A micro fluidized bed reactor and method for gasification of multi-source resin waste

Abstract

The application discloses a micro fluidized bed reactor for gasifying multi-source resin waste, and discloses a method for gasifying multi-source resin waste by using the reactor. The reactor comprises a gas inlet cavity, a gas mixing cavity and a reaction cavity. The gas inlet cavity is connected with an external gas cylinder through a gas inlet. A first air distribution plate is arranged between the gas inlet cavity and the gas mixing cavity. A steam generating pipe is further connected with the gas mixing cavity. A steam outlet of the steam generating pipe is connected with the gas mixing cavity. An electric heating belt is arranged on the steam generating pipe. A second air distribution plate is arranged between the gas mixing cavity and the reaction cavity. The reaction cavity is provided with a feeding port and a gas outlet. A heating device is further arranged on the reactor. The application has high target synthesis gas yield and high resin conversion rate.

Description

Technical Field

[0001] This invention relates to a micro fluidized bed reactor for gasifying multi-source resin waste, and also to a method for gasifying multi-source resin waste using the above-described reactor. Background Technology

[0002] Currently, landfilling and incineration remain the primary methods for treating multi-source resin waste. Due to the extremely strong chemical inertness of multi-source resin waste, it is difficult to degrade naturally, leading to long-term land occupation of land resources through simple landfilling. While direct incineration can achieve significant volume reduction and heat recovery, the secondary environmental limitations it generates remain prominent: during combustion, multi-source resin waste is prone to producing dioxins and furans (persistent organic pollutants) due to uneven temperature distribution, thus harming the environment. Gasification technology, as a typical thermochemical conversion method, can convert organic solid waste into combustible syngas at high temperatures, thereby achieving the resource utilization of resin waste.

[0003] Microfluidized beds can achieve gas-solid reactions under isothermal conditions. Due to their controllable gas flow, temperature, and feed rate, as well as their compatibility with various analytical instruments, they have been widely used in fluidized bed gasification experimental research. Currently, there are no reports on using microfluidized beds coupled with air-steam gasification technology to treat multi-source resin waste. Summary of the Invention

[0004] Purpose of the invention: The purpose of this invention is to provide a micro fluidized bed reactor for gasifying multi-source resin waste. Another purpose of this invention is to provide a method for gasifying multi-source resin waste using the above-mentioned reactor. This invention has high target syngas yield and high resin conversion rate.

[0005] Technical Solution: The micro fluidized bed reactor for gasifying multi-source resin waste according to the present invention includes an inlet chamber, a gas mixing chamber, and a reaction chamber; the inlet chamber is connected to an external gas cylinder through an inlet; a primary air distribution plate is provided between the inlet chamber and the gas mixing chamber; the gas mixing chamber is also connected to a steam generating pipe, the steam outlet of the steam generating pipe is connected to the gas mixing chamber, and an electric heating belt (heating tape) is sleeved on the steam generating pipe; a secondary air distribution plate is provided between the gas mixing chamber and the reaction chamber; the reaction chamber has a feed inlet and a gas outlet (the gas outlet is connected to the gas inlet of an external process mass spectrometer); it also includes a heating device sleeved outside the reactor; wherein, the primary air distribution plate is provided between the gas mixing chamber and the reaction chamber; the secondary air distribution plate is provided between the gas mixing chamber and the reaction chamber; the reaction chamber has a feed inlet and a gas outlet (the gas outlet is connected to the gas inlet of an external process mass spectrometer); and a heating device is also included outside the reactor; wherein, the primary air distribution plate is connected to the gas mixing chamber, the gas mixing chamber is connected to the gas inlet of an external process mass spectrometer. Both the primary and secondary air distribution plates are glass plates with through holes. The primary air distribution plate has a hole diameter of 30µm to 60µm and an opening rate of 40% to 45%. This size can both initially stabilize the reaction gas flow rate to form a stable reaction gas jet and ensure that the reaction gas and steam are fully mixed before being input into the secondary air distribution plate. At the same time, it can also ensure that the mixed gas input into the reaction chamber obtains a uniform airflow organization. The secondary air distribution plate has a hole diameter of 30µm to 60µm and an opening rate of 30% to 40%. This size can both fully ensure the mixed gas flow rate to maintain the fluidized state of the multi-source resin waste and support the material to prevent the material or post-reaction particles from falling into the gas chamber (gas mixing chamber).

[0006] A filter plate is provided at the gas outlet. The filter plate is a glass plate with through holes, and the pore size of the filter plate is 30µm~60µm, with an opening rate of 30%~40%. This size can prevent materials or reaction particles from falling into the gas outlet, while ensuring that the target synthesis gas can pass smoothly through the filter plate and be discharged from the gas outlet.

[0007] The reaction chamber is also connected to a thermocouple temperature measuring tube, and a thermocouple (temperature sensor) is placed inside the thermocouple temperature measuring tube.

[0008] The reaction chamber has a length of 30mm-40mm and an inner diameter of 15mm-30mm. This size enhances the contact efficiency between multi-source resin waste and the mixed gas, and utilizes the confined space effect to strengthen heat and mass transfer efficiency, resulting in a more uniform temperature field distribution and increased reaction rate. It also provides sufficient residence time for the gas-solid reaction, promoting reaction depth and improving conversion rate. The gas mixing chamber has a length of 120mm-160mm and an inner diameter of 15mm-30mm. This size ensures thorough mixing of the reactant gas and steam, while also allowing the steam to remain in a gaseous state. The steam generating pipe has a length of 120mm-150mm and an inner diameter of 7mm-9mm. This size ensures good heat transfer efficiency for vaporizing deionized water into steam, and also ensures that the steam at the outlet can fully contact the reactant gas jet for thorough mixing.

[0009] The method for treating multi-source resin waste using the above-mentioned reactor gasification includes the following steps:

[0010] (1) The reaction chamber is filled with quartz sand, the particle size of which is larger than the pore size of the through holes on the secondary air distribution plate and the filter plate; quartz sand can effectively improve the mass and heat transfer efficiency of the gas-solid reaction in the reaction chamber.

[0011] (2) The temperature of the reaction chamber is raised to not less than 950°C by a heating device, and the reaction chamber is purged with Ar gas for 10-20 minutes.

[0012] (3) After purging, resin powder is sent into the reaction chamber by pulse injection (i.e., resin powder is sent into the reaction chamber by argon gas with a certain pressure). At this time, the temperature of the electric heating belt is heated to not less than 200°C. Deionized water is injected into the opening of the steam generating tube away from the gas mixing chamber by a micro injection pump. At the same time, the flow regulating valve is started to introduce the reaction gas into the reactor through the gas inlet. After passing through the primary air distribution plate, the reaction gas is mixed with steam in the gas mixing chamber and then enters the reaction chamber through the secondary air distribution plate. The vapor partial pressure of water vapor in the mixed gas is 10~20%. Gas is generated after 15~40s of reaction and the reaction is completed after 1~3min.

[0013] During the reaction, the yield of syngas (CO, H2, CH4, CO) was monitored in real time. To ensure the normal operation of the process mass spectrometer, the syngas was first passed through a drying tube containing 200 mL of 1 mol / L sodium carbonate solution and color-changing silica gel before being introduced into the process mass spectrometer for detection. Before the experiment, the process mass spectrometer needed to be calibrated by passing standard gases to obtain a standard curve; the standard gases included at least high-purity argon, 500 ppm H2, CO, CO2, and CH4, and 1000 ppm H2, CO, CO2, and CH4.

[0014] Beneficial effects: Compared with the prior art, the present invention has the following significant advantages: the present invention has a high target syngas yield and a high resin conversion rate; specifically, the H2 yield can reach 0.812 m³ / s. 3 / kg, CH4 production can reach 0.034m 3 / kg, CO production can reach 0.797m 3 / kg, CO2 production can reach 0.278m³. 3 / kg, the total syngas production can reach 1.921m³. 3 / kg, with a resin conversion rate of up to 92.8%. Attached Figure Description

[0015] Figure 1 This is a schematic diagram of the micro fluidized bed reactor for gasification treatment of multi-source resin waste according to the present invention;

[0016] Figure 2 The synthesis gas yields of Examples 1-3 and Comparative Example 1 of this invention;

[0017] Figure 3 The conversion rate of waste circuit board resin powder in Examples 1-3 and Comparative Example 1 of the present invention;

[0018] Figure 4 The synthesis gas yields of Examples 4-6 and Comparative Example 2 of this invention;

[0019] Figure 5 The conversion rates of the dry film residue in Examples 4-6 and Comparative Example 2 of this invention are shown. Detailed Implementation

[0020] like Figure 1 As shown, the present invention discloses a micro fluidized bed reactor for gasifying multi-source resin waste, comprising an inlet chamber 8, a gas mixing chamber 9, and a reaction chamber 2. The inlet chamber 8 is connected to an external gas cylinder via an inlet 11. A primary air distribution plate 6 is provided between the inlet chamber 8 and the gas mixing chamber 9. The gas mixing chamber 9 is also connected to a steam generating pipe 5, the steam outlet of which is connected to the gas mixing chamber 9. An electric heating belt is fitted over the steam generating pipe. A secondary air distribution plate 4 is provided between the gas mixing chamber 9 and the reaction chamber 2. The reaction chamber 2 has a feed inlet 3 and a gas outlet 12 (the gas outlet 12 is connected to the gas inlet of an external process mass spectrometer). The reactor of the present invention also includes a heating device fitted outside the reactor. The primary air distribution plate 6 and the secondary air distribution plate 4 are connected to the gas mixing chamber 9 via an inlet 11. All air distribution plates 4 are glass plates with through holes; the thickness of the primary air distribution plate 6 is 4mm~6mm, the hole diameter is 30µm~60µm, and the opening rate is 40%~45%; this size can both initially stabilize the reaction gas flow rate to form a stable reaction gas jet and ensure that the reaction gas and steam are fully mixed before being input into the secondary air distribution plate 4; at the same time, it can also ensure that the mixed gas input into the reaction chamber 2 obtains a uniform airflow organization; the thickness of the secondary air distribution plate 4 is 4mm~6mm, the hole diameter is 30µm~60µm, and the opening rate is 30%~40%; this size can both fully ensure the mixed gas flow rate to maintain the fluidized state of the multi-source resin waste and support the material to prevent the material or post-reaction particles from falling into the gas chamber (gas mixing chamber).

[0021] The reactor of this invention uses a primary air distribution plate 6 to initially stabilize the reaction gas flow rate, ensuring that the reaction gas forms a uniform and stable gas jet, thereby enhancing the contact and mixing of the reaction gas and steam to form a uniform mixture. The steam generating pipe 5 can be set to above 200°C to ensure that the deionized water is vaporized into steam and will not condense before entering the reaction chamber 2. The secondary air distribution plate 4 ensures that the mixed gas forms a uniform and stable gas jet to enhance gas-solid contact, while stabilizing the flow rate. After the flow rate is stabilized, the gas-solid contact is more uniform. The feeding method of this invention is to introduce inert pulsed gas with a certain pressure, thereby ensuring that the introduced gas does not participate in the vaporization reaction. At the same time, a certain pulsed gas pressure can ensure that the resin waste particles are all transported into the reaction chamber 2 for sufficient gas-solid contact.

[0022] A filter plate 1 is installed at the gas outlet 12. The filter plate 1 is a glass plate with through holes. The thickness of the filter plate 1 is 4mm~6mm, the pore size is 30µm~60µm, and the porosity is 30%~40%. This size can prevent materials or particulate matter after the reaction from entering the gas outlet 12, while ensuring that the target synthesis gas can pass smoothly through the filter plate 1 and be discharged from the gas outlet 12. That is, the filter plate 1 only allows the synthesis gas generated by the gasification reaction to pass through, which can prevent particles from entering the gas outlet 12 and causing blockage of subsequent pipelines.

[0023] The reaction chamber 2 is also connected to a thermocouple sensing tube 7, inside which a thermocouple 10 (temperature sensor) is placed. The thermocouple sensing tube 7 has a length of 100mm~120mm, a wall thickness of 3mm~5mm, and an inner diameter of 5mm~7mm. This size can both fix the thermocouple 10 to ensure that the thermocouple 10 collects temperature data at the fixed point, and protect the thermocouple 10 by reducing the impact of airflow or particles on the thermocouple.

[0024] The reactor is entirely made of quartz glass. Reaction chamber 2 has a length of 30mm-40mm and an inner diameter of 15mm-30mm. This size enhances the contact efficiency between multi-source resin waste and the mixed gas, and utilizes the confined space effect to strengthen heat and mass transfer efficiency, resulting in a more uniform temperature field distribution and increased reaction rate. It also provides sufficient residence time for the gas-solid reaction, promoting reaction depth and improving conversion rate. Gas mixing chamber 9 has a length of 120mm-160mm and an inner diameter of 15mm-30mm. This size ensures thorough mixing of the reactant gas and steam while maintaining the steam in a gaseous state. Steam generating pipe 5 has a length of 120mm-150mm, a wall thickness of 1.5mm-3mm, and an inner diameter of 7mm-9mm. This size ensures good heat transfer efficiency for vaporizing deionized water and guarantees sufficient contact between the steam and the reactant gas jet at the outlet for thorough mixing. The feed pipe 3 has a length of 130mm~150mm, a wall thickness of 5mm~7mm, and an inner diameter of 9mm~12mm. This size ensures that the multi-source resin waste is fully filled into the feed pipe 3, creating a certain pressure difference between the inside and outside of the feed pipe 3 to ensure that the pulsed gas delivers the multi-source resin waste particles to the reaction chamber 2. It also has a reasonable pipe wall thickness to withstand the impact intensity brought by the pulsed gas. The outer diameters of the primary air distribution plate 6, the secondary air distribution plate 4, and the filter plate 1 are consistent with the inner diameter of the reactor chamber.

[0025] Example 1

[0026] The method for treating multi-source resin waste using the above-mentioned reactor gasification includes the following steps:

[0027] (1) Quartz sand with a particle size of 80~120µm is loaded into the reaction chamber. The length (height) of the reaction chamber is 30mm and the inner diameter is 15mm. At this time, the amount of quartz sand added is 0.35g. The thermocouple is inserted into the thermocouple measuring tube, and then the reactor is placed into the furnace (heating device). The thickness of the first-stage air distribution plate is 4mm, the pore size is 30µm, and the opening rate is 45%. The thickness of the second-stage air distribution plate is 4mm, the pore size is 50µm, and the opening rate is 40%. The thickness of the filter plate is 4mm, the pore size is 30µm, and the opening rate is 40%.

[0028] (2) Screen waste circuit board resin powder with a particle size of 100~120μm, dry it in a drying oven at 105℃ for 6h to constant weight, weigh 6mg of waste circuit board resin powder (error ±0.05mg), and load the weighed sample into the feed tube; the feed tube is 150mm long, 7mm thick, and 12mm in diameter.

[0029] (3) Set the heating program so that the temperature of the reaction chamber rises from room temperature to 950°C at a heating rate of 30°C / min. During the heating and isothermal process, argon gas with a flow rate of 100 mL / min is continuously introduced into the reactor to purge the reactor for about 20 min until the baseline signals of each gas phase component of the mass spectrometer are stable.

[0030] (4) The pulse pressure is set to 0.2MPa by the pressure reducing valve. The resin powder in the feed pipe is injected into the reaction chamber by pulse injection. The temperature of the electric heating belt is heated to 200℃. Deionized water is injected into the steam generating pipe on the side away from the gas mixing chamber by the micro injection pump. The injection flow rate is 37µL / min. At the same time, the flow regulating valve is started to introduce the reaction gas into the reactor through the gas inlet (the reaction gas entering from the gas inlet includes O2 and Ar. The total volume flow rate of the reaction gas is 460mL / min, the flow rate of O2 is 20mL / min, and the flow rate of Ar is 440mL / min). After the reaction gas passes through the primary air distribution plate, it is mixed with steam in the gas mixing chamber. The vapor partial pressure of water vapor in the mixed gas is 10%. The mixed gas enters the reaction chamber through the secondary air distribution plate to make the bed material reach the fluidized state. The length of the gas mixing chamber is 120mm and the inner diameter is 15mm. The length of the steam generating pipe is 120mm, the wall thickness is 1.5mm, and the inner diameter is 7mm.

[0031] (5) Gas begins to be generated after 40 seconds of reaction, and the reaction is completed in about 2.9 minutes (judgment of reaction completion time: the reaction is considered to be terminated after the response curves of each gas phase component smoothly return to the baseline).

[0032] The yield of syngas (CO, H2, CH4, CO) was monitored in real time during the reaction. To ensure the normal operation of the process mass spectrometer, the syngas was first passed through a drying tube containing 200 mL of 1 mol / L sodium carbonate solution and color-changing silica gel before being introduced into the process mass spectrometer for detection. The detection results are as follows: Figures 2-3 As shown, the target H2 yield in the syngas is 0.092 m³. 3 / kg, CH4 production was 0.019m 3 / kg, CO production is 0.319m 3 / kg, CO2 production is 0.029m 3 / kg, the total syngas production is 0.459m³. 3 / kg, the conversion rate of waste circuit board resin powder is 78.5%.

[0033] Given the sensitivity linear drift phenomenon caused by vacuum instability in process mass spectrometers during long-duration detection, in order to ensure high accuracy of quantitative conversion, this method immediately introduces 500ppm and 1000ppm multi-component standard gases into the system for three-point linear calibration after each loop test. The product current signal is linearly calculated by periodically correcting the calibration curve, thereby obtaining the transient partial pressure and yield of the target syngas with high confidence.

[0034] Example 2

[0035] Example 2 is the same as Example 1, except that in step (4), the temperature of the electric heating belt is heated to 200°C, and deionized water is injected into the steam generating pipe at the opening away from the gas mixing chamber using a micro injection pump. The injection flow rate is 55µL / min. At the same time, the flow regulating valve is activated to introduce the reaction gas into the reactor through the inlet (the reaction gas entering through the inlet includes O2 and Ar, the total volume flow rate of the reaction gas is 460mL / min, the flow rate of O2 is 20mL / min, and the flow rate of Ar is 440mL / min). After passing through the primary air distribution plate, the reaction gas is mixed with steam in the gas mixing chamber. The vapor partial pressure of water vapor in the mixed gas is 15%. The mixed gas enters the reaction chamber through the secondary air distribution plate to make the bed material reach the fluidized state. Gas is generated after 30s of reaction, and the reaction is completed in about 2.2min.

[0036] The yield of syngas (CO, H2, CH4, CO) was monitored in real time during the reaction. To ensure the normal operation of the process mass spectrometer, the syngas was first passed through a drying tube containing 200 mL of 1 mol / L sodium carbonate solution and color-changing silica gel before being introduced into the process mass spectrometer for detection. The detection results are as follows: Figures 2-3 As shown, the target H2 yield in the syngas is 0.097 m³. 3 / kg, CH4 production was 0.019m 3 / kg, CO production is 0.323m 3 / kg, CO2 production is 0.035m 3 / kg, total yield was 0.474m 3 / kg, with a conversion rate of 80.89%.

[0037] Example 3

[0038] Example 3 is the same as Example 1, except that in step (4), the temperature of the electric heating belt is heated to 200°C, and deionized water is injected into the opening of the steam generating pipe away from the gas mixing chamber using a micro injection pump. The injection flow rate is 74µL / min. At the same time, the flow regulating valve is activated to introduce the reaction gas into the reactor through the air inlet (the reaction gas entering through the air inlet includes O2 and Ar, the total volume flow rate of the reaction gas is 460mL / min, the flow rate of O2 is 20mL / min, and the flow rate of Ar is 440mL / min). After passing through the primary air distribution plate, the reaction gas is mixed with steam in the gas mixing chamber. The vapor partial pressure of water vapor in the mixed gas is 20%. The mixed gas enters the reaction chamber through the secondary air distribution plate to make the bed material reach the fluidized state. Gas is generated after 20s of reaction, and the reaction is completed in about 1.5min.

[0039] The yield of syngas (CO, H2, CH4, CO) was monitored in real time during the reaction. To ensure the normal operation of the process mass spectrometer, the syngas was first passed through a drying tube containing 200 mL of 1 mol / L sodium carbonate solution and color-changing silica gel before being introduced into the process mass spectrometer for detection. The detection results are as follows: Figures 2-3 As shown, the target H2 production in the syngas is 0.1 m³. 3 / kg, CH4 production was 0.021m 3 / kg, CO production is 0.329m 3 / kg, CO2 production is 0.042m 3 / kg, total yield was 0.491m 3 / kg, with a conversion rate of 83.89%.

[0040] Comparative Example 1

[0041] The method of Comparative Example 1 is the same as that of Example 1, except that in step (4), the temperature of the electric heating belt is heated to 200°C, and deionized water is injected into the opening of the steam generating pipe away from the gas mixing chamber using a micro injection pump. The injection flow rate is 0µL / min, so that the vapor partial pressure of water vapor in the mixed gas is 0%. At the same time, the flow regulating valve is activated to introduce the reaction gas into the reactor through the air inlet (the reaction gas entering from the air inlet includes O2 and Ar, the total volume flow rate of the reaction gas is 460mL / min, the flow rate of O2 is 20mL / min, and the flow rate of Ar is 440mL / min). The reaction gas enters the reaction chamber through the primary air distribution plate and then through the secondary air distribution plate to make the bed material reach the fluidized state. Gas is generated after 50s of reaction, and the reaction is completed after about 3.5min.

[0042] The yield of syngas (CO, H2, CH4, CO) was monitored in real time during the reaction. To ensure the normal operation of the process mass spectrometer, the syngas was first passed through a drying tube containing 200 mL of 1 mol / L sodium carbonate solution and color-changing silica gel before being introduced into the process mass spectrometer for detection. The detection results are as follows: Figures 2-3 As shown, the target H2 yield in the syngas is 0.086 m³. 3 / kg, CH4 production is 0.017m 3 / kg, CO production is 0.318m 3 / kg, CO2 production is 0.017m 3 / kg, total yield was 0.438m 3 / kg, with a conversion rate of 75.43%.

[0043] Example 4

[0044] The method for treating multi-source resin waste using the above-mentioned reactor gasification includes the following steps:

[0045] (1) Quartz sand with a particle size of 80~120µm is loaded into the reaction chamber. The length of the reaction chamber is 30mm and the inner diameter is 15mm. At this time, the amount of quartz sand added is 0.5g. The thermocouple is inserted into the thermocouple measuring tube, and then the reactor is placed into the furnace (heating device). The thickness of the first-stage air distribution plate is 4mm, the pore size is 30µm, and the opening rate is 45%. The thickness of the second-stage air distribution plate is 4mm, the pore size is 50µm, and the opening rate is 40%. The thickness of the filter plate is 4mm, the pore size is 30µm, and the opening rate is 40%.

[0046] (2) Screen dry film residue with a particle size of 100~120μm, dry it in a drying oven at 105℃ for 6h to constant weight, weigh 6mg of dry film residue (error ±0.05mg), and load the weighed sample into the feed tube; the feed tube is 150mm long, 7mm thick, and 12mm in diameter.

[0047] (3) Set the heating program so that the temperature of the reaction chamber rises from room temperature to 950°C at a heating rate of 30°C / min. During the heating and constant temperature process, argon gas with a flow rate of 100 mL / min is continuously introduced into the reactor to purge the reactor for about 20 min.

[0048] (4) The pulse pressure is set to 0.2MPa by the pressure reducing valve. The dry film residue in the feed pipe is injected into the reaction chamber by pulse injection. The temperature of the electric heating belt is heated to 200℃. Deionized water is injected into the steam generating pipe on the side away from the gas mixing chamber by the micro injection pump. The injection flow rate is 40µL / min. At the same time, the flow regulating valve is started to introduce the reaction gas into the reactor through the gas inlet (the reaction gas entering from the gas inlet includes O2 and Ar. The total volume flow rate of the reaction gas is 500mL / min, the flow rate of O2 is 30mL / min, and the flow rate of Ar is 470mL / min). After the reaction gas passes through the primary air distribution plate, it is mixed with steam in the gas mixing chamber. The vapor partial pressure of water vapor in the mixed gas is 10%. The mixed gas enters the reaction chamber through the secondary air distribution plate to make the bed material reach the fluidized state. The length of the gas mixing chamber is 120mm and the inner diameter is 15mm. The length of the steam generating pipe is 120mm, the wall thickness is 1.5mm, and the inner diameter is 7mm.

[0049] (5) Gas begins to be produced after 35 seconds of reaction, and the reaction is completed in about 2.7 minutes.

[0050] The yield of syngas (CO, H2, CH4, CO) was monitored in real time during the reaction. To ensure the normal operation of the process mass spectrometer, the syngas was first passed through a drying tube containing 200 mL of 1 mol / L sodium carbonate solution and color-changing silica gel before being introduced into the process mass spectrometer for detection. The detection results are as follows: Figures 4-5 As shown, the target H2 yield in the syngas is 0.253 m³. 3 / kg, CH4 production is 0.075m 3 / kg, CO production is 0.69m 3 / kg, CO2 production is 0.141m 3 / kg, the total syngas production is 1.158m³. 3 / kg, the conversion rate of dry film residue is 75.78%.

[0051] Example 5

[0052] Example 5 is the same as Example 4, except that in step (4), the temperature of the electric heating belt is heated to 200°C, and deionized water is injected into the steam generating pipe at the opening away from the gas mixing chamber using a micro injection pump. The injection flow rate is 60µL / min. At the same time, the flow regulating valve is activated to introduce the reaction gas into the reactor through the inlet (the reaction gas entering through the inlet includes O2 and Ar, the total volume flow rate of the reaction gas is 500mL / min, the flow rate of O2 is 30mL / min, and the flow rate of Ar is 470mL / min). After passing through the primary air distribution plate, the reaction gas is mixed with steam in the gas mixing chamber. The vapor partial pressure of water vapor in the mixed gas is 15%. The mixed gas enters the reaction chamber through the secondary air distribution plate to make the bed material reach the fluidized state. Gas is generated after 25s of reaction, and the reaction is completed in about 2min.

[0053] The yield of syngas (CO, H2, CH4, CO) was monitored in real time during the reaction. To ensure the normal operation of the process mass spectrometer, the syngas was first passed through a drying tube containing 200 mL of 1 mol / L sodium carbonate solution and color-changing silica gel before being introduced into the process mass spectrometer for detection. The detection results are as follows: Figures 4-5 As shown, the target H2 yield in the syngas is 0.443 m³. 3 / kg, CH4 production was 0.058m 3 / kg, CO production is 0.757m 3 / kg, CO2 production is 0.175m 3 / kg, total yield was 1.433m 3 / kg, with a conversion rate of 82.87%.

[0054] Example 6

[0055] Example 6 is the same as Example 4, except that in step (4), the temperature of the electric heating belt is heated to 200°C, and deionized water is injected into the opening of the steam generating pipe away from the gas mixing chamber using a micro injection pump. The injection flow rate is 80µL / min. At the same time, the flow regulating valve is activated to introduce the reaction gas into the reactor through the air inlet (the reaction gas entering through the air inlet includes O2 and Ar, the total volume flow rate of the reaction gas is 500mL / min, the flow rate of O2 is 30mL / min, and the flow rate of Ar is 470mL / min). After passing through the primary air distribution plate, the reaction gas is mixed with steam in the gas mixing chamber. The vapor partial pressure of water vapor in the mixed gas is 20%. The mixed gas enters the reaction chamber through the secondary air distribution plate to make the bed material reach the fluidized state. Gas is generated after 15s of reaction, and the reaction is completed in about 1.3min.

[0056] The yield of syngas (CO, H2, CH4, CO) was monitored in real time during the reaction. To ensure the normal operation of the process mass spectrometer, the syngas was first passed through a drying tube containing 200 mL of 1 mol / L sodium carbonate solution and color-changing silica gel before being introduced into the process mass spectrometer for detection. The detection results are as follows: Figures 4-5 As shown, the target H2 yield in the syngas is 0.812 m³. 3 / kg, CH4 production was 0.034m 3 / kg, CO production is 0.797m 3 / kg, CO2 production is 0.278m 3 / kg, total yield was 1.921m 3 / kg, with a conversion rate of 92.8%.

[0057] Comparative Example 2

[0058] The method of Comparative Example 2 is the same as that of Example 4, except that in step (4), the temperature of the electric heating belt is heated to 200°C, and deionized water is injected into the opening of the steam generating pipe away from the gas mixing chamber using a micro injection pump. The injection flow rate is 0µL / min, so that the vapor partial pressure of water vapor in the mixed gas is 0%. At the same time, the flow regulating valve is activated to introduce the reaction gas into the reactor through the air inlet (the reaction gas entering from the air inlet includes O2 and Ar, the total volume flow rate of the reaction gas is 500mL / min, the flow rate of O2 is 30mL / min, and the flow rate of Ar is 470mL / min). The reaction gas enters the reaction chamber through the primary air distribution plate and then through the secondary air distribution plate to make the bed material reach the fluidized state. Gas is generated after 45s of reaction, and the reaction is completed after about 3.3min.

[0059] The yield of syngas (CO, H2, CH4, CO) was monitored in real time during the reaction. To ensure the normal operation of the process mass spectrometer, the syngas was first passed through a drying tube containing 200 mL of 1 mol / L sodium carbonate solution and color-changing silica gel before being introduced into the process mass spectrometer for detection. The detection results are as follows: Figures 4-5 As shown, the target H2 production in the syngas is 0.122 m³. 3 / kg, CH4 production was 0.099m 3 / kg, CO production is 0.577m 3 / kg, CO2 production is 0.066m 3 / kg, total yield is 0.865m 3 / kg, with a conversion rate of 63.17%.

Claims

1. A micro fluidized bed reactor for gasifying multi-source resin waste, characterized in that: It includes an air inlet chamber (8), a gas mixing chamber (9), and a reaction chamber (2); the air inlet chamber (8) is connected to an external gas cylinder through an air inlet (11); a primary air distribution plate (6) is provided between the air inlet chamber (8) and the gas mixing chamber (9); the gas mixing chamber (9) is also connected to a steam generating pipe (5), the steam outlet of the steam generating pipe (5) is connected to the gas mixing chamber (9), and an electric heating belt is provided on the outer sleeve of the steam generating pipe; the gas mixing chamber (9) and the reaction chamber (2) A secondary air distribution plate (4) is provided between the reaction chamber (2) and the reaction chamber (2) is provided with a feed inlet (3) and an air outlet (12); it also includes a heating device sleeved outside the reactor; wherein, the primary air distribution plate (6) and the secondary air distribution plate (4) are both provided with through holes; the aperture of the primary air distribution plate (6) is 30µm~60µm and the opening rate is 40%~45%; the aperture of the secondary air distribution plate (4) is 30µm~60µm and the opening rate is 30%~40%.

2. The micro fluidized bed reactor for gasifying multi-source resin waste according to claim 1, characterized in that: A filter plate (1) is provided at the air outlet (12).

3. The micro fluidized bed reactor for gasifying multi-source resin waste according to claim 2, characterized in that: The filter plate (1) has through holes, the pore diameter of the filter plate (1) is 30µm~60µm, and the porosity is 30%~40%.

4. The micro fluidized bed reactor for gasifying multi-source resin waste according to claim 1, characterized in that: The reaction chamber (2) is also connected to a thermocouple measuring tube (7), and a thermocouple (10) is placed inside the thermocouple measuring tube (7).

5. The micro fluidized bed reactor for gasifying multi-source resin waste according to claim 1, characterized in that: The reaction chamber (2) has a length of 30mm~40mm and an inner diameter of 15mm~30mm.

6. The micro fluidized bed reactor for gasifying multi-source resin waste according to claim 1, characterized in that: The length of the gas mixing chamber (9) is 120mm~160mm and the inner diameter is 15mm~30mm.

7. The micro fluidized bed reactor for gasifying multi-source resin waste according to claim 1, characterized in that: The length of the steam generating pipe (5) is 120mm~150mm and the inner diameter is 7mm~9mm.

8. The method for treating multi-source resin waste by gasification using the reactor described in claim 1, characterized in that, Includes the following steps: (1) Fill the reaction chamber with quartz sand, the particle size of which is larger than the pore size of the secondary air distribution plate and the filter plate; (2) The temperature of the reaction chamber is raised to not less than 950°C by a heating device, and the reaction chamber is purged with Ar gas for 10-20 minutes. (3) After purging, resin powder is sent into the reaction chamber by pulse jet. At this time, the temperature of the electric heating belt is heated to not less than 200°C. Deionized water is injected into the opening on the side of the steam generating pipe away from the gas mixing chamber. At the same time, the flow regulating valve is started to introduce the reaction gas into the reactor through the air inlet. The reaction gas is mixed with steam in the gas mixing chamber after passing through the primary air distribution plate. After mixing, it enters the reaction chamber through the secondary air distribution plate. The vapor partial pressure of water vapor in the mixed gas is 10~20%. Gas is generated after 15~40s of reaction and the reaction is completed after 1~3min.

9. The method for gasifying multi-source resin waste according to claim 8, characterized in that: In step (2), the reaction chamber is heated from room temperature to no less than 950°C at a rate of 25~30°C / min.

10. The method for gasifying multi-source resin waste according to claim 8, characterized in that: In step (2), the pulse pressure is not less than 0.2 MPa.

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