A method for treating organic pharmaceutical hazardous waste

Abstract

This invention discloses a method for treating organic pharmaceutical-derived hazardous waste, belonging to the technical field of organic pharmaceutical-derived hazardous waste treatment. It addresses the problems of complex treatment processes, low efficiency, and difficulty in ensuring the safety and environmental friendliness of existing treatment methods for organic pharmaceutical-derived hazardous waste. The method includes: thermally drying the hazardous waste particles to obtain thermally dried particles; subjecting the thermally dried particles to anaerobic pyrolysis gasification to obtain decomposed particles and pyrolysis gas; coking the decomposed particles to obtain coked particles; subjecting the coked particles to aerobic incineration to obtain combusted particles. During aerobic incineration, the coked particles exhibit a smoldering state, releasing heat during combustion, which provides heat for coking, anaerobic pyrolysis gasification, and thermal drying; and vitrifying the combusted particles to complete the treatment of the organic pharmaceutical-derived hazardous waste. This invention can be used for the treatment of organic pharmaceutical-derived hazardous waste.

Description

Technical Field

[0001] This invention belongs to the field of organic pharmaceutical hazardous waste treatment technology, and particularly relates to a method for treating organic pharmaceutical hazardous waste. Background Technology

[0002] With the booming development of the pharmaceutical industry, the amount of organic pharmaceutical-derived hazardous waste generated is increasing daily. This type of organic pharmaceutical-derived hazardous waste has a complex composition, usually containing a variety of organic compounds, heavy metals, and biologically active substances. If not handled properly, it can pose a serious threat to the environment and human health.

[0003] Currently, direct combustion is a common treatment method for organic pharmaceutical hazardous waste. However, the process is extremely complex.

[0004] Before combustion, organic pharmaceutical hazardous waste needs to undergo strict pretreatment. After combustion, the organic pharmaceutical hazardous waste will produce a large amount of exhaust gas containing harmful substances such as dioxins. The removal of dioxins requires specialized adsorption and decomposition equipment, and the treatment temperature and time conditions are very demanding.

[0005] The complexity of processing organic medicinal materials leads to high costs, low efficiency, and difficulty in ensuring safety and environmental friendliness. There is an urgent need to develop more efficient and convenient processing technologies. Summary of the Invention

[0006] Based on the above analysis, the present invention aims to provide a method for treating organic pharmaceutical hazardous waste, in order to solve the problems of complex treatment processes, low treatment efficiency, and difficulty in ensuring the safety and environmental protection of the treatment process in the prior art.

[0007] The objective of this invention is mainly achieved through the following technical solutions.

[0008] This invention provides a method for treating organic pharmaceutical hazardous waste, comprising the following steps:

[0009] Step 1: Heat dry the hazardous waste particles to obtain heat-dried particles;

[0010] Step 2: The heat-dried particles are subjected to anaerobic pyrolysis and gasification to obtain decomposed particles and pyrolysis gas;

[0011] Step 3: Coke the decomposed particles to obtain coke particles;

[0012] Step 4: The coking particles are subjected to oxygen-enriched combustion to obtain combusted particles. During the oxygen-enriched combustion process, the coking particles are in a smoldering state and release heat during combustion. The heat generated provides heat for coking, oxygen-deficient pyrolysis gasification and thermal drying.

[0013] Step 5: Vitrify the particles after combustion to complete the treatment of organic pharmaceutical hazardous waste.

[0014] Furthermore, in step 2, the oxygen content of the environment for anaerobic pyrolysis and gasification is 6%~8%.

[0015] Furthermore, the oxygen content in the oxygen-enriched combustion environment is 20% to 30%.

[0016] Furthermore, in step 1, the heat drying temperature is 180~250℃.

[0017] Furthermore, in step 2, the temperature for anaerobic pyrolysis and gasification is 450~550℃.

[0018] Furthermore, in step 3, the coking temperature is 850~950℃.

[0019] Furthermore, in step 4, the temperature for oxygen-enriched combustion is 1250~1350℃.

[0020] Furthermore, in step 5, the vitrification temperature is 1450~1550℃.

[0021] Furthermore, the heat generated by the combustion of the pyrolysis gas produced in step 2 preheats the air required for oxygen-enriched combustion.

[0022] Furthermore, the following steps are included before step 1:

[0023] The hazardous waste slurry is sequentially dehydrated, dried, and granulated to obtain hazardous waste particles.

[0024] Compared with the prior art, the present invention can achieve at least one of the following beneficial effects:

[0025] A) The method for treating organic pharmaceutical hazardous waste provided by the present invention involves sequentially subjecting the hazardous waste particles to thermal drying, anaerobic pyrolysis gasification, coking, oxygen-enriched incineration, and vitrification for thorough treatment.

[0026] B) The method for treating organic pharmaceutical hazardous waste provided by this invention reduces the moisture content of the hazardous waste particles through thermal drying, ensuring sufficient subsequent treatment; and through anaerobic pyrolysis gasification, the hazardous waste particles undergo thermal decomposition. Anaerobic pyrolysis gasification essentially does not produce dioxins, and the pyrolysis gas mainly includes CO, H2, and NO. X and SO XThe pyrolysis gas can be utilized subsequently, realizing the full utilization of energy in hazardous waste; through coking, further deep pyrolysis and baking are achieved, so that the particles are in a coking state; through oxygen-enriched incineration, the coking particles are in a smoldering state, releasing heat during combustion, and no dioxins are produced during the oxygen-enriched incineration process; through vitrification, the aluminosilicates in the particles after combustion vitrify to form a hard and dense glass shell, which encapsulates heavy metals, realizing the solidification and non-toxic and harmless treatment of heavy metals.

[0027] C) The method for treating organic pharmaceutical hazardous waste provided by this invention adopts a multi-temperature, multi-step treatment approach combined with anaerobic pyrolysis gasification and oxygen-enriched incineration, which can effectively improve the utilization rate of organic pharmaceutical hazardous waste, reduce treatment costs, and basically not produce dioxins during the treatment process, thus effectively preventing secondary pollution.

[0028] In this invention, the above-described technical solutions can be combined with each other to achieve more preferred combinations. Other features and advantages of this invention will be set forth in the following description, and some advantages may become apparent from the description or be learned by practicing the invention. The objects and other advantages of this invention can be realized and obtained through the embodiments described and the accompanying drawings, which are particularly pointed out. Attached Figure Description

[0029] The accompanying drawings are for illustrative purposes only and are not intended to limit the invention. Throughout the drawings, the same reference numerals denote the same parts.

[0030] Figure 1 This is a flowchart of a method for treating organic pharmaceutical hazardous waste provided in Embodiment 1 of the present invention;

[0031] Figure 2 This is a schematic diagram of the treatment equipment in the treatment method for organic pharmaceutical hazardous waste provided in Embodiment 1 of the present invention;

[0032] Figure 3 This is a flowchart of a method for treating organic pharmaceutical hazardous waste provided in Embodiment 2 of the present invention;

[0033] Figure 4 This is a schematic diagram of the dehydration device in the treatment method for organic pharmaceutical hazardous waste provided in Embodiment 2 of the present invention.

[0034] Figure label:

[0035] 101-Extrusion motor; 102-Inner cylinder; 103-Extrusion roller; 104-Hazardous waste slurry bag; 105-Outer cylinder; 106-Heating coil;

[0036] 201-Incineration air supply fan; 202-Suction fan; 203-Gasification air supply fan; 204-Primary grate; 205-Secondary grate; 206-Feeding cone; 207-Air baffle ring. Detailed Implementation

[0037] The preferred embodiments of the present invention will now be described in detail with reference to the accompanying drawings, which constitute a part of the present invention and are used together with the embodiments of the present invention to illustrate the principles of the present invention, but are not intended to limit the scope of the present invention.

[0038] Example 1

[0039] This embodiment provides a method for treating organic pharmaceutical hazardous waste. See [link to relevant documentation]. Figure 1 It includes the following steps:

[0040] Step 1: Heat-dry the hazardous waste particles (containing antibiotics, aluminosilicates and corn residue) with a moisture content of 15%~20% to obtain heat-dried particles;

[0041] Step 2: The heat-dried particles are subjected to anaerobic pyrolysis gasification with an ambient oxygen content of 6%~8% to obtain decomposed particles and pyrolysis gas.

[0042] Step 3: Coke the decomposed particles to obtain coke particles;

[0043] Step 4: The coking particles are subjected to oxygen-enriched combustion with an ambient oxygen content of 20%~30% to obtain the combustion particles. During the oxygen-enriched combustion process, the coking particles are in a smoldering state and release heat during combustion. The heat generated provides heat for coking, oxygen-deficient pyrolysis gasification and thermal drying.

[0044] Step 5: Vitrify the combustion particles before discharging them to complete the treatment of organic pharmaceutical hazardous waste.

[0045] Compared with existing technologies, the method for treating organic pharmaceutical hazardous waste provided in this embodiment involves sequentially subjecting the hazardous waste particles to thermal drying, anoxic pyrolysis gasification, coking, oxygen-enriched incineration, and vitrification for thorough treatment.

[0046] Specifically, the functions of each of the above steps are as follows:

[0047] Thermal drying can reduce the moisture content of hazardous waste particles, ensuring thorough subsequent treatment.

[0048] Anaerobic pyrolysis gasification allows hazardous waste particles to undergo thermal decomposition. Anaerobic pyrolysis gasification essentially does not produce dioxins, and the pyrolysis gas mainly contains CO, H2, and NO. X and SO X The pyrolysis gas can be utilized in subsequent processes, thus making full use of the energy in hazardous waste.

[0049] Through coking, further deep pyrolysis and baking are achieved, causing the particles to exhibit a coking state.

[0050] Through oxygen-enriched combustion, the coking particles are in a smoldering state, releasing heat during combustion, and no dioxins are produced during the oxygen-enriched combustion process.

[0051] Vitrification is achieved by vitrifying the aluminosilicates in the particles after combustion to form a hard and dense glass shell. This glass shell encapsulates heavy metals, enabling the solidification and non-toxic, harmless treatment of heavy metals.

[0052] In summary, the above-mentioned treatment methods for organic pharmaceutical hazardous waste, which combine multi-temperature, multi-step treatment with anaerobic pyrolysis gasification and oxygen-enriched incineration, can effectively improve the utilization rate of organic pharmaceutical hazardous waste, reduce treatment costs, and generate virtually no dioxins during the treatment process, thus effectively preventing secondary pollution.

[0053] It should be noted that dioxins are a class of highly toxic tricyclic aromatic organic compounds. The most toxic is 2,3,7,8-tetrachlorodibenzo-p-dioxin, which is 1,000 times more toxic than potassium cyanide (KCN). Therefore, it is known as "the most toxic substance on Earth". Because it is difficult to degrade and eliminate naturally once it seeps into the environment, it is also known as "the poison of the century".

[0054] Organic hazardous wastes such as biomass, antibiotic pharmaceutical residues, and municipal solid waste typically contain large amounts of chlorine, which easily generates dioxin-containing pollutants in traditional incinerators. The main temperature range for dioxin formation during incineration is 250–500°C, with 300–450°C being the peak temperature range. When the incineration temperature reaches above 800°C, dioxins and their precursors can be completely decomposed, reducing dioxin production. The internationally recognized incineration control standard is a residence time of ≥2 seconds at 850°C. However, the burnout temperature of organic hazardous waste is usually below 500°C, making it difficult to maintain a high temperature of 850°C in the incinerator. This is the dilemma that current incineration technologies struggle to avoid dioxin formation.

[0055] The process of dioxin generation during the incineration of organic hazardous waste is controlled by temperature and oxygen content. This embodiment avoids dioxin generation by increasing temperature and limiting oxygen conditions, changing the thermal treatment of organic hazardous waste to oxygen-limited pyrolysis, forming a reducing process that inhibits the formation of dioxins through chemical chains. The carbon content of the pyrolyzed hazardous waste increases dramatically, significantly improving energy density, allowing for further oxygen-controlled combustion to achieve a combustion temperature of 1300℃, again preventing dioxin formation. The heat energy generated by combustion is used to power the oxygen-limited pyrolysis, achieving cascaded energy utilization.

[0056] In order to ensure the efficiency and effect of hot drying, for example, in step 1 above, the hot drying temperature is 180~250℃.

[0057] In order to ensure that the anoxic pyrolysis gasification is fully carried out, the temperature of the anoxic pyrolysis gasification in step 2 above is 450~550℃.

[0058] To ensure sufficient coking, the coking temperature in step 3 above is 850~950℃.

[0059] To ensure sufficient oxygenation for combustion, the oxygenation temperature in step 4 above is 1250~1350℃.

[0060] In order to ensure sufficient vitrification and form a dense glass shell, the vitrification temperature in step 5 above is 1450~1550℃.

[0061] It should be noted that limiting the temperature parameters of each step within the above range can ensure the efficient treatment of organic pharmaceutical hazardous waste and improve the treatment efficiency and effect.

[0062] Considering that using colder air for oxygenation and incineration may cause the flame to be extinguished, in the above-mentioned treatment method for organic pharmaceutical hazardous waste, the heat generated by the combustion of pyrolysis gas in step 2 is used to preheat the air required for oxygenation and incineration. By using pyrolysis gas to preheat the air in advance, the flame in the oxygenation and incineration section can be prevented from being extinguished.

[0063] It should be noted that in the above-mentioned treatment methods for organic pharmaceutical hazardous waste, thermal drying, anoxic pyrolysis gasification, coking, oxygen-enriched incineration, and vitrification are carried out in the same chamber. In the vertical direction, thermal drying, anoxic pyrolysis gasification, coking, oxygen-enriched incineration, and vitrification are carried out sequentially from top to bottom in the chamber.

[0064] For example, in order to integrate thermal drying, anaerobic pyrolysis gasification, coking, oxygen-enriched incineration, and vitrification into a single chamber, the above-mentioned method for treating organic pharmaceutical hazardous waste employs a treatment device with the following structure:

[0065] See Figure 2 The processing equipment includes a furnace body and an incineration air supply fan 201. The inner cavity of the furnace body is divided into a hot drying section, an anoxic pyrolysis gasification section, a coking section, an oxygen-enriched incineration section, a vitrification section, and a discharge section from top to bottom. The side wall of the hot drying section has a hazardous waste inlet, and the anoxic pyrolysis gasification section has a pyrolysis gas outlet. The incineration air supply fan 201 is connected to the vitrification section and supplies air or oxygen to the oxygen-enriched incineration section through the vitrification section.

[0066] To facilitate the discharge of pyrolysis gas, the pyrolysis gas outlet of the aforementioned anoxic pyrolysis gasification section is connected to the suction fan 202. The suction fan 202 extracts the pyrolysis gas generated in the anoxic pyrolysis gasification section out of the integrated furnace, thus achieving smooth discharge of the pyrolysis gas.

[0067] It is worth noting that the suction fan 202 will draw airflow into the furnace. In order to avoid drawing the flame in the combustion section to the coking section and the anoxic pyrolysis gasification section, which would cause the hazardous waste particles to burn prematurely and produce pollutants such as dioxins, the anoxic pyrolysis gasification section is provided with a pyrolysis section air inlet. The pyrolysis section air inlet is connected to the gasification air supply fan 203 to supply appropriate airflow (e.g., air) into the anoxic pyrolysis gasification section, thereby avoiding excessive negative pressure in the anoxic pyrolysis gasification section.

[0068] In order to control the falling speed of hazardous waste particles and ensure sufficient reaction, a primary grate 204 is provided between the oxygen thermal decomposition section and the coking section, and a secondary grate 205 is provided between the vitrification section and the discharge section. In this way, the setting of the primary grate 204 and the secondary grate 205 can better control the falling speed of hazardous waste particles, so as to better carry out anoxic pyrolysis gasification and vitrification.

[0069] In order to achieve uniform material distribution, the above-mentioned treatment equipment also includes a feeding cone 206 located below the primary grate 204. The feeding cone 206 has feeding holes and is cone-shaped. After thermal decomposition, the hazardous waste particles fall onto the feeding cone 206 after passing through the grate and are evenly distributed along the cone-shaped feeding cone 206 into the coking section and the oxygen-enriched combustion section.

[0070] Considering that the hot drying section, the anoxic pyrolysis gasification section, the coking section, the oxygen-enriched combustion section, the vitrification section, and the discharge section are located in the same furnace body and are interconnected, in order to achieve anoxic pyrolysis gasification and oxygen-enriched combustion, the above-mentioned treatment equipment also includes an air-blocking ring 207 located between the oxygen-enriched combustion section and the discharge section. By setting the air-blocking ring 207, the air supplied to the vitrification section can be blocked, so as to achieve anoxic pyrolysis gasification and oxygen-enriched combustion.

[0071] In order to further control the anoxic pyrolysis gasification and oxygen-enriched combustion, the projection of the baffle ring 207 and the feeding cone 206 on the radial side of the furnace body completely covers the radial section of the furnace body. In this way, the baffle ring 207 and the feeding cone 206 work together to ensure that the air supplied from the vitrification section can flow smoothly into the oxygen-enriched combustion section, and also to prevent air from flowing directly into the anoxic pyrolysis gasification section and affecting the anoxic pyrolysis gasification.

[0072] Example 2

[0073] The method for treating organic pharmaceutical hazardous waste provided in this embodiment is basically the same as the method for treating organic pharmaceutical hazardous waste provided in Embodiment 1, except that:

[0074] To enable the conversion of hazardous waste slurry into hazardous waste pellets, see [link / reference]. Figure 3 Before step 1 above, the following steps are also included:

[0075] The hazardous waste slurry is sequentially dehydrated, dried, and granulated to obtain hazardous waste particles.

[0076] Specifically, dehydration includes the following steps:

[0077] Step a: Place the hazardous waste slurry bag 104 into the dewatering cylinder;

[0078] Step b: Turn on the extrusion motor 101 to drive the hazardous waste slurry bag 104 to move closer to the extrusion roller 103 and make contact with the extrusion roller 103;

[0079] Step c: Continue to drive the hazardous waste slurry bag 104 to move closer to the extrusion roller 103, turn on the extrusion roller 103, and the extrusion roller 103 dewaters the hazardous waste slurry in the hazardous waste slurry bag 104.

[0080] In this way, the high-pressure mechanical pressure of the extrusion roller 103 is applied directly to the material particles, which can diffuse the mechanical pressure into the particles of hazardous waste slurry, effectively extruding and dewatering the inside of the particles, improving the dewatering rate of hazardous waste and ensuring the dewatering effect.

[0081] For example, the above-mentioned dehydration uses a dehydration device with the following structure, see [link to device]. Figure 4 It includes an extrusion motor 101, a dewatering cylinder and an extrusion roller 103. Hazardous waste slurry bag 104 is placed in the dewatering cylinder, the extrusion roller 103 is placed above the dewatering cylinder, and the extrusion motor 101 is located below the dewatering cylinder.

[0082] To further promote the dewatering of hazardous waste slurry, the dewatering cylinder, exemplarily, includes an inner cylinder 102, an outer cylinder 105, and multiple heating coils 106. The outer cylinder 105 is located outside the inner cylinder 102, with a gap between them. The heating coils 106 are located within this gap, and are arranged vertically in sequence. From bottom to top, the temperature of the heating coils 106 gradually increases. For example, the temperature of the uppermost heating coil 106 is above 100°C, and the temperature of the lowermost heating coil 106 is 50-70°C. Because the uppermost heating coil 106 has a higher heating temperature, it can cause the moisture in the upper part of the hazardous waste slurry bag 104 to turn into steam, increasing the air pressure in the upper space of the hazardous waste slurry bag 104. This air pressure further promotes the discharge of moisture from the hazardous waste slurry bag 104.

[0083] In order to effectively heat the upper surface of the hazardous waste slurry bag to generate steam, the structure of the extrusion roller 103 specifically includes a roller body and a heating element disposed within the roller body.

[0084] It should be noted that the temperature of the heating element is controlled above 100℃ (e.g., 100~120℃).

[0085] The radial cross-sectional shape of the extrusion roller 103 is cam-shaped. During the compression and dewatering process, the initial position of the extrusion roller 103 is with the outer wall surface with the smallest radius facing the hazardous waste slurry bag.

[0086] During implementation, the extrusion motor 101 is turned on, driving the hazardous waste slurry bag to move closer to the extrusion roller 103 and come into contact with it. The hazardous waste slurry bag continues to move closer to the extrusion roller 103, and the extrusion roller 103 performs a first-stage pressure solidification and dewatering of the hazardous waste slurry in the hazardous waste slurry bag. When the hazardous waste slurry bag reaches the preset position, the extrusion motor 101 is turned off, the hazardous waste slurry bag stops moving, and the extrusion roller 103 is turned on. The rotation of the extrusion roller 103 increases the outer diameter of the extrusion roller 103 corresponding to the hazardous waste slurry bag, and continues to depressurize the hazardous waste for a second-stage pressure solidification and dewatering.

[0087] It should be noted that during the rotation of the extrusion roller 103, the outer diameter of the extrusion roller 103 corresponding to the hazardous waste slurry bag is constantly changing, and correspondingly, the mechanical pressure on the hazardous waste slurry in the hazardous waste slurry bag is also constantly changing.

[0088] When the mechanical pressure decreases, gaps will form between the hazardous waste particles in the hazardous waste slurry bag, causing the position of the hazardous waste particles to change.

[0089] When the mechanical pressure increases, the hazardous waste slurry in the hazardous waste slurry bag will be further compressed and dewatered, thereby effectively improving the uniformity and dewatering rate of dewatering.

[0090] Furthermore, during the rotation of the extrusion roller 103, when the mechanical pressure decreases, the space above the hazardous waste slurry bag increases, and the increased space can accommodate more steam. When the mechanical pressure increases, it will force the steam to flow downwards, and the air pressure will further promote the discharge of moisture from the hazardous waste slurry bag.

[0091] The above description is only a preferred embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any changes or substitutions that can be easily conceived by those skilled in the art within the scope of the technology disclosed in the present invention should be included within the scope of protection of the present invention.

Claims

1. A method for treating organic pharmaceutical hazardous waste, characterized in that, Includes the following steps: Step 1: Thermally dry the hazardous waste particles to obtain thermally dried particles; Step 2: Perform anoxic pyrolysis gasification on the thermally dried particles to obtain decomposed particles and pyrolysis gas. The oxygen content of the anoxic pyrolysis gasification environment is 6%~8%; Step 3: Coke the decomposed particles to obtain coke particles; Step 4: Perform oxygen-enriched incineration on the coke particles to obtain combusted particles. During the oxygen-enriched incineration process, the coke particles are in a smoldering state, and the combustion releases heat, which provides heat for coking, anoxic pyrolysis gasification, and thermal drying; Step 5: Vitrify the combusted particles to complete the treatment of organic pharmaceutical hazardous waste; Before step 1, the following steps are also included: the hazardous waste slurry is dehydrated, dried and granulated in sequence to obtain hazardous waste particles; The dewatering process includes the following steps: placing the hazardous waste slurry bag in the dewatering cylinder; turning on the extrusion motor to drive the hazardous waste slurry bag to move closer to the extrusion cylinder and contact it; continuing to drive the hazardous waste slurry bag closer to the extrusion cylinder, where the extrusion cylinder performs a first-stage dewatering of the hazardous waste slurry in the bag; when the hazardous waste slurry bag reaches the preset position, the extrusion motor is turned off, and the bag stops moving; turning on the extrusion cylinder, which rotates to increase the outer diameter of the extrusion cylinder corresponding to the hazardous waste slurry bag, and continuing to depressurize the hazardous waste for a second-stage dewatering. The dewatering cylinder includes an inner cylinder, an outer cylinder, and multiple heating coils. The outer cylinder is located outside the inner cylinder, and there is a gap between the inner and outer cylinders. The heating coils are located in the gap, and the multiple heating coils are arranged vertically in sequence. From bottom to top, the temperature of the heating coils gradually increases, with the temperature of the uppermost heating coil exceeding 100°C and the temperature of the lowermost heating coil being 50-70°C. The extrusion roller includes a roller body and a heating element disposed within the roller body. The temperature of the heating element is controlled to be above 100°C. The radial cross-sectional shape of the extrusion roller is cam-shaped, and the initial position of the extrusion roller is with the outer wall surface with the smallest radius facing the hazardous waste slurry bag. During the rotation of the extrusion roller, the outer diameter of the extrusion roller corresponding to the hazardous waste slurry bag is constantly changing, and the mechanical pressure on the hazardous waste slurry inside the hazardous waste slurry bag is also constantly changing. When the mechanical pressure decreases, gaps are generated between the hazardous waste particles in the hazardous waste slurry bag, and the position of the hazardous waste particles changes. When the mechanical pressure increases, the hazardous waste slurry inside the hazardous waste slurry bag is compressed and dehydrated. When the mechanical pressure decreases, the space above the hazardous waste slurry bag increases, and the increased space can hold steam. When the mechanical pressure increases, the steam flows downward, and the air pressure promotes the discharge of water from the hazardous waste slurry bag. The processing equipment used in the treatment method includes a furnace body. The inner cavity of the furnace body is divided from top to bottom into a hot drying section, an anoxic pyrolysis gasification section, a coking section, an oxygen-enriched combustion section, a vitrification section, and a discharge section. A primary grate is provided between the anoxic pyrolysis section and the coking section. The processing equipment also includes a feeding cone located below the primary grate and a baffle ring located between the oxygen-enriched combustion section and the discharge section. The projections of the baffle ring and the feeding cone on the radial direction of the furnace body completely cover the radial section of the furnace body. The pyrolysis gas outlet of the anoxic pyrolysis gasification section is connected to the suction fan, and the pyrolysis gasification section has a pyrolysis section air inlet, which is connected to the gasification air supply fan; the heat generated by the combustion of the pyrolysis gas in step 2 preheats the air required for oxygen-enriched combustion.

2. The method for treating organic pharmaceutical hazardous waste according to claim 1, characterized in that, The oxygen content in the oxygen-enriched incineration environment is 20% to 30%.

3. The method for treating organic pharmaceutical hazardous waste according to claim 1, characterized in that, In step 1, the heat drying temperature is 180~250℃.

4. The method for treating organic pharmaceutical hazardous waste according to claim 1, characterized in that, In step 2, the temperature of the anoxic pyrolysis gasification is 450~550℃.

5. The method for treating organic pharmaceutical hazardous waste according to claim 1, characterized in that, In step 3, the coking temperature is 850~950℃.

6. The method for treating organic pharmaceutical hazardous waste according to claim 1, characterized in that, In step 4, the temperature of the oxygen-enriched incineration is 1250~1350℃.

7. The method for treating organic pharmaceutical hazardous waste according to claim 1, characterized in that, In step 5, the vitrification temperature is 1450~1550℃.

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