valve;

[0082] 80PDR high temperature pulse wave reactor;

[0083] 81PDR secondary air distribution chamber;

[0084] 100 low-concentration VOCs waste gas;

[0085] 101 low-concentration VOCs waste gas inlet pipeline;

[0086] 102 low concentration VOCs exhaust gas inlet valve;

[0087] 103 low-concentration VOCs exhaust gas bypass pipeline;

[0088] 104 low concentration VOCs waste gas bypass valve;

[0089] 105 low concentration VOCs exhaust gas bypass;

[0090] 106 bypass air regulating valve;

[0091] 107 bypass air line;

[0092] 108 first heat storage bed air inlet valve;

[0093] 109 second heat storage bed air inlet valve;

[0094] 110 third heat storage bed air inlet valve;

[0095] 111 bypass air;

[0096] 112 Cleaning the windmill;

[0097] 113 The main lure windmill;

[0098] 114 chimneys;

[0099] 115 first thermal storage bed exhaust valve;

[0100] 116 second thermal storage bed exhaust valve;

[0101] 117 third thermal storage bed exhaust valve;

[0102] 118 The first heat storage bed cleans the exhaust valve;

[0103] 119 The second heat storage bed cleans the exhaust valve;

[0104] 120 The third heat storage bed cleans the exhaust valve;

[0105] 121VOCs waste gas inlet pipe;

[0106] 122VOCs waste gas inlet manifold;

[0107] 123 first heat storage bed inlet pipe;

[0108] 124 second heat storage bed inlet pipe;

[0109] 125 The third heat storage bed enters the air pipe;

[0110] 131 first heat storage bed exhaust pipe;

[0111] 132 second thermal storage bed exhaust pipe;

[0112] 133 third heat storage bed exhaust pipe;

[0113] 134 thermal storage bed exhaust manifold;

[0114] 135 export pipeline;

[0115] 136 Main attractor windmill outlet pipeline;

[0116] 137 Regenerative bed exhaust manifold temperature controller;

[0117] 138 flow control valve;

[0118] 141 The first regenerator bed cleans the exhaust pipe;

[0119] 142 The second regenerator bed cleans the exhaust pipe;

[0120] 143 The third regenerator bed cleans the exhaust pipe;

[0121] 144 Regenerator bed cleans exhaust manifold;

[0122] 145 Regenerative Bed Cleaning Exhaust Pipeline;

[0123] 146 Clean the exhaust manifold;

[0124] 200 deionized water;

[0125] 201 deionized water supply pipeline;

[0126] 202 degassing tank;

[0127] 203 deionized water supply pump;

[0128] 204 deionized water supply flow controller;

[0129] 205 deionized water supply flow control valve;

[0130] 206 deionized water supply line;

[0131] 207 boiler water preheating tube bank;

[0132] 208 boiler water pipeline;

[0133] 209 boiler water preheater;

[0134] 220 lower header;

[0135] 221 upper header;

[0136] 222 waste heat recovery boiler tube bank;

[0137] 223 waste heat recovery boiler room;

[0138] 224 riser;

[0139] 225 downcomer;

[0140] 230 steam drums;

[0141] 231 gas-liquid separation device;

[0142] 232 steam drum level controller;

[0143] 240 steam lines;

[0144] 241 Steam drum pressure controller;

[0145] 242 steam flow regulating valve;

[0146] 244 steam flow controller;

[0147] 245 steam;

[0148] 812 high concentration VOCs waste gas feed pipe;

[0149] 814 High-concentration VOCs exhaust gas feed mixing chamber;

[0150] 816 high concentration VOCs waste gas feeding section;

[0151] 817 flame arrester core;

[0152] 818 flame arrester;

[0153] 819 multi-hole fixing fixture;

[0154] 820 fixed end plate of high concentration VOCs exhaust gas dispersion feed pipe;

[0155] 822 high concentration VOCs waste gas dispersion feed pipe;

[0156] 824 High-concentration VOCs exhaust gas dispersion feed pipe internal flame prevention structure;

[0157] 830 combustion air / low concentration VOCs exhaust gas;

[0158] 832 combustion air / low concentration VOCs exhaust gas feed pipe;

[0159] 834 Combustion air / low concentration VOCs exhaust gas feed mixing and distribution room;

[0160] 840 combustion air / low concentration VOCs exhaust gas feeding section;

[0161] 850 detonation pulse wave reactor tube end plate;

[0162] 860 detonation pulse wave reactor body;

[0163] 862 cooling facilities;

[0164] 866 detonation pulse wave reactor tube;

[0165] 870 detonation booster;

[0166] 871 reduced diameter pipe section;

[0167] 872 expanded diameter pipe section;

[0168] 873 straight pipe section;

[0169] 875 cooling water inlet;

[0170] 876 cooling water outlet;

[0171] 880 ignition device group;

[0172] 890 detonation pulse wave reactor outlet section;

[0173] 892 secondary vortex air jacket;

[0174] 894 pulse nozzle;

[0175] 896RTO connecting flange;

[0176] 900 reaction products. DETAILED DESCRIPTION

[0177] In order to make the objectives, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below in conjunction with specific embodiments and with reference to the accompanying drawings.

[0178] High-concentration VOCs waste gas (Volatile Organic Compounds, VOCs) generated by the petrochemical, refining, chemical, plastics, rubber, storage and transportation industries is inherently flammable and explosive. In addition, some emergency discharge valves emit VOCs waste gas at irregular intervals, resulting in rapid changes in concentration and flow. For over a hundred years, this high-concentration VOCs waste gas has been treated by flaring. It is one of the main sources of environmental pollution and large-scale carbon emissions caused by the petrochemical, refining, chemical, plastics, rubber, storage and transportation industries.

[0179] The present invention adopts detonation technology to solve the flammable and explosive characteristics of high-concentration VOCs waste gas, and combines RTO (Regenerative Thermal Oxidizer) and waste heat recovery boiler to invent a PDR-RTO device for treating high-concentration VOCs waste gas, comprising diverting low-concentration VOCs waste gas and high-concentration VOCs waste gas into the PDR-RTO device, wherein the low-concentration VOCs waste gas is introduced into the PDR-RTO device by RTO, and the high-concentration VOCs waste gas is introduced into the PDR-RTO device by PDR; the low-concentration VOCs waste gas is preheated by the RTO regenerative bed, subjected to high-temperature oxidation treatment, and the energy generated by combustion is recovered by the regenerative bed, so that VOCs VOCs exhaust gas is completely destroyed and treated. High-concentration VOCs exhaust gas is introduced into the high-temperature oxidation chamber of the RTO via a PDR (Pulsed Wave Reactor). After being destroyed by detonation, the VOCs are then completely oxidized at high temperatures. A portion of the high-temperature exhaust gas is recovered in a waste heat recovery boiler to generate steam. Because PDR utilizes high-temperature detonation technology, its energy density is over 100 million times that of traditional combustion technologies. With velocities exceeding one kilometer per second within the PDR's detonation tube, the PDR can withstand transient fluctuations in VOC flow and concentration without compromising safe operation. This PDR-RTO system allows VOCs to be completely destroyed within the device, while recovering the energy generated by high-altitude flaring. This energy recovery reduces the significant equipment investment and operating costs. This PDR-RTO system is effectively applicable to VOCs exhaust gas treatment in various industries, including the chemical, petrochemical, pharmaceutical, and semiconductor industries.

[0180] Before explaining the main application of the present invention, we can use an explosion accident in a polystyrene factory [Walsileski 2005, 2007] to illustrate the industrial necessity of the present invention. The user in this case is a polystyrene production unit. Basically, the granular polystyrene solid (SPS) is produced by polymerizing styrene monomer, and then impregnated with isopentane (C5H 12) is processed into expanded polystyrene (EPS) production plant. When this enterprise was considering building its VOCs waste gas treatment equipment, the factory had considered the following equipment: direct-fired incinerator (DFTO), reheat incinerator, regenerative thermal incinerator (RTO), regenerative catalytic incinerator (RCO), and finally, considering the rapid changes in system concentration, the factory accepted the manufacturer's suggestion to dilute the VOCs gas and then use RCO for treatment. When the company was designing the equipment, the design basis took into account several possible sources of waste gas and operating conditions. The average flow rate, maximum flow rate, average concentration and maximum concentration of the gas were taken into account at the time of design, and the design basis of RCO was formulated based on these basic data. In this case, the two gases discharged from the reactor contained a higher concentration of VOCs isopentane (C5H 12 ), the other gases are nitrogen for protection against explosion. This type of VOCs gas belongs to high-concentration VOCs waste gas (HVOC); there are three other low-concentration VOCs gases, which are basically VOCs isopentane (C5H 12 ) trace polluted air, that is, low-concentration VOCs exhaust gas (LVOC). The lower explosion limit concentration of isopentane is 1.4%, and the upper explosion limit concentration is 7.6%. If the internal gas concentration in any pipeline or equipment is within this range, extreme caution must be exercised. In addition, HVOC is a small flow rate. Although the flow rate accounts for about 3% of the total flow, its concentration has exceeded that of isopentane (C5H 12 ) has a lower explosion limit of 1.4%. LVOC is a high flow rate, and basically the concentration is below 25% of the lower explosion limit. The design unit believes that it is safe to transport the gas in the pipeline. Based on the above analysis of VOCs exhaust gas flow and concentration data, the design engineer believes that since the HVOC flow rate only accounts for 3%, if a mixing tank is designed to introduce HVOC and LVOC into the mixing tank for mixing, and the mixing tank is equipped with a nitrogen exhaust design to ensure safety, then the VOCs concentration at the outlet of the mixing tank is only 0.24-0.3% according to his calculations, which is still lower than 25% of the LEL, that is, 0.37% (LEL=1.4%). The design engineer believes that this design complies with the HSE design guidelines and is considered a safe design after review. Therefore, according to this design concept, the gas mixing point of the VOCs exhaust gas treatment system of this polystyrene plant is as follows Figure 1As shown. During the system design phase, the planning team was concerned that the mixture curve would pass through the explosion range. However, the design team determined that the concentration of the gases would be well below the lower explosion limit after mixing in the mixing tank. Furthermore, the gases were already fully mixed before entering the baghouse, where there were no ignition sources and a considerable distance from the RCO. Furthermore, with the presence of a wind turbine, they believed the RCO flame would not penetrate the wind turbine and ignite the gases in the mixing tank ahead of the baghouse. Therefore, they determined that the system design would not pose an explosion risk. After the equipment was completed and tested, low-concentration VOC waste gas (LVOC) was first introduced. The system successfully started up and operated stably. After a period of operation with the LVOC, the decision was made to introduce HVOC. However, upon the introduction of the first stream of HVOC, the combustion chamber instantly shut down, and the safety interlock system automatically closed the dual valves in the VOC waste gas line. The combustible gases in the combustion chamber then spontaneously ignited, resulting in a combustion and explosion trip. After the explosion and trip, the control personnel, following safety guidelines, activated the blower to purge the combustion chamber. The operator then pressed the RESET button on the combustion system to restart the burner, causing an explosion and damaging the RCO equipment. Similar designs and operating methods are widely used in industry, but they have also repeatedly resulted in serious explosions.

[0181] The main purpose of the present invention is to provide a PDR-RTO device 1 for treating high-concentration VOCs waste gas. Figure 2 As shown, the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas includes: an RTO equipment 2, a waste heat recovery boiler 3, and a plurality of PDR high-temperature pulse wave reactors 80 installed on the high-temperature oxidation reaction chamber 40 of the RTO equipment 2.

[0182] In the PDR-RTO device 1 for treating high-concentration VOCs waste gas, the low-concentration VOCs waste gas 100 and the high-concentration VOCs waste gas 70 are separated and introduced into the PDR-RTO device 1 for treating high-concentration VOCs waste gas, wherein the low-concentration VOCs waste gas 100 is introduced into the RTO device 2 via the low-concentration VOCs waste gas inlet pipeline 101 of the RTO device 2; and the high-concentration VOCs waste gas 70 is introduced into the high-temperature oxidation reaction chamber 40 of the RTO device 2 via the PDR high-temperature pulse wave reactor 80;

[0183] In the PDR-RTO device 1 for treating high-concentration VOCs waste gas, low-concentration VOCs waste gas 100 is preheated by the ceramic heat storage bed 12 of the first heat storage bed, the ceramic heat storage bed 22 of the second heat storage bed, or the ceramic heat storage bed 32 of the third heat storage bed of the RTO device 2, and undergoes high-temperature oxidation treatment in the high-temperature oxidation reaction chamber 40 of the RTO device 2. The energy generated by combustion is recovered by using the ceramic heat storage bed 12 of the first heat storage bed, the ceramic heat storage bed 22 of the second heat storage bed, or the ceramic heat storage bed 32 of the third heat storage bed, so that the low-concentration VOCs waste gas 100 can be completely destroyed and treated, and the purpose of effectively recovering energy is achieved by alternating switching of the heat storage beds.

[0184] In the PDR-RTO device 1 for treating high-concentration VOCs waste gas, the high-concentration VOCs waste gas 70 is introduced into the high-temperature oxidation reaction chamber 40 of the RTO device 2 via the PDR high-temperature pulse wave reactor 80; after the high-concentration VOCs waste gas 70 is destroyed by detonation in the PDR high-temperature pulse wave reactor 80, its explosive power is eliminated, and then it is thoroughly oxidized at high temperature in the high-temperature oxidation reaction chamber 40 of the RTO device 2. Part of the high-temperature waste gas generated in the high-temperature oxidation reaction chamber 40 is reused in the waste heat recovery boiler 3 to recover energy and generate steam 245.

[0185] In the RTO device 2 in the PDR-RTO device 1 for treating high-concentration VOCs waste gas, the operating temperature of its high-temperature oxidation reaction chamber 40 is controlled by the high-temperature oxidation reaction chamber temperature controller 43 installed in the high-temperature oxidation reaction chamber 40, which controls the combustion air flow controller 64 installed in the combustion air pipeline 63 in a PID control mode to adjust and control the combustion air control valve 62 for air-leading mode fuel control; then, the output of the combustion air flow controller 64 is cascade-controlled to control the fuel flow controller 53 installed in the fuel supply pipeline 51, which is used to adjust the combustion air-fuel ratio calculation 54 to control the fuel control valve 52 to adjust the fuel supply, so that the burner 56 of the high-temperature oxidation reaction chamber 40 of the RTO device 2 can adjust and control the temperature of the high-temperature oxidation reaction chamber 40 of the RTO device 2.

[0186] The operating temperature of the high-temperature oxidation reaction chamber 40 of the RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas is monitored by a high-temperature oxidation reaction chamber temperature controller 43 installed in the high-temperature oxidation reaction chamber 40. Only when the temperature of the high-temperature oxidation reaction chamber 40 is higher than the auto-ignition temperature of the low-concentration VOCs waste gas 100, the low-concentration VOCs waste gas 100 is allowed to be introduced from the RTO device 2 into the PDR-RTO device 1 for treating high-concentration VOCs waste gas.

[0187] The oxidation temperature of the high-temperature oxidation reaction chamber 40 of the RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas is monitored by a high-temperature oxidation reaction chamber temperature controller 43 installed in the high-temperature oxidation reaction chamber 40. Only when the temperature of the high-temperature oxidation reaction chamber 40 is higher than the auto-ignition temperature of the high-concentration VOCs waste gas 70, the high-concentration VOCs waste gas 70 is allowed to be introduced into the PDR-RTO device 1 for treating high-concentration VOCs waste gas from the PDR high-temperature pulse wave reactor 8.

[0188] The RTO device 2 in the PDR-RTO device 1 for treating high-concentration VOCs exhaust gas includes at least three or more regenerator beds, such as a first regenerator bed 10, a second regenerator bed 20, and a third regenerator bed 30. Each regenerator bed includes an air inlet chamber, a ceramic regenerator bed formed by stacking ceramic regenerator materials, and a regenerator bed gas mixing chamber. For example, the first regenerator bed 10 includes a first regenerator bed air inlet chamber 11, a first regenerator bed ceramic regenerator bed 12, a first regenerator bed gas mixing chamber 13, and a first regenerator bed refractory furnace wall 14. The second regenerator bed 20 includes an air inlet chamber 21 for the second regenerator bed, a ceramic regenerator bed 22 for the second regenerator bed, an air mixing chamber 23 for the second regenerator bed, and a refractory furnace wall 24 for the second regenerator bed; the third regenerator bed 30 includes an air inlet chamber 31 for the third regenerator bed, a ceramic regenerator bed 32 for the third regenerator bed, an air mixing chamber 33 for the third regenerator bed, and a refractory furnace wall 34 for the third regenerator bed; and a group of VOCs waste gas inlet valves, a group of cleaning exhaust valves, and a group of combustion waste gas exhaust valves are provided under each ceramic regenerator bed; for example, in the first A first thermal storage bed air inlet valve 108, a first thermal storage bed cleaning exhaust valve 118 and a first thermal storage bed exhaust valve 115 are provided below the first thermal storage bed 10; a second thermal storage bed air inlet valve 109, a second thermal storage bed cleaning exhaust valve 119 and a second thermal storage bed exhaust valve 116 are provided below the second thermal storage bed 20; a third thermal storage bed air inlet valve 110, a third thermal storage bed cleaning exhaust valve 120 and a third thermal storage bed exhaust valve 117 are provided below the third thermal storage bed 30; a VOCs waste gas inlet valve and a thermal storage bed air inlet valve below each ceramic thermal storage bed are provided. An inlet flame arrester is provided between the heat storage bed and the air inlet valve 108 to facilitate the introduction of low-concentration VOCs exhaust gas, so that the maximum concentration allowed is 50% of the LEL; for example, an inlet flame arrester 15 of the first heat storage bed is provided between the bottom of the first heat storage bed 10 and the first heat storage bed air inlet valve 108; an inlet flame arrester 25 of the second heat storage bed is provided between the bottom of the second heat storage bed 20 and the second heat storage bed air inlet valve 109; and an inlet flame arrester 35 of the third heat storage bed is provided between the bottom of the third heat storage bed 30 and the third heat storage bed air inlet valve 110.

[0189] The RTO device 2 in the PDR-RTO device 1 for treating high-concentration VOCs waste gas includes a high-temperature oxidation reaction chamber 40, which is located above the first heat storage bed 10, the second heat storage bed 20 and the third heat storage bed 30 and is combined with the first heat storage bed 10, the second heat storage bed 20 and the third heat storage bed 30; the high-temperature oxidation reaction chamber 40 is covered by a high-temperature oxidation reaction chamber refractory furnace wall 41, so that the interior 42 of the high-temperature oxidation reaction chamber inside can be covered with insulation material, which is not easy to cause heat loss; a plurality of PDR high-temperature pulse wave reactors 80 are provided on the side walls of the high-temperature oxidation reaction chamber 40 to provide destruction treatment for high-concentration VOCs waste gas 70 and a plurality of burners 54.

[0190] The waste heat recovery boiler 3 in the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas comprises a lower header 220, an upper header 221, a set of waste heat recovery boiler pipes 222, and a waste heat recovery boiler chamber 223, which is positioned adjacent to the high-temperature oxidation reaction chamber 40. The flow rate of gas flowing through the waste heat recovery boiler 3 is regulated by a flow control valve 138 on an outlet pipeline 135 of a boiler water preheater 209 below the waste heat recovery boiler chamber 223, utilizing the temperature change potential of a heat storage bed exhaust manifold temperature controller 137 located on the outlet heat storage bed exhaust manifold 134 of the first heat storage bed exhaust valve 115, the second heat storage bed exhaust valve 116, and the third heat storage bed exhaust valve 117 below the heat storage beds 12, 22, and 32. This utilizes the excess energy within the high-temperature oxidation reaction chamber 40 of the RTO equipment 2 in the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas to be recovered by the waste heat recovery boiler 3 for steam generation.

[0191] The present invention develops a unique control strategy among the RTO device 2, the waste heat recovery boiler 3, and the multiple PDR high-temperature pulse wave reactors 80 installed on the high-temperature oxidation reaction chamber 40 of the PDR-RTO device 1 that constitutes a PDR-RTO device for treating high-concentration VOCs waste gas. In response to the high-concentration VOCs waste gas introduced into the system by the multiple PDR high-temperature pulse wave reactors 80, the temperature variation potential of the aforementioned heat storage bed exhaust manifold temperature controller 137 is used to control the flow control valve 138 on the outlet pipeline 135 of the boiler water preheater 209 below the waste heat recovery boiler compartment 223 to adjust the gas flow through the waste heat recovery boiler 3. The excess energy in the high-temperature oxidation reaction chamber 40 of the RTO device 2 is recovered by the waste heat recovery boiler 3 to generate steam. Since the temperature displayed by the heat storage bed exhaust manifold temperature controller 137 of the heat storage bed exhaust manifold 134 at the outlet of the RTO device 2 will dynamically rise and fall periodically, as shown in FIG. Figure 8 As shown, this temperature change cannot be used to directly determine and control the opening adjustment of the flow control valve 138 on the outlet pipeline 135 of the boiler water preheater 209 below the waste heat recovery boiler compartment 223. However, a careful analysis Figure 8The cyclical temperature changes can reveal the rate of change and the speed at which the rated maximum temperature is reached, generating a trend that can be digitized through Fourier transform into a temperature change potential. This quantified indicator of temperature change potential, combined with expert rule judgment, serves as a basis for adjusting the opening of flow control valve 138 on the outlet pipeline 135 of boiler water preheater 209 below waste heat recovery boiler compartment 223. This helps achieve a dynamic energy balance for the PDR-RTO system 1 treating high-concentration VOCs exhaust gas, regulates the load of waste heat recovery boiler 3, and maximizes the energy recovery efficiency of the system. When the temperature change potential changes, the percentage increase or decrease in the temperature change potential within a period of dynamic cyclical temperature change serves as the set value for increasing or decreasing the opening of flow control valve 138. The thermal storage bed exhaust manifold temperature controller 137 of the thermal storage bed exhaust manifold 134 adjusts the opening of flow control valve 138 using PID control mode.

[0192] The waste heat recovery boiler 3 includes a steam drum 230 located above the waste heat recovery boiler compartment 223 and connected to the upper header 221 of the waste heat recovery boiler 3. The steam drum 230 contains a gas-liquid separator 231, connected to the upper header 221 via an ascending pipe 224 to collect saturated steam and hot water generated by the waste heat recovery boiler tube banks 222. The steam drum 230 is connected to the lower header 220 via a downcomer 225 to supply boiler feed water to the waste heat recovery boiler tube banks 222. A steam drum pressure controller 241 is located above the steam drum 230. This controller regulates a steam flow control valve 242 located on a steam pipeline 240 connected to the steam drum 230 outlet, adjusting the flow rate of the supplied steam 245 and effectively controlling the operating pressure of the waste heat recovery boiler 3.

[0193] Because high-VOC exhaust gas often experiences dramatic, instantaneous fluctuations in flow and concentration, the waste heat recovery boiler 3 of the PDR-RTO system 1 treating high-VOC exhaust gas must be able to withstand the rapid energy supply fluctuations caused by these transient changes in flow and concentration of high-VOC exhaust gas entering the system. This in turn generates rapidly fluctuating boiler loads, necessitating real-time and rapid steam drum 230 liquid level control in the steam drum 230 of the waste heat recovery boiler 3. The steam drum 230 liquid level of the waste heat recovery boiler 3 utilizes a three-component control mode. This mode utilizes the output of a steam flow controller 244 provided on the steam outlet line 240 of the steam drum 230 as a feedback condition, the output of a boiler feedwater flow controller 204 provided on the boiler feedwater line 206 as a feedforward condition, and the liquid level controller 232 on the steam drum 230 as a liquid level control compensation condition. This ternary control mode utilizes automated software to intelligently regulate the boiler feedwater flow control valve 205 to effectively control the rapidly fluctuating steam drum 230 liquid level.

[0194] The heat storage bed 12, heat storage bed 22 and heat storage bed 32 of the RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas respectively use the switching of the air inlet valve 108, the air inlet valve 109, and the air inlet valve 110, the cleaning exhaust valve 118, the cleaning exhaust valve 119, the cleaning exhaust valve 120 and the exhaust valve 115, the exhaust valve 116 and the exhaust valve 117 to alternately serve as an air inlet heating tank, a purification tank and an exhaust energy recovery tank, and at least one of the heat storage beds is used as a clean air heating tank. The heat storage bed 10 is used as an air intake tank, the heat storage bed 20 is used as a cleaning exhaust tank, and the heat storage bed 30 is used as an exhaust tank; the heat storage bed 10 is used as a cleaning exhaust tank, the heat storage bed 20 is used as an exhaust tank, and the heat storage bed 30 is used as an air intake tank; the heat storage bed 10 is used as an exhaust tank, the heat storage bed 20 is used as an exhaust tank, and the heat storage bed 30 is used as an air intake tank; the heat storage bed 10 is used as an exhaust tank, the heat storage bed 20 is used as an air intake tank, and the heat storage bed 30 is used as a cleaning exhaust tank; and the above three cycles are repeated.

[0195] In each cycle of switching the thermal storage bed within the RTO unit 2 of a PDR-RTO system 1 treating high-VOC exhaust gas, a fixed switching time or achieving a target exhaust temperature can be used as a switching indicator. The RTO unit valve switching operation cycle lasts for a specific duration of 60 to 600 seconds. Since the PDR-RTO device 1 for treating high-concentration VOCs waste gas will have irregularly discharged high-concentration VOCs waste gas 70 with unstable concentration in the high-temperature oxidation reaction chamber 40 of its RTO device 2, which will be destroyed by explosion in the PDR device 80 and then completely oxidized at high temperature in the high-temperature oxidation reaction chamber 40 of the RTO device 2, there will be irregular excess energy in the high-temperature oxidation reaction chamber 40 of the RTO device 2, which needs to be recovered from the waste heat recovery boiler 3 to generate steam 245. The flow rate of the steam 245 needs to be controlled by adjusting the flow control valve 138 on the outlet pipeline 135 of the boiler water preheater 209 below the waste heat recovery boiler compartment 223 by controlling the temperature change potential of the temperature controller 137 on the outlet pipeline 134 of the exhaust valves 115, 116, and 117 below the heat storage beds 12, 22, and 32. The temperature controller 137's potential for change is determined by the rate of change in the time required for the temperature controller 137 to reach the set temperature for each cycle of thermal bed switching. This potential is then used to adjust the opening of the control valve 138 on the outlet pipeline 135 of the boiler water preheater 209 to effectively remove excess energy. Because the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas of the present invention includes a waste heat recovery boiler 3 for excess energy removal, it can discharge excess energy from the high-temperature oxidation reaction chamber 40 of the RTO equipment 1. Therefore, the specific duration of the valve switching operation cycle of the RTO equipment 1 can typically be extended to 180 to 900 seconds, with typical operation ranging from 300 to 600 seconds.

[0196] In each cycle of switching the function of the heat storage bed in the RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas, the low-concentration VOCs waste gas 100 first flows through the air inlet heating tank (10, 20, 30), and is heated by the ceramic material (210, 211, 212) in the heated ceramic heat storage bed (12, 22, 32) to increase the temperature to above its autoignition temperature (AutoIgnition Temperature), and then enters the high-temperature oxidation reaction chamber 40 for oxidation reaction; after use, the air inlet heating tank is converted into a purification tank, and the clean gas after combustion in the high-temperature oxidation reaction chamber 40 is extracted by the cleaning windmill 112, and is backwashed to clean the ceramic heat storage bed serving as the purification tank; after cleaning, the purification tank is switched to an exhaust energy recovery tank.

[0197] Taking the RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs exhaust gas with three thermal storage beds as an example, the typical operating cycle of the RTO device 2 can be divided into three operating cycles by sequentially switching the air inlet valve, the purge exhaust valve, and the exhaust valve, as shown in Table 1 below:

[0198] Table 1

[0199]

[0200] In the above table, "Inlet air heating" means that the thermal storage bed of RTO equipment 2 is used as an inlet air heating tank. For the corresponding thermal storage bed, the inlet valve needs to be opened, the cleaning exhaust valve needs to be closed, and the exhaust valve needs to be closed; "Purification" means that the thermal storage bed of RTO equipment 2 is used as a purification tank. For the corresponding thermal storage bed, the inlet valve needs to be closed, the cleaning exhaust valve needs to be opened, and the exhaust valve needs to be closed; "Energy recovery" means that the thermal storage bed of RTO equipment 2 is used as an exhaust energy recovery tank. For the corresponding thermal storage bed, the inlet valve needs to be closed, the cleaning exhaust valve needs to be closed, and the exhaust valve needs to be opened.

[0201] In the three cycle operations of the above-mentioned RTO equipment 2, the gas used to backwash and clean the purification tank contains low-concentration VOCs waste gas, which is transported to the secondary air distribution chamber 81 of multiple groups of PDR high-temperature pulse wave reactors 80 through the cleaning windmill 112 and used as the detonation feed air of the PDR high-temperature pulse wave reactor 80 or the secondary air of the PDR. Since the gas used to backwash and clean the purification tank contains low-concentration VOCs waste gas, when it is used as the detonation feed air of the PDR high-temperature pulse wave reactor 80 or the secondary air of the PDR, a flame arrester should be installed in the pipeline connected to the PDR high-temperature pulse wave reactor 80.

[0202] like Figure 3As shown, the first cycle operation (1 in, 3 out, 2 cleaning) of the RTO device 2 is as follows: the first thermal storage bed 10 is used as an air intake heating tank, and the low-concentration VOCs waste gas 100 passes through the low-concentration VOCs waste gas inlet valve 102, the VOCs waste gas inlet manifold 122, first flows through the first thermal storage bed inlet valve 108, passes through the first thermal storage bed 10, and uses the thermal storage material accumulated in the ceramic thermal storage bed 12 of the first thermal storage bed that has been heated to heat the VOCs waste gas, raising its temperature to above its auto-ignition temperature, and then enters the high-temperature oxidation reaction chamber 40 through the mixing chamber 13 of the first thermal storage bed to carry out high-temperature oxidation reaction in the interior 42 of the high-temperature oxidation reaction chamber; the second thermal storage bed 20 is used as a purification tank for cleaning exhaust gas, and the clean gas after high-temperature oxidation combustion in the interior 42 of the high-temperature oxidation reaction chamber is extracted by the cleaning windmill 112, and is backwashed to clean the second thermal storage bed 20 of the second thermal storage bed used as the purification tank. The ceramic regenerative bed 22 of the bed will use the regenerative bed to clean the exhaust manifold 144 to extract and discharge the VOCs waste gas retained in the ceramic material accumulated in the ceramic regenerative bed 22 of the second regenerative bed and in the air inlet chamber 21 of the second regenerative bed, and send it to the PDR secondary air distribution chamber 81 of the multiple groups of PDR high-temperature pulse wave reactors 80 through the cleaning exhaust manifold 146, and use it as the secondary air of the PDR high-temperature pulse wave reactor 80; the third regenerative bed 30 is used as exhaust and as an exhaust energy recovery tank, and the high-temperature clean gas after high-temperature oxidation combustion in the high-temperature oxidation reaction chamber 42 of the high-temperature oxidation reaction chamber 40 is exchanged with the ceramic material accumulated inside the ceramic regenerative bed 32 of the third regenerative bed of the exhaust energy recovery tank, and the energy is stored in the ceramic material accumulated inside the ceramic regenerative bed 32 of the third regenerative bed for the next cycle to preheat the VOCs waste gas. Since the PDR-RTO device 1 for treating high-concentration VOCs waste gas will have irregularly discharged, unstable concentrations of high-concentration VOCs waste gas 70 in the high-temperature oxidation reaction chamber 40 of its RTO device 2, which will be destroyed by explosion in the PDR device 80 and then completely oxidized at high temperature in the high-temperature oxidation reaction chamber 40 of the RTO device 2, there will be irregular excess energy in the high-temperature oxidation reaction chamber 40 of the RTO device 2, which needs to be recovered from the waste heat recovery boiler 3 to generate steam 245, the flow of which needs to be controlled by the temperature change potential of the temperature controller 137 on the outlet pipeline 134 of the exhaust valve 117 below the heat storage bed 32, and the flow control valve 138 on the outlet pipeline 135 of the boiler water preheater 209 below the waste heat recovery boiler compartment 223 to adjust the gas flow through the waste heat recovery boiler 3. The temperature controller 137's potential for change is determined by the rate of change in the time required for the temperature controller 137 to reach the set temperature for each cycle of switching between thermal storage beds. The temperature controller 137's potential for change is used to adjust the opening of the control valve 138 on the outlet pipeline 135 of the boiler water preheater 209 to effectively remove excess energy.The second heat storage bed 20 is used as a purification tank for cleaning exhaust. The gas backwashed to clean the purification tank contains low-concentration VOCs waste gas, which is transported to the secondary air distribution chamber 81 of multiple groups of PDR high-temperature pulse wave reactors 80 through the second heat storage bed cleaning exhaust pipe 142 and the second heat storage bed cleaning exhaust valve 119 by the cleaning windmill 112 to be used as the detonation batching air of the PDR high-temperature pulse wave reactor 80 or the secondary air of the PDR. Since the gas backwashed to clean the purification tank contains low-concentration VOCs waste gas, when it is used as the detonation batching air of the PDR high-temperature pulse wave reactor 80 or the secondary air of the PDR, a flame arrester should be installed in the pipeline connected to the PDR high-temperature pulse wave reactor 80.

[0203] like Figure 4As shown, this is the second cycle operation of the RTO device 2 (3 in, 2 out, 1 cleaning): the third regenerator bed 30 is used as an air inlet heating tank, and the low-concentration VOCs waste gas 100 passes through the low-concentration VOCs waste gas inlet valve 102, the VOCs waste gas inlet manifold 122, first flows through the third regenerator bed inlet valve 110, passes through the third regenerator bed 30, and uses the heat storage material accumulated in the ceramic regenerator bed 32 of the heated third regenerator bed to heat the VOCs waste gas, raising its temperature to above its auto-ignition temperature, and then enters the high-temperature oxidation reaction chamber 40 through the mixing chamber 33 of the third regenerator bed to carry out high-temperature oxidation reaction in the interior 42 of the high-temperature oxidation reaction chamber; the first regenerator bed 10 is used as a purification tank for cleaning exhaust gas, and the clean gas after high-temperature oxidation combustion in the interior 42 of the high-temperature oxidation reaction chamber is extracted by the cleaning windmill 112, and is backwashed to clean the first regenerator bed 10 of the first regenerator bed 10 serving as the purification tank. The ceramic regenerative bed 12 of the bed will use the regenerative bed to clean the exhaust manifold 144 to extract and discharge the VOCs waste gas retained in the ceramic material accumulated in the ceramic regenerative bed 12 of the first regenerative bed and in the air inlet chamber 11 of the first regenerative bed through the cleaning windmill 112, and will be sent to the PDR secondary air distribution chamber 81 of multiple groups of PDR high-temperature pulse wave reactors 80 through the cleaning exhaust manifold 146 to be used as secondary air of the PDR high-temperature pulse wave reactor 80; the second regenerative bed 20 is used as exhaust and as an exhaust energy recovery tank, and the high-temperature clean gas after high-temperature oxidation combustion in the high-temperature oxidation reaction chamber 42 of the high-temperature oxidation reaction chamber 40 is exchanged with the ceramic material accumulated inside the ceramic regenerative bed 22 of the second regenerative bed of the exhaust energy recovery tank to store the energy in the ceramic material accumulated inside the ceramic regenerative bed 22 of the second regenerative bed for preheating the VOCs waste gas in the next cycle. Since the PDR-RTO device 1 for treating high-concentration VOCs waste gas will have irregularly discharged high-concentration VOCs waste gas 70 with unstable concentration in the high-temperature oxidation reaction chamber 40 of its RTO device 2, which will be destroyed by explosion in the PDR device 80 and then completely oxidized at high temperature in the high-temperature oxidation reaction chamber 40 of the RTO device 2, there will be irregular excess energy in the high-temperature oxidation reaction chamber 40 of the RTO device 2, which needs to be recovered from the waste heat recovery boiler 3 to generate steam 245, and the flow rate of the steam needs to be controlled by the temperature change potential of the temperature controller 137 on the outlet pipeline 134 of the exhaust valve 116 below the heat storage bed 22, and the flow control valve 138 on the outlet pipeline 135 of the boiler water preheater 209 below the waste heat recovery boiler compartment 223 adjusts the gas flow through the waste heat recovery boiler 3 to control the gas flow. The temperature controller 137's potential for change is determined by the rate of change in the time required for the temperature controller 137 to reach the set temperature for each cycle of switching between thermal storage beds. The temperature controller 137's potential for change is used to adjust the opening of the control valve 138 on the outlet pipeline 135 of the boiler water preheater 209 to effectively remove excess energy.The first heat storage bed 10 is used as a purification tank for cleaning exhaust gas. The gas used for backwashing and cleaning the purification tank contains low-concentration VOCs waste gas. It passes through the first heat storage bed cleaning exhaust pipe 141 and the first heat storage bed cleaning exhaust valve 118 and is transported by the cleaning windmill 112 to the secondary air distribution chamber 81 of multiple groups of PDR high-temperature pulse wave reactors 80 for use as detonation feed air or secondary air of PDR. Since the gas used for backwashing and cleaning the purification tank contains low-concentration VOCs waste gas, when it is used as detonation feed air or secondary air of PDR, a flame arrester should be installed in the pipeline connected to the PDR high-temperature pulse wave reactor 80.

[0204] like Figure 5As shown, the third cycle operation (2 in, 1 out, 3 cleaning) of the RTO device 2 is as follows: the second thermal storage bed 20 is used as an air intake heating tank, and the low-concentration VOCs waste gas 100 passes through the low-concentration VOCs waste gas inlet valve 102, the VOCs waste gas inlet manifold 122, first flows through the second thermal storage bed inlet valve 109, passes through the second thermal storage bed 20, and uses the thermal storage material accumulated in the ceramic thermal storage bed 22 of the heated second thermal storage bed to heat the VOCs waste gas, raising its temperature to above its auto-ignition temperature, and then enters the high-temperature oxidation reaction chamber 40 through the mixing chamber 23 of the second thermal storage bed to carry out high-temperature oxidation reaction in the interior 42 of the high-temperature oxidation reaction chamber; the third thermal storage bed 30 is used as a purification tank for cleaning exhaust gas, and the clean gas after high-temperature oxidation combustion in the interior 42 of the high-temperature oxidation reaction chamber is extracted by the cleaning windmill 112, and is backwashed to clean the third thermal storage bed 30 serving as the purification tank. The ceramic regenerative bed 32 of the bed will use the regenerative bed to clean the exhaust manifold 144 to extract and discharge the VOCs waste gas retained in the ceramic material accumulated in the ceramic regenerative bed 32 of the third regenerative bed and in the air inlet chamber 31 of the third regenerative bed, and send it to the PDR secondary air distribution chamber 81 of the multiple groups of PDR high-temperature pulse wave reactors 80 through the cleaning exhaust manifold 146, and use it as the secondary air of the PDR high-temperature pulse wave reactor 80; the first regenerative bed 10 is used as exhaust and as an exhaust energy recovery tank, and the high-temperature clean gas after high-temperature oxidation and combustion in the high-temperature oxidation reaction chamber 42 of the high-temperature oxidation reaction chamber 40 is exchanged with the ceramic material accumulated inside the ceramic regenerative bed 12 of the first regenerative bed of the exhaust energy recovery tank, and the energy is stored in the ceramic material accumulated inside the ceramic regenerative bed 12 of the first regenerative bed for the next cycle to preheat the VOCs waste gas. Since the PDR-RTO device 1 for treating high-concentration VOCs waste gas will have irregularly discharged high-concentration VOCs waste gas 70 with unstable concentration in the high-temperature oxidation reaction chamber 40 of its RTO device 2, which will be destroyed by explosion in the PDR device 80 and then completely oxidized at high temperature in the high-temperature oxidation reaction chamber 40 of the RTO device 2, there will be irregular excess energy in the high-temperature oxidation reaction chamber 40 of the RTO device 2, which needs to be recovered from the waste heat recovery boiler 3 to generate steam 245, and the flow rate of the steam needs to be controlled by the temperature change potential of the temperature controller 137 on the outlet pipeline 134 of the exhaust valve 115 below the heat storage bed 12, and the flow control valve 138 on the outlet pipeline 135 of the boiler water preheater 209 below the waste heat recovery boiler compartment 223 adjusts the gas flow through the waste heat recovery boiler 3 to control the gas flow. The temperature controller 137's potential for change is determined by the rate of change in the time required for the temperature controller 137 to reach the set temperature for each cycle of switching between thermal storage beds. The temperature controller 137's potential for change is used to adjust the opening of the control valve 138 on the outlet pipeline 135 of the boiler water preheater 209 to effectively remove excess energy.The third heat storage bed 30 is used as a purification tank for cleaning exhaust. The gas backwashed to clean the purification tank contains low-concentration VOCs waste gas, which is transported through the third heat storage bed cleaning exhaust pipe 143 and the third heat storage bed cleaning exhaust valve 120, and then by the cleaning windmill 112 through the cleaning exhaust manifold 146 to the secondary air distribution chamber 81 of multiple groups of PDR high-temperature pulse wave reactors 80 for use as detonation feed air or secondary air of the PDR high-temperature pulse wave reactor 80. Since the gas backwashed to clean the purification tank contains low-concentration VOCs waste gas, when it is used as detonation feed air or secondary air of the PDR high-temperature pulse wave reactor 80, a flame arrester should be installed in the pipeline connected to the PDR high-temperature pulse wave reactor 80.

[0205] Low-concentration VOCs waste gas 100 introduced into the PDR-RTO apparatus 1 through the RTO apparatus 2 of the PDR-RTO apparatus for treating high-concentration VOCs waste gas, and high-concentration VOCs waste gas 70 introduced into the PDR-RTO apparatus via multiple PDR high-temperature pulse wave reactors 80, undergo high-temperature oxidation reactions in the high-temperature oxidation reaction chamber 40 of the RTO apparatus 2. The high-temperature waste gas generated may exceed the energy required for stable operation of the RTO apparatus 2. Therefore, a portion of the high-temperature waste gas generated after the high-temperature oxidation reaction is directed to the waste heat recovery boiler 3 for energy recovery and steam generation. The remaining gas discharged from the high-temperature oxidation reaction chamber 40 undergoes heat energy recovery in the exhaust energy recovery tank, where the heat is stored in the ceramic thermal storage bed of the exhaust energy recovery tank for use as preheating for the low-concentration VOCs waste gas 100 in the next cycle. The exhaust gas is then mixed with the exhaust gas from the outlet pipeline 135 of the waste heat recovery boiler 3 through the thermal storage bed exhaust manifold 134, extracted by the main induced draft fan 113, and discharged through the main induced draft fan outlet pipeline 136 through the chimney 114.

[0206] The cleaning windmill 112 is used to clean the purification tank of the RTO equipment 2. Its gas flow rate is preferably 3% to 10% of the low-concentration VOCs waste gas 100 treatment flow rate, and is best to be less than 5% of the low-concentration VOCs waste gas 100 treatment flow rate.

[0207] The purpose of the PDR-RTO device 1 for treating high-concentration VOCs waste gas of the present invention is to completely destroy and treat low-concentration VOCs waste gas 100 and high-concentration VOCs waste gas 70 and effectively recover the energy generated. The energy released by the high-temperature oxidation and combustion of the low-concentration VOCs waste gas 100 and high-concentration VOCs waste gas 70 will be used to recover and generate steam, except for a small amount of energy used to provide gas heating for the low-concentration VOCs waste gas 100 as the inlet of the RTO device 2. Taking gas containing propane as an example, when the VOCs (i.e., propane) concentration of the low-concentration VOCs waste gas 100 and the high-concentration VOCs waste gas 70 reaches the minimum concentration C min= 500ppmv, in the RTO device 2 with a heat storage bed having an energy recovery efficiency of 95%, the high-temperature oxidation reaction chamber 40 of the RTO device 2 can be operated at 800 to 900°C without adding auxiliary fuel, and the low-concentration VOCs exhaust gas 100 and the high-concentration VOCs exhaust gas 70 can be completely destroyed and treated. That is, if the propane VOCs concentration reaches the minimum concentration C min = 500ppmv or more, the energy released by the high temperature oxidation combustion can provide the low concentration VOCs waste gas 100 and the high concentration VOCs waste gas 70 with a temperature increase from the gas inlet temperature T i Increase the product discharge temperature T to the main induced wind turbine outlet pipeline 136 o Therefore, if the VOCs concentration in the mixture of the low-concentration VOCs waste gas 100 and the high-concentration VOCs waste gas 70 is higher than the minimum concentration C min , the energy released by the high-temperature oxidation and combustion of VOCs contained in the mixture of low-concentration VOCs waste gas 100 and high-concentration VOCs waste gas 70 becomes excess energy for the traditional RTO equipment 2, and an appropriate method must be used to remove it. The traditional method is to reduce the discharge temperature of the product of the RTO equipment 2 to T oThe RTO unit 2 is improved to maintain the energy balance of the RTO unit 2. However, if the product discharged from the main induced wind turbine outlet pipeline 136 still cannot effectively discharge excess energy, the RTO unit 2 may overheat, burn, or explode. Therefore, the present invention provides an opening in the high-temperature oxidation reaction chamber 40 of the RTO unit 2 and utilizes a high-temperature oxidation reaction chamber bypass pipe 44 to connect to the waste heat recovery boiler 3. Since high-concentration VOCs waste gas usually faces huge instantaneous flow rate changes and concentration changes, the waste heat recovery boiler 3 of the PDR-RTO equipment 1 that treats high-concentration VOCs waste gas must be able to withstand the rapid energy supply changes caused by the instantaneous flow rate changes and concentration changes of the high-concentration VOCs waste gas 70 entering the PDR-RTO equipment 1 that treats high-concentration VOCs waste gas, which will thereby produce rapidly changing boiler loads. As a result, the steam drum 230 that the waste heat recovery boiler 3 must have must be capable of real-time and rapid steam drum 230 liquid level control and pressure control; the steam pressure generated by the waste heat recovery boiler 3 is adjusted by the steam flow controller 244 set on the cascade steam outlet pipeline 240 of the steam drum pressure controller 241 to control the steam flow control valve 242. The liquid level of the steam drum 230 of the waste heat recovery boiler 3 adopts a three-component control mode. The output value of the steam flow controller 244 installed on the steam outlet pipeline 240 of the steam drum 230 is used as the feedback condition. The output value of the boiler feed water flow controller 204 installed on the boiler feed water pipeline 206 is used as the feedforward condition. In addition, the liquid level controller 232 on the steam drum 230 is used as the liquid level control compensation condition. The ternary control mode is adopted to intelligently adjust the boiler feed water flow control valve 205 with automated software to effectively control the rapidly fluctuating liquid level of the steam drum 230.

[0208] The RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas of the present invention is combined with the waste heat recovery boiler 3 embodiment, such as Figure 2As shown, the waste heat recovery boiler 3 comprises a steam drum 230, a waste heat recovery boiler chamber 223, a set of waste heat recovery boiler pipe banks 222, an upper header 221, a lower header 220, and a boiler water preheater 209. The waste heat recovery boiler pipe banks 222 are integrally located between the upper header 221 and the lower header 220. The waste heat recovery boiler 3 is connected to the high-temperature oxidation reaction chamber 40 of the RTO unit 2 via a high-temperature oxidation reaction chamber bypass pipe 44. The steam drum 230 of the waste heat recovery boiler 3 is a horizontal steel pressure vessel located above the waste heat recovery boiler chamber 223. The waste heat recovery boiler chamber 223 can utilize a membrane water pipe wall design or a container lined with insulation material. The steam drum 230 of the waste heat recovery boiler 3 is connected to the upper header 221 via an ascending pipe 224. A gas-liquid separator 231 is installed at the connection point of the ascending pipe 224 within the steam drum 230 to collect saturated steam and hot water generated by the waste heat recovery boiler tube banks 222. The steam drum 230 of the waste heat recovery boiler 3 is connected to the lower header 220 via a downcomer 225 to supply boiler feed water to the waste heat recovery boiler tube banks 222. A steam drum pressure controller 241 is installed above the steam drum 230. This controller regulates a steam flow control valve 242 located on a steam pipeline 240 connected to the steam drum 230 outlet, adjusting the flow rate of the supplied steam 245 and effectively controlling the operating pressure of the waste heat recovery boiler 3.

[0209] When starting the PDR-RTO system 1 for treating high-concentration VOCs waste gas from a cold state, the system first activates the main induced draft blower 113, initiates the valve switching cycle of the RTO unit 2, and activates the combustion air blower 61 to allow combustion air 60 to enter the PDR-RTO system 1 for treating high-concentration VOCs waste gas. The multiple burners 56 of the RTO unit 2 are then activated to increase the temperature of the high-temperature oxidation reaction chamber 40. After the temperature inside the high-temperature oxidation reaction chamber 42 reaches the rated startup temperature, the low-concentration VOCs waste gas 100 introduction process begins. When the system is started cold, the low-concentration VOCs waste gas inlet valve 102 is first closed and the low-concentration VOCs waste gas bypass valve 104 is opened, so that the low-concentration VOCs waste gas 100 will not enter the RTO device 2 of the PDR-RTO device 1 that processes high-concentration VOCs waste gas; then the bypass air regulating valve 106 is opened so that the bypass air 111 can be introduced into the VOCs waste gas inlet manifold 122 through the bypass air pipeline 107 to enter the RTO device 2 of the PDR-RTO device 1 that processes high-concentration VOCs waste gas; then the operation cycle of the sequential opening and closing of the air inlet valve, the cleaning exhaust valve, and the exhaust valve of the RTO device 2 of the PDR-RTO device 1 that processes high-concentration VOCs waste gas is started; after confirming that the valve opening and closing sequence is stably operated, the multiple burners 56 on the high-temperature oxidation reaction chamber 40 are ignited to heat the ceramic heat storage bed (such as Figure 2The temperature of the first thermal storage bed 12, the second thermal storage bed 22, or the third thermal storage bed 32 is increased until the temperature of the high temperature oxidation reaction chamber 40 reaches the set operating temperature T c ; Then, the low-concentration VOCs waste gas 100 is first introduced into the RTO device 2, and the low-concentration VOCs waste gas 100 is stably operated and processed in the RTO device 2.

[0210] After the low-concentration VOCs waste gas 100 is stably processed in the RTO device 2, and the temperature field of the high-temperature oxidation reaction chamber 40 of the RTO device 2 is established and the temperature conditions for introducing the high-concentration VOCs waste gas 70 are reached, the high-concentration VOCs waste gas 70 is introduced into the PDR high-temperature pulse wave reactor 80 of the PDR-RTO device 1 that treats high-concentration VOCs waste gas; after waiting for the PDR high-temperature pulse wave reactor 80 to operate stably, stable VOCs waste gas treatment operations can be carried out.

[0211] When the number of thermal storage beds of the RTO device 2 of the PDR-RTO device 1 treating high-concentration VOCs exhaust gas is a multiple of three (i.e., M=3N), the inlet air heating, purification, and energy recovery operation modes of the RTO device 2 can be simplified to three operation cycles.

[0212] When the number of thermal storage beds in RTO Unit 2 of PDR-RTO Unit 1 treating high-VOC exhaust gas is an odd number (i.e., M = 2N + 1), the inlet air heating, purification, and energy recovery operation modes of RTO Unit 2 must be planned to have the same number of operating cycles as the number of thermal storage beds (M). For example, when N = 1, M = 2N + 1 = 3, resulting in 3 operating cycles; when N = 2, M = 2N + 1 = 5, resulting in 5 operating cycles; when N = 3, M = 2N + 1 = 7, resulting in 7 operating cycles; and so on.

[0213] For example, if the RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs exhaust gas has five thermal storage beds, its typical operating cycle can be planned into five groups of operating cycles by sequentially opening and closing the air inlet valve, the purge exhaust valve, and the exhaust valve, as shown in Table 2 below:

[0214] Table 2

[0215]

[0216] If the number of thermal storage beds in the RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas is a multiple of three, that is, M=3N, for example, when N=1, M=3N=3, and the number of operating cycles is 3; when N=2, M=3N=6, and the number of operating cycles is still 3; when N=3, M=3N=9, and the number of operating cycles is still 3; and so on. For example, when the RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas has six thermal storage beds, its typical operating cycle can be planned into three groups of operating cycles by sequentially opening and closing the air inlet valve, the purge exhaust valve, and the exhaust valve, as shown in Table 3 below:

[0217] Table 3

[0218]

[0219] Purification (1) and purification (2) can be performed simultaneously, or can be divided into two stages and performed consecutively within one operation cycle.

[0220] In the application scenario of treating high-concentration VOCs waste gas 70, a PDR high-temperature pulse wave reactor 80 is provided in the high-temperature oxidation reaction chamber 40 of the RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas (for example, Taiwan invention patent application number 113130710, Taiwan invention patent number I44865). The high-concentration VOCs waste gas 70 is pressurized by the high-concentration VOCs waste gas variable frequency booster fan 71, and is protected by the anti-detonation flame arrester 72. The high-concentration VOCs waste gas pressure controller 75 is used to adjust and control the operating frequency of the variable frequency high-concentration VOCs waste gas variable frequency booster fan 71, and then the high-concentration VOCs waste gas 70 is sent to the PDR high-temperature pulse wave reactor 80 through the high-concentration VOCs waste gas pipeline 74; then, the high-concentration VOCs waste gas flow controller 73 installed on the high-concentration VOCs waste gas pipeline 74 is used to cascade adjust and control the installation. The high-concentration VOCs waste gas proportioning air flow controller 76 on the assembly proportioning air pipeline 78 regulates and controls the proportioning air flow calculator 77 installed on the assembly proportioning air pipeline 78 to adjust the proportioning air flow regulating valve 79, so that the appropriately proportioned high-concentration VOCs waste gas 70 is dynamically matched with the appropriate amount of combustion air 60. The high-temperature detonation principle is then used to destroy and remove the explosive power of the high-concentration VOCs waste gas 70, and then it is sent to the high-temperature oxidation reaction chamber 40 of the RTO device 2. The high-temperature oxidation environment inside the high-temperature oxidation reaction chamber 42 of the RTO device 2 is further used to completely destroy it. The principle and operation of the PDR high-temperature pulse wave reactor 80 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas are as follows: Figure 6 and Figure 7 shown.

[0221] The PDR high-temperature pulse wave reactor 80 of the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas comprises: a high-concentration VOCs waste gas feed section 816, an anti-detonation flame arrester 818, a combustion air / low-concentration VOCs waste gas feed section 840, a detonation pulse wave reactor body 860, and a detonation pulse wave reactor outlet section 890. The PDR high-temperature pulse wave reactor 80 is connected to the RTO equipment 2 via an RTO connection flange 896. The gaseous reaction products 900 generated by the PDR high-temperature pulse wave reactor 80 during treatment of the high-concentration VOCs waste gas 70 are fed into the high-temperature oxidation reaction chamber 40 of the RTO equipment 2 for further complete oxidation to generate heat energy. The PDR high-temperature pulse wave reactor 80 of the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas is characterized by: (1) the high-concentration VOCs waste gas feeding section 817 includes a high-concentration VOCs waste gas feeding pipe 812 and a high-concentration VOCs waste gas feeding mixing chamber 814; (2) the anti-detonation flame arrester 818 is composed of a flame arrester core 817 and a porous fixing fixture 819; (3) the combustion air / low-concentration VOCs waste gas feeding section 840 includes a combustion air / low-concentration VOCs waste gas feeding pipe 832 and a combustion air / low-concentration VOCs waste gas feeding mixing distribution chamber 834; (4) the detonation pulse wave reactor body 860 includes a high-concentration VOCs waste gas dispersion feeding pipe fixed end plate 820, a detonation pulse wave reactor body 860, and a high-concentration VOCs waste gas dispersion feeding pipe fixed end plate 820. The detonation pulse wave reactor tube end plate 850, a detonation pulse wave reactor tube 866 containing a detonation promoter 870, a cooling facility 862 is provided on the outside of the detonation pulse wave reactor tube 866, and a plurality of high-concentration VOCs waste gas dispersion feeding pipes 822 and a plurality of ignition device groups 880 are provided inside the detonation pulse wave reactor tube 866; the cooling facility 862 on the outside of the detonation pulse wave reactor tube 866 uses a cooling water inlet 875 and a cooling water outlet 876 to provide cooling water cooling; (5) the detonation pulse wave reactor outlet section 890 is composed of a secondary vortex air jacket 892 and a pulse nozzle 894, and uses an RTO connecting flange 896 to combine the PDR high-temperature pulse wave reactor 80 with the RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas.

[0222] The characteristics of the detonation-proof flame arrester 818 of the PDR high-temperature pulse wave reactor 80 in the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas are as follows: the maximum experimental safety gap MESG (Maximum Experimental Safety Gap) of the detonation-proof flame arrester 818 is determined by the composition of the high-concentration VOCs waste gas 70: for Class IIC organic gases, the MESG needs to be designed to be less than 0.5 mm; for Class IIB organic gases, the MESG needs to be designed to be less than 0.8 mm; for other types of organic gases, the MESG needs to be designed to be less than 1.0 mm; therefore, the maximum experimental safety gap MESG of the detonation-proof flame arrester 818 of the PDR high-temperature pulse wave reactor 80 in the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas is usually designed to be between 0.3 mm and 1.0 mm. However, since high-concentration VOCs waste gas 70 usually collects waste gas from different sources and is processed in a centralized manner, the MESG of various high-concentration VOCs waste gas 70 may be different. In order to meet the usage requirements, the maximum experimental safety distance MESG of the anti-detonation flame arrester 818 of the PDR high-temperature pulse wave reactor 80 in the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas is preferably designed to be between 0.3mm and 0.5mm.

[0223] In the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas, the high-concentration VOCs waste gas dispersion feeding pipe 822 of the PDR high-temperature pulse wave reactor 80 is provided with a high-concentration VOCs waste gas dispersion feeding pipe internal flame prevention structure 824 at its outlet end, which has a backfire prevention function; the maximum experimental safety gap (MESG) of the high-concentration VOCs waste gas dispersion feeding pipe internal flame prevention structure 824 is determined by the composition of the high-concentration VOCs waste gas 70: for Class IIC organic gases, the MESG needs to be designed to be less than 0.5 mm; for Class IIB organic gases, the MESG needs to be designed to be less than 0.8 mm; for other types of organic gases, the MESG needs to be designed to be less than 1.0 mm; therefore, the maximum experimental safety gap (MESG) of the high-concentration VOCs waste gas dispersion feeding pipe internal flame prevention structure 824 of the PDR high-temperature pulse wave reactor 80 in the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas is usually designed to be between 0.3 mm and 1.0 mm. However, since high-concentration VOCs waste gas 70 typically aggregates waste gas from various sources for centralized treatment, the MESG values ​​for various high-concentration VOCs waste gas streams 70 may differ. To address these requirements, the maximum experimental safety clearance (MESG) of the flame barrier structure 824 within the high-concentration VOCs waste gas dispersing feed pipe of the PDR high-temperature pulse wave reactor 80 in the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas is preferably designed to be between 0.3mm and 0.5mm. The flame barrier structure 824 within the high-concentration VOCs waste gas dispersing feed pipe can be fabricated by sintering metal powder with a mesh size of 20 to 100 to provide the appropriate porosity and pore size, with sintering metal powder with a mesh size of 35 to 45 being particularly suitable.

[0224] The MESG is less than 0.3mm to 1.0mm. For example, in the aforementioned PDR-RTO equipment for treating high-concentration VOCs waste gas, the high-concentration VOCs waste gas dispersion feed pipe of the PDR high-temperature pulse wave reactor has a porous structure at its outlet end to prevent backfire, and the MESG is less than 0.3mm to 0.5mm.

[0225] For example, in the above-mentioned PDR-RTO equipment for treating high-concentration VOCs waste gas, the porous structure inside the outlet end of the high-concentration VOCs waste gas dispersion feeding pipe of the PDR high-temperature pulse wave reactor is made by sintering metal powder.

[0226] In the detonation pulse wave reactor tube 866 of the PDR high-temperature pulse wave reactor 80 in the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas, the minimum diameter of the reduced diameter pipe section 871 of the detonation accelerator 870 is 1 / 3 to 1 times the diameter of the straight pipe section 873 of the detonation accelerator 870; the maximum diameter of the expanded diameter pipe section 872 is 1.5 to 2 times the diameter of the straight pipe section 873 of the detonation accelerator 870; and the spacing between adjacent reduced diameter pipe sections 871 is 1 to 3 times the diameter of the straight pipe section 873. Among them, when the minimum diameter of the reduced pipe section 871 of the detonation promoter 870 in the detonation pulse wave reactor tube 866 of the PDR high-temperature pulse wave reactor 80 is 1 times the diameter of the straight pipe section 873 of the detonation promoter 870, and the spacing between adjacent reduced pipe sections 871 of the detonation promoter 870 in the detonation pulse wave reactor tube 866 of the PDR high-temperature pulse wave reactor 80 is 2 times the diameter of the straight pipe section 873, the required length of the detonation promoter 870 can be minimized and the detonation promotion efficiency can be maximized.

[0227] The high-concentration VOCs waste gas dispersion feeding pipe 822 of the PDR high-temperature pulse wave reactor 80 of the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas passes through the opening of the detonation pulse wave reactor tube end plate 850 and extends into the interior of the detonation pulse wave reactor tube 866. The detonation shock wave can be effectively controlled if the length protruding from the detonation pulse wave reactor tube end plate 850 is more than 0.5 times the detonation shock wavelength. Experiments have confirmed that it is best to have a length protruding from the detonation pulse wave reactor tube end plate 850 of 1.0 to 3.0 times the detonation shock wavelength.

[0228] In the PDR-RTO device 1 for treating high-concentration VOCs waste gas, the high-concentration VOCs waste gas 70 is treated by introducing it into the RTO device 2 using a PDR high-temperature pulse wave reactor 80. Its characteristics are as follows:

[0229] (1) The high-concentration VOCs waste gas 70 is introduced into the high-concentration VOCs waste gas feeding mixing chamber 814 from the high-concentration VOCs waste gas feeding pipe 812 of the PDR high-temperature pulse wave reactor 80;

[0230] (2) The combustion air / low-concentration VOCs waste gas 830 is introduced into the combustion air / low-concentration VOCs waste gas feeding mixing and distribution chamber 834 through the combustion air / low-concentration VOCs waste gas feeding pipe 832 of the PDR high-temperature pulse wave reactor 80;

[0231] (3) The flame arrester 818 of the PDR high-temperature pulse wave reactor 80 is installed at the outlet of the high-concentration VOCs waste gas feeding mixing chamber 814, followed by a high-concentration VOCs waste gas dispersion feeding pipe fixed end plate 820 connected to the high-concentration VOCs waste gas dispersion feeding pipe 822;

[0232] (4) The high-concentration VOCs waste gas dispersing feeding pipe 822 of the PDR high-temperature pulse wave reactor 80 is installed on the high-concentration VOCs waste gas dispersing feeding pipe fixed end plate 820 and passes through the detonation pulse wave reactor pipe end plate 850;

[0233] (5) The detonation accelerator 870 in the detonation pulse wave reactor tube 866 of the PDR high-temperature pulse wave reactor 80 is composed of a plurality of serially connected reduced diameter pipe sections 871, expanded diameter pipe sections 872, and straight pipe sections 873;

[0234] (6) The installation of the high-concentration VOCs waste gas dispersion feed pipe 822 of the PDR high-temperature pulse wave reactor 80 protrudes the detonation pulse wave reactor tube end plate 850, so that it has the function of providing gas mixing and terminating the countercurrent detonation pulse wave;

[0235] (7) The ignition device 880 of the PDR high temperature pulse wave reactor 80 is installed at the downstream end of the detonation accelerator 870;

[0236] (8) The PDR high-temperature pulse wave reactor 80 utilizes the high-concentration VOCs waste gas dispersion feed pipe 822 to continuously inject the high-concentration VOCs waste gas 70 into the detonation pulse wave reactor pipe 866;

[0237] (9) The PDR high temperature pulse wave reactor 80 utilizes the combustion air / low concentration VOCs waste gas feed pipe 832 to continuously inject the combustion air / low concentration VOCs waste gas 830 into the detonation pulse wave reactor pipe 866;

[0238] (10) The PDR high temperature pulse wave reactor 80 utilizes a detonation accelerator 870 to promote the mixing of high concentration VOCs exhaust gas 70 and combustion air / low concentration VOCs exhaust gas 830;

[0239] (11) The PDR high-temperature pulse wave reactor 80 uses an ignition device 880 to ignite the high-concentration VOCs waste gas 70 and the gas mixture of combustion air / low-concentration VOCs waste gas 830 in the detonation pulse wave reactor tube 866;

[0240] (12) The PDR high temperature pulse wave reactor 80 utilizes the detonation accelerator 870 in the detonation pulse wave reactor tube 866 to cause the ignited gas mixture to backfire and generate a countercurrent detonation pulse wave;

[0241] (13) The PDR high-temperature pulse wave reactor 80 utilizes a countercurrent detonation pulse wave to pass through the high-concentration VOCs exhaust gas dispersion feed pipe 822 protruding from the detonation pulse wave reactor tube end plate 850, so that the detonation pulse wave impacts the detonation pulse wave reactor tube end plate 850 and extinguishes the flame;

[0242] (14) The PDR high-temperature pulse wave reactor 80 utilizes the pressure release expansion after the detonation shock wave flame is extinguished to generate a counter-shock wave to discharge the reaction products out of the detonation pulse wave reactor body 860 and send them into the RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas through the pulse nozzle 894;

[0243] (15) The above procedure is repeated continuously, so that the high-concentration VOCs waste gas 70 can continuously undergo chemical reactions in the PDR high-temperature pulse wave reactor 80 using the high temperature, high pressure, and high speed of the detonation shock wave.

[0244] The basic operating principle of the PDR high temperature pulse wave reactor 80 in the PDR-RTO equipment 1 for treating high concentration VOCs waste gas is as follows: Figure 7 As shown, the description is as follows:

[0245] (1) The PDR high-temperature pulse wave reactor 80 has multiple high-concentration VOCs waste gas feed pipes 812, which can be a single feed pipe or multiple feed pipes, so that multiple high-concentration VOCs waste gases 70 can be fed simultaneously and continuously. The PDR high-temperature pulse wave reactor 80 also has multiple combustion air / low-concentration VOCs waste gas feed pipes 832, which can also be a single feed pipe or multiple feed pipes, and can receive air, inert gas, oxygen, water, catalyst, etc., for continuous feeding simultaneously. The detonation pulse wave reactor tube 866 installed inside the detonation pulse wave reactor body 860 of the PDR high-temperature pulse wave reactor 80 contains a detonation promoter 870, which can promote the mixing of the high-concentration VOCs waste gas 70 and the combustion air / low-concentration VOCs waste gas 830, so that the gas mixture of the high-concentration VOCs waste gas 70 and the combustion air / low-concentration VOCs waste gas 830 flows evenly from the detonation pulse wave reactor tube end plate 850 to the reaction product outlet 900 in the detonation pulse wave reactor body 860, as shown in FIG. Figure 7 The feeding step 510 to the filling step 520 is shown.

[0246] (2) When the gas mixture of high-concentration VOCs exhaust gas 70 and combustion air / low-concentration VOCs exhaust gas 830 reaches the position of the ignition device group 880 installed on the straight pipe section 873 downstream of the detonation accelerator 870, the gas mixture of high-concentration VOCs exhaust gas 70 and combustion air / low-concentration VOCs exhaust gas 830 will be ignited by the ignition device group 880, as shown in FIG. Figure 7 The ignition step is shown as 530 .

[0247] (3) Since there is no flammable gas downstream of the ignition device group 880, the flame will backfire and burn toward the detonation pulse wave reactor tube end plate 850 of the PDR high temperature pulse wave reactor 8, generating a countercurrent flame that moves toward the detonation accelerator 870, as shown in FIG. Figure 7 Deflagration step 540 is shown.

[0248] (4) The flame then passes through the detonation accelerator 870 to provide good mixing, so that the ignited high-concentration VOCs waste gas 70 and the combustion air / low-concentration VOCs waste gas 830 combustible gas mixture burns quickly, increases temperature, pressure, and speed, and then turns to produce countercurrent detonation (Countercurrent Detonation), such as Figure 7 Deflagration acceleration step 550 is shown.

[0249] (5) The detonation shock wave continues to compress the combustible gas mixture of high-concentration VOCs exhaust gas 70 and combustion air / low-concentration VOCs exhaust gas 830 to react, and continues to accelerate to reach the CJ shock wave speed, such as Figure 7 This is shown in step 560 of detonation.

[0250] (6) When the detonation shock wave reaches the detonation pulse wave reactor tube end plate 850 of the PDR high-temperature pulse wave reactor 8, since the high-concentration VOCs waste gas dispersion feeding pipe 822 extends beyond the detonation pulse wave reactor tube end plate 850, the detonation shock wave quickly surpasses the high-concentration VOCs waste gas 70 combustible fuel supply passing through the high-concentration VOCs waste gas dispersion feeding pipe 822 outlet end, and the high-concentration VOCs waste gas 70 supply is instantly cut off, causing the detonation shock wave to instantly have no energy supply, resulting in instant flame extinction. At the same time, the pressure effect of the detonation shock wave is used to extinguish the flame, as shown in FIG. Figure 7 The flame extinguishing step 570 is shown.

[0251] (7) After the detonation shock wave loses the fuel supply of the high-concentration VOCs exhaust gas 70 and extinguishes the flame, since there is no more energy to continue compressing the gas, the gas in the high-temperature and high-pressure shock wave will automatically undergo adiabatic expansion, causing the volume to expand rapidly and form a counter-shock wave, which discharges the reaction products 900 in the detonation pulse wave reactor tube 866 from the detonation pulse wave reactor outlet section 890, as shown in FIG. Figure 7 The back-shock discharge step is shown in step 580 .

[0252] (8) The speed from the ignition step 530 to the flameout step 570 and then to the back-shock discharge step 580 is extremely fast, and the time required is only a few milliseconds to a few tenths of a second, depending on the design of the detonation promoter 870.

[0253] (9) The detonation pulse wave reactor outlet section 890 of the PDR high temperature pulse wave reactor 8 of the PDR-RTO device 1 for treating high concentration VOCs waste gas is connected to the RTO device 2 of the PDR-RTO device 1 for treating high concentration VOCs waste gas by using the RTO connection flange 896. During operation, the reaction product 800 is discharged from the detonation pulse wave reactor outlet section 890 by using the back shock wave of the detonation shock wave. Figure 7 As shown in the back-shock discharge step 580, the waste gas is then sent to the RTO device 2 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas for thorough oxidation treatment, and then the waste heat recovery boiler 3 is used to recover excess energy to generate steam 245.

[0254] (10) When the above-mentioned operation procedure is performed, the feeding of the high-concentration VOCs waste gas 70 and the combustion air / low-concentration VOCs waste gas 830 can continue stably, and the procedures of turbulent mixing, ignition, countercurrent detonation, and flameout of the high-concentration VOCs waste gas 70 and the combustion air / low-concentration VOCs waste gas 830 are continuously repeated, so that the high-concentration VOCs waste gas 70 can continuously react or be destroyed by the high temperature and high pressure of the detonation shock wave in the PDR high-temperature pulse wave reactor 8 of the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas.

[0255] A PDR-RTO device 1 for treating high-concentration VOCs waste gas, wherein the high-concentration VOCs waste gas dispersion feeding pipe 822 in the PDR high-temperature pulse wave reactor 8 passes through the opening of the detonation pulse wave reactor tube end plate 850 and extends into the interior of the detonation pulse wave reactor tube 866, and the length protruding from the detonation pulse wave reactor tube end plate 850 is more than 1.5 times the detonation shock wavelength, and it is best to have the length protruding from the detonation pulse wave reactor tube end plate 850 be 2.0 times the detonation shock wavelength.

[0256] In the case of the high-temperature oxidation reaction chamber 40 of the RTO unit 2 overheating, the waste heat recovery boiler 3 overpressure, or the simultaneous extinguishing of multiple burners 56 in the high-temperature oxidation reaction chamber 40, the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas of the present invention will undergo a safety interlock shutdown to ensure the safe operation of the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas. At this time, the high-concentration VOCs waste gas 70 from the PDR high-temperature pulse wave reactor 80 is first discharged, and then the low-concentration VOCs waste gas 100 from the RTO unit 2 is discharged, thereby ensuring the safe operation of the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas. The process for discharging the high-concentration VOCs waste gas 70 from the PDR high-temperature pulse wave reactor 80 is to shut off the high-concentration VOCs waste gas variable frequency booster fan 71 and open the high-concentration VOCs waste gas bypass valve 69. The process of exporting the low-concentration VOCs waste gas 100 of the RTO equipment 2 is to open the low-concentration VOCs waste gas bypass valve 104 installed on the low-concentration VOCs waste gas bypass pipeline 103 to export the low-concentration VOCs waste gas bypass 105, and close the low-concentration VOCs waste gas inlet valve 102 to bypass the low-concentration VOCs waste gas; then open the bypass air regulating valve 106 to allow the bypass air 111 to be introduced into the RTO equipment 2 from the bypass air pipeline 107 to maintain the stable operation of the PDR-RTO equipment 1 that treats high-concentration VOCs waste gas.

[0257] In an embodiment of the PDR-RTO device 1 for treating high-concentration VOCs waste gas of the present invention, the treatment of VOCs waste gas containing cyclohexane is taken as an example. The concentration of the low-concentration VOCs waste gas 100 is about 1000 ppmv and the flow rate is about 100,000 NCMH; the concentration of the high-concentration VOCs waste gas 70 is about 10-50% and the flow rate is about 200-500 NCMH; when the PDR-RTO device 1 for treating high-concentration VOCs waste gas of the present invention is used, the operating temperature of the high-temperature oxidation reaction chamber 40 of the RTO device 2 is in the range of 800°C to 1000°C, when the low-concentration VOCs waste gas 100 and the high-concentration VOCs waste gas 70 are separated and flowed through the PD for treating high-concentration VOCs waste gas. During the treatment by the R-RTO device 1, the low-concentration VOCs waste gas 100 is fed into the RTO device 2 for processing, and the high-concentration VOCs waste gas 70 is treated by the PDR high-temperature pulse wave reactor 80 and then sent to the high-temperature oxidation reaction chamber 40 of the RTO device 2. The high-temperature oxidation reaction chamber 40 of the PDR-RTO device 1 for treating high-concentration VOCs waste gas only needs to provide the auxiliary fuel 50 required by the burner 56 to maintain the mother fire to maintain a stable mother fire, thereby ensuring that the VOCs waste gas 100 and the high-concentration VOCs waste gas 70 can be effectively destroyed, and its destruction efficiency can reach more than 99.5%. The excess energy can also be flexibly utilized by the waste heat recovery boiler 3 to generate 3 to 8 metric tons / hour of steam 245, and an average of about 5 metric tons / hour of steam 245 can be generated throughout the year. In terms of the present invention, the VOCs concentration / flow combination allowed to be treated by the PDR-RTO device 1 for treating high-concentration VOCs waste gas is:

[0258] (1) The maximum allowable operating concentration of low-concentration VOCs waste gas 100 is 25% of the lower explosion limit of low-concentration VOCs waste gas 100, the minimum allowable operating concentration is 0 ppm, the minimum allowable operating flow rate is 10,000 NCMH, the maximum allowable operating flow rate is 110% of the design capacity, that is, 110,000 NCMH, and the load-reduction ratio is 1:1.1;

[0259] (2) The maximum allowable operating concentration of the high-concentration VOCs exhaust gas 70 is 100% VOCs, that is, the maximum allowable operating concentration of the high-concentration VOCs exhaust gas 70 is unlimited, the minimum allowable operating concentration is 0% VOCs, the minimum allowable operating flow rate is 0 NCMH, and the maximum design flow rate is 500 NCMH;

[0260] (3) Since the PDR high-temperature pulse wave reactor 80 uses detonation technology to destroy the high-concentration VOCs waste gas 70, the energy density of the PDR high-temperature pulse wave reactor 80 is more than 100 million times that of traditional combustion technology. Therefore, the PDR high-temperature pulse wave reactor 80 allows the high-concentration VOCs waste gas 70 to have rapid changes in instantaneous concentration and flow without affecting its safe operation.

[0261] The present invention has been verified through actual testing that the PDR high-temperature pulse wave reactor 80 can tolerate an instantaneous overload of 300% without affecting its operational safety. The PDR-RTO equipment 1 for treating high-concentration VOCs waste gas according to the present invention can replace the high-altitude flare originally used to treat abnormal emissions. In addition to generating 245 tons of steam to achieve energy conservation and carbon reduction goals, it can also save 2.5 metric tons of steam per hour for the flare; that is, the recovered steam volume plus the saved flare steam volume can generate a total benefit of 7.5 metric tons per hour. The investment benefit of the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas according to the present invention is calculated at RMB 200 per ton of steam. The value of steam saving and recovery = 8,000 hours / year × (RMB 200 / metric ton × 7.5 metric tons / hour) = RMB 12,000,000 / year.

[0262] The above description shows that the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas of the present invention does have the effect of energy conservation and carbon reduction. Moreover, through the energy recovery and utilization technology of the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas of the present invention, the VOCs treatment problem that originally required a large amount of auxiliary energy expenditure can be transformed into a renewable energy investment opportunity that can recover a large amount of energy generated by VOCs combustion through VOCs treatment and obtain huge investment returns. The application of the PDR-RTO equipment 1 for treating high-concentration VOCs waste gas of the present invention not only provides a brand-new technical solution to the century-old unresolved pollution problems of petrochemical, refining, plastics, rubber and other petrochemical industries, but also, through the integrated application of detonation technology, combustion technology and energy recovery technology, invents a new technology with energy conservation, carbon reduction and circular economy benefits, which can make significant contributions to the ecological environment and the mitigation of global warming.

[0263] The above description is only illustrative of the present invention and not restrictive. Those skilled in the art will understand that many modifications, changes or equivalent substitutions may be made without departing from the concept and scope defined by the claims of the invention, but all of them will fall within the scope defined by the claims of the invention.

[0264] The specific embodiments described above further illustrate the objectives, technical solutions and beneficial effects of the present invention in detail. It should be understood that the above are only specific embodiments of the present invention and are not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the scope of protection of the present invention.

Claims

1. A PDR-RTO device for treating high-concentration VOCs waste gas, comprising: It consists of a set of RTO equipment, a set of waste heat recovery boiler, and multiple sets of PDR high temperature pulse wave reactors installed on the RTO equipment; The RTO equipment contains multiple heat storage beds, a high-temperature oxidation reaction chamber, and a set of VOCs waste gas inlet valves, a set of cleaning exhaust valves and a set of combustion waste gas exhaust valves under each heat storage bed; The waste heat recovery boiler is provided with multiple groups of lower headers, multiple groups of upper headers and multiple groups of waste heat recovery boiler tube banks, which are placed sideways beside the high-temperature oxidation reaction chamber; The low-concentration VOCs waste gas and the high-concentration VOCs waste gas are separated and introduced into the PDR-RTO equipment for treating the high-concentration VOCs waste gas; Low-concentration VOCs waste gas is introduced into the PDR-RTO equipment for treating high-concentration VOCs waste gas through the air inlet of the RTO equipment; High-concentration VOCs waste gas is introduced into the PDR-RTO equipment for treating high-concentration VOCs waste gas using the PDR high-temperature pulse wave reactor; After the low-concentration VOCs waste gas enters the PDR-RTO equipment that treats high-concentration VOCs waste gas, it is first preheated by the heat storage bed of the RTO equipment, and then oxidized at high temperature in the high-temperature oxidation reaction chamber. The energy generated by combustion is recovered by another heat storage bed of the RTO equipment, so that the VOCs waste gas can be completely destroyed and treated; High-concentration VOCs waste gas is passed through the PDR high-temperature pulse wave reactor using detonation technology to remove the explosion energy of VOCs, and then introduced into the high-temperature oxidation reaction chamber of the RTO equipment to completely oxidize it at high temperature; The low-concentration VOCs waste gas introduced into the PDR-RTO device for treating high-concentration VOCs waste gas through the RTO device and the high-concentration VOCs waste gas introduced into the PDR-RTO device for treating high-concentration VOCs waste gas using the PDR high-temperature pulse wave reactor undergo oxidation reaction in the high-temperature oxidation reaction chamber of the RTO device. Part of the high-temperature waste gas generated is directed to the waste heat recovery boiler for energy recovery to generate steam; The high-temperature exhaust gas discharged from part of the high-temperature oxidation reaction chamber is recovered in the exhaust energy recovery tank of the RTO equipment, and the heat is stored in the ceramic heat storage bed of the exhaust energy recovery tank of the RTO equipment, and then discharged from the combustion exhaust gas exhaust valve, and extracted by the induced fan and sent to the chimney for discharge; The flow rate regulating control valve at the outlet of the waste heat recovery boiler is used to regulate the gas flow entering the waste heat recovery boiler for energy recovery and steam generation; The opening ratio of the flow regulating control valve is dynamically adjusted using the outlet temperature variation potential of the combustion exhaust gas exhaust valve of the RTO device.

2. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 1, wherein: The high-concentration VOCs waste gas of the PDR-RTO equipment that treats high-concentration VOCs waste gas is introduced using the PDR high-temperature pulse wave reactor, with a concentration of 0% to 100%. The PDR high-temperature pulse wave reactor can allow instantaneous overload operation and instantaneous flow and concentration changes.

3. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 2, wherein: The RTO equipment uses the switching of the air intake valve, the cleaning exhaust valve and the combustion exhaust valve to make the heat storage tank alternately used as the air intake heating tank, the purification tank and the exhaust energy recovery tank, and at least one of the heat storage tanks is used as a purification tank, and the others are used as air intake heating tanks and exhaust energy recovery tanks. The operation cycle is: The low-concentration VOCs waste gas is introduced into the air heating tank through the air inlet valve of the RTO equipment, and the temperature is raised by the heated heat storage bed in the air inlet heating tank, and then enters the high-temperature oxidation reaction chamber of the RTO equipment for oxidation reaction. After that, part of the combustion product flows through the exhaust energy recovery tank of the RTO equipment, and the energy of the combustion product is stored in the ceramic heat storage bed of the exhaust energy recovery tank, and part of it flows through the waste heat recovery boiler to recover energy and generate steam; In the purification tank of the RTO equipment, the clean gas after combustion in the high-temperature oxidation reaction chamber of the RTO equipment is extracted by a cleaning windmill, backwashed into the ceramic heat storage bed of the cleaning purification tank, and the gas is discharged to the PDR high-temperature pulse wave reactor for use; Each operation cycle of the RTO equipment lasts for a specific time and then switches to the next operation cycle. The air intake heating tank is converted into a purification tank in the next operation cycle after use. The purification tank is converted into an exhaust energy recovery tank in the next operation cycle after cleaning. The exhaust energy recovery tank is converted into an air intake heating tank in the next operation cycle of the RTO equipment.

4. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 3, wherein: An inlet flame arrester is provided between the VOCs waste gas inlet valve and the thermal storage bed under each ceramic thermal storage bed of the RTO equipment.

5. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 4, wherein: The maximum experimental safety distance MESG of the inlet flame arrester is determined by high-concentration VOCs exhaust gas, but is between 0.3mm and 1.0mm.

6. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 4, wherein: The maximum experimental safety distance MESG of the inlet flame arrester is between 0.3mm and 0.5mm.

7. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 1, wherein: The maximum concentration of low-concentration VOCs exhaust gas that RTO equipment can tolerate is 25% of the LEL.

8. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 1, wherein: The maximum concentration of low-concentration VOCs exhaust gas that RTO equipment can tolerate is 50% of the LEL.

9. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 3, wherein: The gas flow rate of the cleaning wind turbine used in the RTO equipment purification tank is less than 10% of the VOCs waste gas treatment flow rate.

10. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 3, wherein: The gas flow rate of the cleaning windmill used for the RTO equipment purification tank is 3% to 5% of the volatile organic chemical waste gas treatment flow rate.

11. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 3, wherein: In the purification tank of the RTO equipment, the clean gas after combustion inside the high-temperature oxidation reaction chamber is extracted by a cleaning windmill, back-flushed into the ceramic heat storage bed of the RTO equipment cleaning purification tank, and the gas is discharged to the PDR high-temperature pulse wave reactor for nozzle cooling and secondary air.

12. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 3, wherein: The operating cycle of the RTO equipment valve switching lasts for a specific time of 180 seconds to 900 seconds.

13. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 3, wherein: The operating cycle of the RTO equipment valve switching lasts for a specific time of 300 seconds to 600 seconds.

14. According to claim 3, the oxidation temperature of the high-temperature oxidation reaction chamber of the RTO equipment of the PDR-RTO equipment for treating high-concentration VOCs waste gas is higher than the auto-ignition temperature of the low-concentration VOCs waste gas, so that the low-concentration VOCs waste gas is allowed to be introduced from the RTO equipment into the PDR-RTO equipment for treating high-concentration VOCs waste gas.

15. According to claim 1, the oxidation temperature of the high-temperature oxidation reaction chamber of the RTO equipment of the PDR-RTO equipment for treating high-concentration VOCs waste gas is higher than the auto-ignition temperature of the high-concentration VOCs waste gas, so that the high-concentration VOCs waste gas is allowed to be introduced into the PDR-RTO equipment for treating high-concentration VOCs waste gas from the PDR high-temperature pulse wave reactor.

16. The waste heat recovery boiler of the PDR-RTO equipment for treating high-concentration VOCs waste gas according to claim 1, wherein the load control is to utilize the exhaust temperature change of the heat storage bed of the RTO equipment, which is converted into temperature change potential through Fourier function, and is controlled by adjusting the flow control valve in combination with expert rules.

17. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 1, wherein: PDR high temperature pulse wave reactor includes: A set of high-concentration VOCs waste gas feeding section; A set of anti-detonation flame arresters; A set of combustion air / low-concentration VOCs exhaust gas feeding section; A set of detonation pulse wave reactor bodies; A set of detonation pulse wave reactor exit sections; Its characteristics are The high concentration VOCs waste gas feeding section includes: High concentration VOCs waste gas feed pipe, A set of high-concentration VOCs exhaust gas feed mixing chamber; The combustion air / low-concentration VOCs exhaust gas feed section includes: Combustion air / low concentration VOCs exhaust gas feed pipe, A set of combustion air / low-concentration VOCs exhaust gas feed mixing and distribution chamber; The detonation pulse wave reactor body includes: A set of fixed end plates for high-concentration VOCs exhaust gas dispersion feed pipes, A set of detonation pulse wave reactor tube end plates, A set of detonation pulse wave reactor tubes containing detonation boosters, A cooling facility, Multiple high-concentration VOCs waste gas dispersion feed pipes, Multiple ignition device groups, A flange assembly connected to the high temperature oxidation reaction chamber; The high-concentration VOCs waste gas is introduced into the high-concentration VOCs waste gas feeding mixing chamber through the high-concentration VOCs waste gas feeding pipe; The combustion air / low-concentration VOCs waste gas is introduced into the combustion air / low-concentration VOCs waste gas feed mixing and distribution chamber through the combustion air / low-concentration VOCs waste gas feed pipe; The flame arrester is installed at the outlet of the high-concentration VOCs waste gas feeding mixing chamber, and a fixed end plate of the high-concentration VOCs waste gas dispersing feeding pipe is arranged behind it, which is connected to the high-concentration VOCs waste gas dispersing feeding pipe; The high-concentration VOCs waste gas dispersion feeding pipe is installed on the fixed end plate of the high-concentration VOCs waste gas dispersion feeding pipe, and passes through the end plate of the detonation pulse wave reactor pipe to feed the high-concentration VOCs waste gas into the detonation pulse wave reactor pipe; The detonation accelerator in the detonation pulse wave reactor tube is composed of a plurality of serially connected reduced diameter pipe sections, expanded diameter pipe sections and straight pipe sections; The installation of the high-concentration VOCs waste gas dispersion feed pipe highlights the detonation pulse wave reactor tube end plate, so that it has the function of providing gas mixing and terminating the countercurrent detonation pulse wave; The ignition device is installed at the downstream end of the detonation accelerator; High-concentration VOCs waste gas is continuously injected into the detonation pulse wave reactor tube by using a high-concentration VOCs waste gas dispersion feeder pipe; The combustion air / low-concentration VOCs waste gas is continuously injected into the detonation pulse wave reactor tube by using the combustion air / low-concentration VOCs waste gas feed pipe; Use a detonation accelerator to promote the mixing of high-concentration VOCs exhaust gas and combustion air / low-concentration VOCs exhaust gas; The high-concentration VOCs waste gas and the gas mixture of combustion air / low-concentration VOCs waste gas in the detonation pulse wave reactor tube are ignited by an ignition device; Using a detonation accelerator in a detonation pulse wave reactor tube, the ignited gas mixture is flashed back to generate a countercurrent detonation pulse wave; The countercurrent detonation pulse wave is used to pass through the high-concentration VOCs waste gas dispersion feed pipe protruding from the detonation pulse wave reactor tube end plate, so that the detonation pulse wave impacts the detonation pulse wave reactor tube end plate and extinguishes the flame; The detonation shock wave is used to release pressure and expand after flame extinction to generate a reverse shock wave to discharge the reaction products out of the detonation pulse wave reactor body; The above procedures are repeated continuously, so that the high-concentration VOCs waste gas can continuously utilize the high temperature, high pressure and high speed of the detonation shock wave to carry out chemical reactions.

18. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The maximum experimental safety distance MESG of the detonation flame arrester is determined by the high concentration of VOCs exhaust gas, but is between 0.3mm and 1.0mm.

19. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The maximum experimental safety distance MESG of the detonation-proof flame arrester is between 0.3mm and 0.5mm.

20. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The high-concentration VOCs waste gas dispersion feeding pipe in the PDR high-temperature pulse wave reactor is provided with a high-concentration VOCs waste gas dispersion feeding pipe internal flame prevention structure at its outlet end, which has a backfire prevention function, and its MESG is less than 0.3mm to 1.0mm.

21. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The high-concentration VOCs waste gas dispersion feeding pipe of the PDR high-temperature pulse wave reactor is provided with a porous structure inside its outlet end to prevent backfire, and its MESG is less than 0.3mm to 0.5mm.

22. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The porous structure inside the outlet end of the high-concentration VOCs waste gas dispersion feed pipe of the PDR high-temperature pulse wave reactor is made by sintering metal powder with a mesh size of 20 to 100.

23. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The minimum diameter of the reduced diameter pipe section of the detonation accelerator in the detonation pulse wave reactor tube of the PDR high-temperature pulse wave reactor is 1 / 3 to 1 times the diameter of the straight pipe section of the detonation accelerator; the maximum diameter of the expanded diameter pipe section is 1.5 to 2 times the diameter of the straight pipe section of the detonation accelerator; the spacing between adjacent reduced diameter pipe sections is 1 to 3 times the diameter of the straight pipe section.

24. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The minimum diameter of the reduced diameter pipe section of the detonation accelerator of the PDR high temperature pulse wave reactor is 1 times the diameter of the straight pipe section of the detonation accelerator.

25. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The maximum diameter of the expanded pipe section of the detonation accelerator of the PDR high temperature pulse wave reactor is twice the diameter of the straight pipe section of the detonation accelerator.

26. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The spacing between adjacent reduced diameter pipe sections of the detonation accelerator of the PDR high temperature pulse wave reactor is twice the diameter of the straight pipe section.

27. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The high-concentration VOCs waste gas dispersion feeding pipe of the PDR high-temperature pulse wave reactor extends into the interior of the detonation pulse wave reactor tube after passing through the opening of the detonation pulse wave reactor tube end plate, and the length protruding from the detonation pulse wave reactor tube end plate is more than 1 / 2 times the detonation shock wavelength.

28. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The high-concentration VOCs waste gas dispersion feeding pipe of the PDR high-temperature pulse wave reactor extends into the interior of the detonation pulse wave reactor tube after passing through the opening of the detonation pulse wave reactor tube end plate, and the length protruding from the detonation pulse wave reactor tube end plate is 1.0 to 3.0 times the detonation shock wavelength.

29. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The detonation pulse wave reactor tube end plate of the PDR high temperature pulse wave reactor has multiple openings, some of which have high concentration VOCs waste gas dispersion feeding pipes passing through, and the remaining openings are for combustion air / low concentration VOCs waste gas to flow through.

30. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The detonation pulse wave reactor tube end plate of the PDR high temperature pulse wave reactor has an opening through which a high concentration VOCs waste gas dispersion feeding pipe passes, and the opening diameter is 1.0 to 2.0 times the diameter of the high concentration VOCs waste gas dispersion feeding pipe.

31. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The detonation pulse wave reactor tube end plate of the PDR high-temperature pulse wave reactor has an opening for the high-concentration VOCs waste gas dispersion feeding pipe to pass through, and the gap larger than the diameter of the high-concentration VOCs waste gas dispersion feeding pipe is for the circulation of combustion air / low-concentration VOCs waste gas.

32. A PDR-RTO device for treating high-concentration VOCs waste gas according to claim 17, wherein: The opening of the detonation pulse wave reactor tube end plate of the PDR high-temperature pulse wave reactor has an internal turbulence facility to promote turbulent mixing of combustion air / low-concentration VOCs exhaust gas and high-concentration VOCs exhaust gas.

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