Organic solid waste treatment, metal recovery and carbon material preparation integrated device and use method thereof

Abstract

The invention provides an integrated device integrating organic solid waste treatment, metal recovery and carbon material preparation and a use method of the integrated device, and belongs to the field of environmental science and engineering. The problems that the utilization rate of organic solid waste heat energy is low, the recovery rate of metal-containing waste materials is low, and the carbon yield and quality of carbon materials prepared from agriculture and forestry biomass waste are low are solved. The integrated device comprises a feeding system, a solid waste heat treatment system, a steam utilization system, a tail gas purification and recovery system, a biomass carbonization system and a metal pyrolysis and recovery system, the solid waste heat treatment system comprises a pyrolysis gasification chamber and a high-temperature cracking chamber, and the high-temperature cracking chamber is divided into a left chamber and a right chamber; the steam utilization system comprises a high-pressure steam chamber, a low-pressure steam chamber and a hot water chamber, and the tail gas purification and recovery system comprises a cyclone dust collector, a spraying denitrification and denitration chamber, a water bath purification chamber, an electrostatic dust collector and a gas collector. The method is mainly used for organic solid waste treatment, metal recovery and carbon material preparation.

Description

Technical Field

[0001] The present invention belongs to the field of environmental science and engineering, and in particular relates to an integrated device integrating organic solid waste treatment, metal recovery and carbon material preparation and a use method thereof. Background Art

[0002] Thermal energy conversion is an important form of utilization of organic solid waste, pyrolysis recovery is an important form of metal purification, and carbon material preparation is an important form of utilization of agricultural and forestry organic solid waste. Due to the complex composition of organic solid waste, especially industrial solid waste, the different sources of raw materials lead to complex composition. Traditional methods are difficult to achieve full combustion, and the thermal energy conversion rate is low, which leads to the generation of a large amount of complex gases and high tail gas treatment costs. The traditional metal pyrolysis recovery produces a large amount of waste gas, which is difficult to treat and costly, especially metal oxidation leads to low utilization rate, and the traditional method of preparing biochar and fuel charcoal from agricultural and forestry biomass waste has low yield and low energy utilization rate. At present, the thermal energy utilization rate of organic solid waste is low, the recovery rate of metal-containing waste is low, and the carbon yield of agricultural and forestry biomass waste is low and the quality is not high, which restricts the high-value utilization of organic solid waste, the efficient recovery of metals and the development of carbon materials. Therefore, it is of great significance to develop an integrated device integrating high-temperature cracking treatment of organic solid waste, metal recovery and carbon material preparation to achieve high-value utilization of organic solid waste thermal energy, high metal recovery rate and high yield of carbon materials.

[0003] At present, the thermal energy conversion of organic solid waste, metal recovery and carbon material preparation are handled separately, resulting in a large amount of tail gas, high treatment costs, low thermal energy utilization rate and low equipment operation efficiency. In addition, there is currently a lack of pyrolysis treatment links for the gas generated by solid waste, especially dioxins produced by plastics in organic solid waste. Due to insufficient high-temperature cracking, a large amount of dioxin tail gas is generated. In addition, for the resynthesis of dioxins in the tail gas cooling process, the cooling method currently used has a high resynthesis rate, resulting in high tail gas treatment costs. The existing organic solid waste is not fully pyrolyzed, the thermal energy utilization rate is low, and the tail gas output is large and the composition is complex, resulting in low resource utilization. Due to the high plastic content in most metal wastes, the cost of tail gas treatment after pyrolysis recovery is high, and the biomass gas generated by carbon material preparation is difficult to collect, and there are safety risks in collection and storage. The existing metal recovery method has a high metal oxidation loss rate due to the lack of a strict oxygen-free environment, and the use of nitrogen and inert gases leads to increased metal costs; the environmental requirements for biochar preparation are strict, and conventional heating methods are inefficient and costly. Summary of the invention

[0004] In view of this, the present invention aims to propose an integrated device integrating organic solid waste treatment, metal recovery and carbon material preparation and its use method, so as to solve a series of problems such as low thermal energy utilization rate of organic solid waste, low recovery rate of metal-containing waste, low charcoal yield and low quality of carbon materials prepared from agricultural and forestry biomass waste, and high cost of exhaust gas purification.

[0005] To achieve the above-mentioned purpose, the present invention adopts the following technical scheme: an integrated device for organic solid waste treatment, metal recovery and carbon material preparation, which includes a feeding system, a solid waste heat treatment system, a steam utilization system, a tail gas purification and recovery system, a biomass carbonization system and a metal pyrolysis recovery system, the solid waste heat treatment system includes a pyrolysis gasification chamber and a high-temperature cracking chamber, the high-temperature cracking chamber is divided into a left chamber and a right chamber, the steam utilization system includes a high-pressure steam room, a low-pressure steam room and a hot water room, the tail gas purification and recovery system includes a cyclone dust collector, a spray denitrification and denitrification chamber, a water bath purification chamber, an electrostatic precipitator and a gas collector, the feeding system and the pyrolysis gasification chamber The pyrolysis gasification chamber is connected to the left chamber of the high-temperature cracking chamber through a primary air outlet, the left chamber of the high-temperature cracking chamber is connected to the right chamber through a secondary air outlet, the right chamber of the high-temperature cracking chamber is connected to the high-pressure steam room through a first air outlet, the high-pressure steam room is connected to the low-pressure steam room, the low-pressure steam room is connected to the hot water room through a second air outlet, the upper end of the hot water room is connected to the low-pressure steam room through a hot water return pipe, a return valve is provided on the hot water return pipe, the hot water room is connected to the cyclone dust collector through a first smoke exhaust pipe, the exhaust pipe of the cyclone dust collector is connected to the spray denitrification and denitrification chamber through a connecting pipe, and an induced draft valve is provided on the connecting pipe. The spray denitrification and denitrification chamber is connected to the water bath purification chamber through the second smoke exhaust pipe, the water bath purification chamber is connected to the electrostatic precipitator through the third smoke exhaust pipe, the electrostatic precipitator is connected to the gas collector through the tail gas collection pipe, the gas collector is connected to the discharge pipe, the discharge pipe is connected with a tail gas reflux pipe and a tail gas cooling and utilization pipe, the end of the discharge pipe is a tail gas discharge port, the discharge pipe is provided with a tail gas external discharge control valve, the tail gas reflux pipe is connected to the left chamber and the right chamber of the high temperature cracking chamber and the reflux fan, the reflux fan is connected to the air inlet of the pyrolysis gasification chamber through the air inlet pipe, the tail gas cooling and utilization pipe is connected to the biomass carbonization system, the tail An exhaust gas cooling and utilization control valve is provided on the gas cooling and utilization pipe, and hot air inlets are provided in both the biomass carbonization system and the metal pyrolysis recovery system. Two hot air pipes are connected on both sides of the first air duct, and the two hot air pipes are respectively connected to the hot air inlets of the biomass carbonization system and the metal pyrolysis recovery system. Hot air intake control valves are respectively provided on the two hot air pipes. A biomass gas exhaust port is provided in the biomass carbonization system, and a fuel gas outlet is provided in the metal pyrolysis recovery system. The biomass gas exhaust port and the fuel gas outlet are respectively connected to the pyrolysis gasification chamber through a biomass gas reflux pipe, and a biomass gas control valve is provided on the biomass gas reflux pipe.

[0006] Furthermore, the biomass carbonization system includes a carbonization chamber, a first feeding system and a carbonizing machine. A first feed port and a plurality of hot air inlets are provided on the side wall of the carbonization chamber, the first feed port and the plurality of hot air inlets are arranged opposite to each other, the first feed port is connected to the first feeding system, a plurality of biomass gas exhaust outlets are provided on the top of the carbonization chamber, a cooling gas inlet is provided at the bottom of the carbonization chamber, the exhaust gas cooling utilization pipe is connected to the cooling gas inlet, a carbonization plate is provided inside the carbonization chamber, rollers are provided at both ends of the carbonization plate, the rollers are connected to a driver, the front end of the carbonization plate is close to the first feed port, the end is close to the aggregate pit, a push-pull plate is provided above the aggregate pit, the aggregate pit is connected to the carbonizing machine, a heat collecting plate is provided above the carbonization plate, and the upper end of the heat collecting plate is open.

[0007] Furthermore, the spacing between the multiple hot air inlets is 0.5-1.0m, the hot air inlet is inclined at an angle of 5-10 degrees in the direction of the first feed inlet, the heat collecting plate is an arched structure, and the opening is 0.2-0.4 times the length of the inner space of the carbonization chamber at a distance from the first feed inlet side, and the number of the biomass gas exhaust outlets is three, one of which is located above the opening of the heat collecting plate, and the other two are located at both ends of the top of the carbonization chamber.

[0008] Furthermore, the first feeding system includes a feeding table, a feeding bucket, a feeding platform, a feeding belt, a feeding hopper, a pushing system and a reel. Reels are arranged on both sides of the feeding belt. One end of the feeding belt is arranged in the feeding hopper, and the other end is arranged on the feeding platform. A feeding bucket is arranged at one end of the feeding platform, and the feeding bucket is located above the feeding table. The feeding bucket is a feeding rotating eccentric form. A pushing system is arranged in the feeding platform, and the output end of the pushing system is arranged on the feeding table, and the feeding table is connected to the first feeding port.

[0009] Furthermore, the metal pyrolysis recovery system includes a metal recovery pyrolysis chamber, a slag discharger and a second feeding system. A second feed port and multiple hot air inlets are provided on the side wall of the metal recovery pyrolysis chamber. The second feed port and the multiple hot air inlets are arranged opposite to each other. The second feed port is connected to the second feeding system. Multiple gas outlets are provided on the top of the metal recovery pyrolysis chamber. A two-way grate is provided inside the metal recovery pyrolysis chamber. The two-way grate is connected to a driver. The front end of the two-way grate is close to the second feed port, and the end is close to a receiving trough. A push-pull plate is provided above the receiving trough. 0.55-0.85 times the capacity of water is injected into the receiving trough. The receiving trough is connected to the slag discharger.

[0010] Furthermore, the spacing between the multiple hot air inlets is 0.3-0.5m, the hot air inlet is inclined at an angle of 3-8 degrees toward the second feed inlet, and the number of the gas outlets is two, which are located at both ends of the top of the metal recovery pyrolysis chamber.

[0011] Furthermore, the second feeding system includes a spiral feed hopper, a feeding plate, a feeding trough and a feeding screw rod. One end of the feeding plate is arranged in the feeding trough, and the other end is arranged on the spiral feed hopper. A feeding screw rod is arranged in the spiral feed hopper, and the feeding screw rod is connected to the second feed port.

[0012] Furthermore, a one-way grate is arranged in the pyrolysis gasification chamber, the front end of the one-way grate is close to the feeding system, and the end is close to the discharge port, a discharge bin is arranged below the discharge port, and a front baffle and a rear baffle are arranged above the one-way grate, both of which are arc-shaped structures, and the air inlet is opened between the front baffle and the rear baffle.

[0013] Furthermore, two exhaust ports are arranged above the left chamber of the high-temperature cracking chamber, and the two exhaust ports of the left chamber are located in the middle and right side of the left chamber. An exhaust port is arranged above the right chamber of the high-temperature cracking chamber, and the exhaust port of the right chamber is located on the right side of the right chamber. The left chamber and the right chamber of the high-temperature cracking chamber discharge hot air through the exhaust ports, and all the exhaust ports are connected to the exhaust gas reflux pipe through the exhaust connecting pipe, and the exhaust connecting pipe and the exhaust gas reflux pipe are provided with a gas reflux valve.

[0014] Furthermore, the hot air flow rate discharged from the left chamber of the high-temperature cracking chamber is 1.5-2.2 times that of the right chamber, and the air volume returned by the gas collector through the tail gas return pipe is 0.15-0.25 times the hot air volume discharged from the high-temperature cracking chamber.

[0015] Furthermore, a combustion-supporting agent inlet is provided on the top of the left chamber of the high-temperature cracking chamber, and an additive adding port is provided on the first air duct, the top and the side wall of the right chamber of the high-temperature cracking chamber.

[0016] Furthermore, a combustion aid is added into the combustion aid inlet, and the combustion aid is a gas containing more than 95% oxygen or a solid fuel with a calorific value of 5000-9000 kcal / kg.

[0017] Furthermore, the additive is added into the additive adding port, and the additive is a mixture of modified biochar, diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, gravel, volcanic rock, activated carbon and river sand, and the mixing ratio is 1: (0.03-0.08): (0.15-0.35): (0.10-0.25): (0.03-0.05): (0.06-0.09): (0.03-0.08): (0.05-0.12): (0.35-0.55): (0.08-0.12).

[0018] Furthermore, the modified biochar is a mixture of iron oxide modified biochar and potassium permanganate modified biochar, the mixing ratio is 1: (0.2-0.5), the particle size is 0.5-2mm, the particle size of the diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, sandstone, volcanic rock, activated carbon and river sand are 0.1-1.0mm, 0.01-0.1mm, 0.25-2.0mm, 0.25-1.0mm, 0.1-1.0mm, 0.25-5.0mm, 0.5-2.0mm, 0.1-2.0mm, 0.1-1.0mm, respectively, and the activated carbon is coal-based activated carbon.

[0019] Furthermore, dust exhaust ports are arranged at the bottom of the left and right chambers, the high-pressure steam room, the low-pressure steam room and the hot water room of the high-temperature cracking chamber. The dust exhaust port at the bottom of the left chamber of the high-temperature cracking chamber is connected to the dust storage pit through a dust pipe. A dust removing fan is arranged on the dust pipe. A dust cover is arranged at the end of the dust pipe. The dust cover is connected by a spring. A dust storage tank is arranged below the dust exhaust port at the bottom of the right chamber of the high-temperature cracking chamber.

[0020] Furthermore, an air outlet is provided at the lower part of the left chamber of the high-temperature cracking chamber, and an air inlet is provided at the lower part of the right chamber of the high-temperature cracking chamber. The air outlet and the air inlet are connected by a flow regulating air duct, and a flow regulating fan is provided on the flow regulating air duct.

[0021] Furthermore, the feeding system includes a loading chamber, a gas separator, a push blower, a feeding box, a first conveyor belt and a feeding platform, one end of the first conveyor belt is arranged in the feeding box, and the other end is arranged on the loading chamber, a second conveyor belt is arranged in the loading chamber, and the end of the second conveyor belt is close to the feeding platform, the gas separator is connected to the push blower, the push blower outlet is arranged on the feeding platform, and the feeding platform is connected to the inlet of the pyrolysis gasification chamber.

[0022] Furthermore, the gas separator uses membrane separation technology to separate nitrogen from the air, and other gases in the air enter the pyrolysis gasification chamber through a push blower.

[0023] Furthermore, the air volume entering the pyrolysis gasification chamber through the air inlet pipe is 0.15-0.35 times the air volume of the push blower.

[0024] Furthermore, positioning plates are provided above the feed inlet of the pyrolysis gasification chamber and the second conveyor belt in the loading chamber, and a baffle plate is provided above the feed inlet of the pyrolysis gasification chamber.

[0025] Furthermore, the cyclone dust collector includes a cyclone dust chamber and an ash collecting chamber, the exhaust pipe is arranged in the cyclone dust chamber, the exhaust pipe is a structure with a larger upper part and a smaller lower part, a dust reduction hole is arranged at the bottom of the cyclone dust chamber, the dust reduction hole is located in the ash collecting chamber, and a dust reduction plate is arranged above the dust reduction hole.

[0026] Furthermore, the spray denitrification and denitrification chamber includes a spray chamber, a desulfurization room and a denitrification room. The spray chamber is connected to a connecting pipe. A water tank is arranged in the spray chamber. A plurality of nozzles are connected to the lower part of the water tank. A waste liquid collecting port is arranged at the bottom of the spray chamber. A waste water collecting barrel is arranged below the waste liquid collecting port. The spray chamber is connected to the desulfurization room through a desulfurization inlet. The desulfurization room is connected to the denitrification room through a denitrification inlet. The denitrification room is connected to the water bath purification chamber through a second smoke exhaust pipe.

[0027] Furthermore, the desulfurization room uses activated carbon material, and the denitrification room uses a mixture of activated carbon and iron oxide.

[0028] Furthermore, an exhaust gas monitoring box is provided on the exhaust gas collecting pipe, and a variety of gas monitoring probes are provided in the exhaust gas monitoring box.

[0029] Furthermore, the biomass carbonization system, metal pyrolysis recovery system, high-pressure steam room, and the left and right chambers of the high-temperature cracking chamber are each provided with 2-6 pressure monitoring gauges and 2-6 temperature monitoring gauges; the pyrolysis gasification chamber, low-pressure steam room, and hot water room are each provided with 2-6 temperature monitoring gauges; and the third smoke exhaust pipe is provided with 1-2 temperature monitoring gauges.

[0030] Furthermore, the gas collector collects carbon dioxide by combining an upward exhaust method with an activated carbon pressure swing adsorption method, and the remaining tail gas enters an exhaust pipe.

[0031] Furthermore, the outer sides of the pyrolysis gasification chamber and the high-temperature cracking chamber are steel plates, and refractory wool, refractory bricks, refractory cement and refractory coatings are arranged in sequence from the outside to the inside.

[0032] Furthermore, the rated steam pressure of the high-pressure steam room is 2.0-3.0 MPa, and the steam pressure of the low-pressure steam room is 1.0-2.0 MPa.

[0033] The present invention also provides a method for using an integrated device for organic solid waste treatment, metal recovery and carbon material preparation, and the specific process is as follows:

[0034] Organic solid waste enters the pyrolysis gasification chamber through the feeding system, and the generated pyrolysis gas enters the left chamber of the high-temperature cracking chamber through the primary air outlet, and enters the right chamber of the high-temperature cracking chamber through the secondary air outlet. After completing the internal circulation of the solid waste heat treatment system, it enters the high-pressure steam room, low-pressure steam room and hot water room in turn, and completes the thermal energy conversion of organic solid waste through the solid waste heat treatment system and the steam utilization system;

[0035] The solid waste heat treatment system is operated simultaneously with the biomass carbonization system and / or the metal pyrolysis recovery system. The hot air in the high-temperature cracking chamber enters the biomass carbonization system and / or the metal pyrolysis recovery system through the hot air pipe. Agricultural and forestry biomass waste is placed in the biomass carbonization system, and the agricultural and forestry biomass waste is carbonized by the biomass carbonization system to prepare biochar or fuel charcoal. Metal waste is placed in the metal pyrolysis recovery system, and the metal waste is separated by the metal pyrolysis recovery system to achieve metal recovery. The combustible gas generated by the biomass carbonization system enters the pyrolysis gasification chamber through the biomass gas outlet and the biomass gas reflux pipe, and the combustible gas generated by the metal pyrolysis recovery system enters the pyrolysis gasification chamber through the gas outlet and the biomass gas reflux pipe.

[0036] The exhaust gas discharged from the hot water room enters the cyclone dust collector, and enters the spray denitrification and denitrification chamber under the action of the induced draft fan. After dust reduction, denitrification and denitrification treatment, the exhaust gas enters the water bath purification chamber, electrostatic precipitator and gas collector in turn. Carbon dioxide is collected in the gas collector, and the remaining part of the exhaust gas enters the pyrolysis gasification chamber through the exhaust gas reflux pipe, and the rest of the exhaust gas enters the biomass carbonization system that completes the carbonization operation through the exhaust gas cooling and utilization pipe or is discharged through the exhaust pipe.

[0037] Furthermore, the organic solid waste has a moisture content of less than 25% and a calorific value of higher than 2000 kcal / kg, the metal waste has a moisture content of less than 10%, and the agricultural and forestry biomass waste has a moisture content of less than 20%. It is first prepared into particles and then dried. When it is prepared into biochar, the particle size is 10-30 mm, and when it is prepared into fuel charcoal, the particle size is 20-50 mm or the columnar diameter and length are 20-80 mm and 100-300 mm respectively.

[0038] Compared with the prior art, the beneficial effects of the present invention are as follows: the present invention provides an integrated device integrating organic solid waste treatment, metal recovery and carbon material preparation and a use method thereof, which can realize the integrated treatment of organic solid waste utilization, metal recovery and carbon material preparation, and solve the problems of low thermal energy utilization rate of organic solid waste, large amount of pollutants generated by metal waste and high metal oxidation loss rate, low biochar yield and large amount of waste gas output, low concentration of carbon dioxide in tail gas and difficulty in recovery, and realize the organic solid waste thermal energy conversion rate of more than 85%, the metal content after purification exceeds 80%, the biochar yield exceeds 30%, and the fuel carbon calorific value is as high as 4200-5400kcal / kg; realize the reduction of carbon dioxide recovery cost in tail gas by more than 30%, and improve the operation efficiency by more than 40%; realize the reduction of tail gas generation by more than 30%, and reduce the tail gas treatment cost by more than 80%; the device realizes continuous operation, high production efficiency, large output and high degree of industrialization; the device has low energy consumption, and does not consume other energy except a small amount of electricity, and has low cost.

[0039] The present invention integrates organic solid waste, metal recovery and carbon material preparation, realizes efficient utilization of tail gas from metal recovery and carbon material preparation, and reduces the cost of tail gas treatment. The tail gas after high-temperature cracking is used to reduce the cost of metal waste treatment. Through oxygen-free hot air treatment, the efficiency is high and the carbon yield is high.

[0040] The present invention realizes full combustion of the system through efficient heat preservation, addition of combustion aid and special structural system, completes multi-stage cracking, fully decomposes dioxins, reduces dioxin resynthesis, and further reduces dioxin resynthesis through special additives, thereby achieving effective removal of dioxins and low tail gas purification cost. The tail gas carbon dioxide concentration collected by the present invention is high, up to 50% or more, which is twice that of conventional organic solid waste of about 25%, and is conducive to the efficient recovery of carbon dioxide. The present invention not only improves the thermal energy utilization efficiency of organic solid waste, improves the metal recovery rate and the yield and quality of carbon materials, but also greatly reduces the output of waste gas, which has important practical significance for promoting the development of organic solid waste treatment, metal recovery and carbon material industries.

[0041] The present invention realizes full combustion of organic solid waste through high-temperature multi-stage pyrolysis, improves thermal energy utilization efficiency, reduces waste gas generation, and thus reduces tail gas treatment costs; improves the recovery rate of metal waste through full carbonization; improves the charcoal yield of biochar through full carbonization; can realize efficient thermal energy utilization of organic solid waste, efficient metal recovery and efficient preparation of biochar in an integrated manner, has a simple process, low energy consumption, little impact on the environment, and has high value for promotion and application. BRIEF DESCRIPTION OF THE DRAWINGS

[0042] The accompanying drawings constituting a part of the present invention are used to provide a further understanding of the present invention. The exemplary embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention. In the accompanying drawings:

[0043] Figure 1 This is a schematic diagram of the vertical cross-sectional structure of an integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to the present invention;

[0044] Figure 2 This is a schematic diagram of a top view of an integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to the present invention;

[0045] Figure 3 It is a schematic diagram of the cross-sectional structure of the biomass carbonization system of the present invention;

[0046] Figure 4 This is a schematic diagram of the cross-sectional structure of the metal pyrolysis recovery system described in the present invention.

[0047] In the figure:

[0048] 1-feeding chamber, 2-pyrolysis gasification chamber, 3-high temperature cracking chamber, 4-high pressure steam room, 5-low pressure steam room, 6-hot water room, 7-cyclone dust collector, 8-spray denitrification and denitrification chamber, 9-water bath purification chamber, 10-electrostatic dust collector, 11-exhaust monitoring box, 12-gas collector, 13-gas separator, 14-push blower, 15-feeding box, 16-first conveyor belt, 17-feeding platform, 18-baffle plate, 19-positioning plate, 20-one-way grate, 21-discharge port, 22-front baffle, 23-rear baffle, 24-discharge bin, 25-air inlet, 26-air inlet pipe, 27-primary air outlet, 28-return fan, 29-secondary air outlet 30-combustion agent inlet, 31-exhaust outlet, 32-dust outlet, 33-dust removal fan, 34-dust cover, 35-dust storage pit, 36-dust storage tank, 37-flow regulating fan, 38-air inlet, 39-additive addition port, 40-first air duct, 41-third smoke exhaust pipe, 42-cyclone dust removal chamber, 43-ash collection chamber, 44-exhaust pipe, 45-dust reduction plate, 46-dust reduction hole, 47-induced draft fan, 48-connecting pipe, 49-spraying chamber, 50-nozzle, 51-wastewater collection barrel, 52-waste liquid collection port, 53-desulfurization inlet, 54-desulfurization room, 55-denitrification inlet, 56-denitrification room, 57-tail gas collection pipe, 58-gas return Flow valve, 59- tail gas reflux pipe, 60- tail gas discharge port, 61- tail gas external discharge control valve, 62- hot water reflux pipe, 63- tail gas cooling utilization pipe, 64- tail gas cooling utilization control valve, 65- carbonization chamber, 66- first feeding system, 67- carbon discharge machine, 68- hot air pipe, 69- pressure monitoring meter, 70- temperature monitoring meter, 71- biomass gas reflux pipe, 72- biomass gas discharge port, 73- hot air inlet, 74- heat collecting plate, 75- aggregate pit, 76- carbonization plate, 77- feeding platform, 78- feeding tipping bucket, 79- feeding platform, 80- feeding belt, 81- feeding hopper, 82- pushing system, 83- reel, 84- roller, 85- push and pull Plate, 86-driver, 87-cooling gas inlet, 88-hot air inlet control valve, 89-biomass gas control valve, 90-metal recovery pyrolysis chamber, 91-screw feed hopper, 92-feeding plate, 93-slag discharger, 94-gas outlet, 95-two-way grate, 96-collecting trough, 97-feeding trough, 98-feeding screw rod, 99-second air duct, 100-return valve, 101-first smoke exhaust pipe, 102-second smoke exhaust pipe, 103-discharge pipe, 104-first feed port, 105-second feeding system, 106-second feed port, 107-dust duct, 108-air outlet, 109-flow adjustment duct, 110-second conveyor belt. DETAILED DESCRIPTION

[0049] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely explain the technical solutions in the embodiments of the present invention. It should be noted that the embodiments of the present invention and the features in the embodiments can be combined with each other without conflict, and the described embodiments are only part of the embodiments of the present invention, not all of the embodiments.

[0050] Example 1: See Figure 1-4The present embodiment is described as an integrated device for organic solid waste treatment, metal recovery and carbon material preparation, which includes a feeding system, a solid waste heat treatment system, a steam utilization system, a tail gas purification and recovery system, a biomass carbonization system and a metal pyrolysis recovery system. The solid waste heat treatment system includes a pyrolysis gasification chamber 2 and a high-temperature cracking chamber 3, and the high-temperature cracking chamber 3 is divided into a left chamber and a right chamber. The steam utilization system includes a high-pressure steam room 4, a low-pressure steam room 5 and a hot water room 6. The tail gas purification and recovery system includes a cyclone dust collector 7, a spray denitrification and denitrification chamber 8, a water bath purification chamber 9, an electrostatic precipitator 10 and a gas collector 12. The feeding system is connected to the feed port of the pyrolysis gasification chamber 2, and the pyrolysis gasification chamber 2 and the left chamber of the high-temperature cracking chamber 3 are connected by a one-time process. The left chamber of the high-temperature cracking chamber 3 is connected to the right chamber through the secondary air port 29, the right chamber of the high-temperature cracking chamber 3 is connected to the high-pressure steam room 4 through the first air duct 40, the high-pressure steam room 4 is connected to the low-pressure steam room 5, the low-pressure steam room 5 is connected to the hot water room 6 through the second air duct 99, the upper end of the hot water room 6 is connected to the low-pressure steam room 5 through the hot water return pipe 62, the hot water return pipe 62 is provided with a return valve 100, the hot water room 6 is connected to the cyclone dust collector 7 through the first exhaust pipe 101, the exhaust pipe 44 of the cyclone dust collector 7 is connected to the spray denitrification and denitrification chamber 8 through the connecting pipe 48, the connecting pipe 48 is provided with an induced draft fan 47, the spray denitrification and denitrification chamber 8 is connected to the second exhaust pipe 10 2 is connected to the water bath purification chamber 9, the water bath purification chamber 9 is connected to the electrostatic precipitator 10 through the third smoke exhaust pipe 41, the electrostatic precipitator 10 is connected to the gas collector 12 through the tail gas collection pipe 57, the gas collector 12 is connected to the discharge pipe 103, the discharge pipe 103 is connected with a tail gas return pipe 59 and a tail gas cooling and utilization pipe 63, the end of the discharge pipe 103 is a tail gas discharge port 60, the discharge pipe 103 is provided with a tail gas external discharge control valve 61, the tail gas return pipe 59 is connected to the left chamber and the right chamber of the high temperature cracking chamber 3 and the return fan 28, the return fan 28 is connected to the air inlet 25 of the pyrolysis gasification chamber 2 through the air inlet pipe 26, the tail gas cooling and utilization pipe 63 is connected to the biomass carbonization system, the tail gas An exhaust gas cooling and utilization control valve 64 is provided on the cooling and utilization pipe 63, and a hot air inlet 73 is provided in both the biomass carbonization system and the metal pyrolysis recovery system. Two hot air pipes 68 are connected to the two sides of the first air duct 40, and the two hot air pipes 68 are respectively connected to the hot air inlet 73 in the biomass carbonization system and the metal pyrolysis recovery system. A hot air intake control valve 88 is provided on the two hot air pipes 68, respectively. A biomass gas exhaust port 72 is provided in the biomass carbonization system, and a gas outlet 94 is provided in the metal pyrolysis recovery system. The biomass gas exhaust port 72 and the gas outlet 94 are respectively connected to the pyrolysis gasification chamber 2 through a biomass gas return pipe 71, and a biomass gas control valve 89 is provided on the biomass gas return pipe 71.

[0051] The specific process of using the method of this embodiment is as follows:

[0052] The organic solid waste enters the pyrolysis gasification chamber 2 through the feeding system, and the generated pyrolysis gas enters the left chamber of the high-temperature cracking chamber 3 through the primary air outlet 27, and enters the right chamber of the high-temperature cracking chamber 3 through the secondary air outlet 29. After completing the internal circulation of the solid waste heat treatment system, it enters the high-pressure steam room 4, the low-pressure steam room 5 and the hot water room 6 in turn, and completes the thermal energy conversion of the organic solid waste through the solid waste heat treatment system and the steam utilization system;

[0053] The solid waste heat treatment system is operated simultaneously with the biomass carbonization system and / or the metal pyrolysis recovery system. The hot air in the high-temperature cracking chamber 3 enters the biomass carbonization system and / or the metal pyrolysis recovery system through the hot air pipe 68. Agricultural and forestry biomass waste is put into the biomass carbonization system, and the agricultural and forestry biomass waste is carbonized by the biomass carbonization system to prepare biochar or fuel charcoal. Metal waste is put into the metal pyrolysis recovery system, and the metal waste is separated by the metal pyrolysis recovery system to achieve metal recovery. The combustible gas generated by the biomass carbonization system enters the pyrolysis gasification chamber 2 through the biomass gas outlet 72 and the biomass gas reflux pipe 71, and the combustible gas generated by the metal pyrolysis recovery system enters the pyrolysis gasification chamber 2 through the gas outlet 94 and the biomass gas reflux pipe 71.

[0054] The exhaust gas discharged from the hot water room 6 enters the cyclone dust collector 7, and enters the spray denitrification and denitrification chamber 8 under the action of the induced draft fan 47. After the dust reduction, denitrification and denitrification treatment, the exhaust gas enters the water bath purification chamber 9, the electrostatic precipitator 10 and the gas collector 12 in sequence. Carbon dioxide is collected in the gas collector 12, and the remaining part of the exhaust gas enters the pyrolysis gasification chamber 2 through the exhaust gas reflux pipe 59. The rest of the exhaust gas enters the biomass carbonization system that completes the carbonization operation through the exhaust gas cooling and utilization pipe 63 or is discharged through the exhaust pipe 103.

[0055] This embodiment is specifically described as follows:

[0056] The organic solid waste has a moisture content of less than 25% and a calorific value of more than 2000 kcal / kg, the metal waste has a moisture content of less than 10%, and the agricultural and forestry biomass waste has a moisture content of less than 20%. It is first prepared into particles and then dried. When prepared into biochar, the particle size is 10-30 mm, and when prepared into fuel charcoal, the particle size is 20-50 mm or the columnar diameter and length are 20-80 mm and 100-300 mm respectively.

[0057] A one-way grate 20 is arranged in the pyrolysis gasification chamber 2, the front end of the one-way grate 20 is close to the feeding system, and the rear end is close to the discharge port 21. A discharge bin 24 is arranged below the discharge port 21, and a front baffle 22 and a rear baffle 23 are arranged above the one-way grate 20. The front baffle 22 and the rear baffle 23 are both arc-shaped structures, and the air inlet 25 is opened between the front baffle 22 and the rear baffle 23.

[0058] Two exhaust ports 31 are arranged above the left chamber of the pyrolysis chamber 3, and the two exhaust ports 31 of the left chamber are located in the middle and right side of the left chamber. One exhaust port 31 is arranged above the right chamber of the pyrolysis chamber 3, and the exhaust port 31 of the right chamber is located on the right side of the right chamber. The left and right chambers of the pyrolysis chamber 3 exhaust hot air through the exhaust ports 31, and all the exhaust ports 31 are connected to the tail gas return pipe 59 through the exhaust connection pipe, and the exhaust connection pipe and the tail gas return pipe 59 are provided with a gas return valve 58, and the gas return valve 58 is used to control the amount of reflux gas in the left and right chambers of the gas collector 12 and the pyrolysis chamber 3. The hot air flow rate discharged from the left chamber of the pyrolysis chamber 3 is 1.5-2.2 times that of the right chamber, and the air volume refluxed by the gas collector 12 through the tail gas return pipe 59 is 0.15-0.25 times the amount of hot air discharged from the pyrolysis chamber 3.

[0059] The top of the left chamber of the high-temperature cracking chamber 3 is provided with an inlet for combustion-supporting agent 30, and the first air duct 40, the top of the right chamber and the side wall of the high-temperature cracking chamber 3 are provided with an additive adding port 39. The combustion-supporting agent inlet 30 is added with a combustion-supporting agent, and the combustion-supporting agent is a gas containing more than 95% oxygen or a solid fuel with a calorific value of 5000-9000 kcal / kg. Additives are added to the additive adding port 39, and the additives are a mixture of modified biochar, diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, gravel, volcanic rock, activated carbon and river sand, and the mixing ratio is 1: (0.03-0.08): (0.15-0.35): (0.10-0.25): (0.03-0.05): (0.06-0.09): (0.03-0.08): (0.05-0.12): (0.35-0.55): (0.08-0.12). The modified biochar is a mixture of iron oxide modified biochar and potassium permanganate modified biochar, the mixing ratio is 1: (0.2-0.5), the particle size is 0.5-2mm, the particle size of the diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, sandstone, volcanic rock, activated carbon and river sand are 0.1-1.0mm, 0.01-0.1mm, 0.25-2.0mm, 0.25-1.0mm, 0.1-1.0mm, 0.25-5.0mm, 0.5-2.0mm, 0.1-2.0mm, 0.1-1.0mm, respectively, and the activated carbon is coal-based activated carbon.

[0060] The left and right chambers of the high-temperature cracking chamber 3, the high-pressure steam room 4, the low-pressure steam room 5 and the hot water room 6 are all provided with dust exhaust ports 32 at the bottom. The dust exhaust port 32 at the bottom of the left chamber of the high-temperature cracking chamber 3 is connected to the dust storage pit 35 through a dust pipe 107. A dust removal fan 33 is provided on the dust pipe 107. A dust cover 34 is provided at the end of the dust pipe 107. The dust cover 34 is spring-connected. A dust storage tank 36 is provided below the dust exhaust port 32 at the bottom of the right chamber of the high-temperature cracking chamber 3.

[0061] An air outlet 108 is provided at the lower part of the left chamber of the high-temperature cracking chamber 3, and an air inlet 38 is provided at the lower part of the right chamber of the high-temperature cracking chamber 3. The air outlet 108 and the air inlet 38 are connected by a flow regulating air duct 109, and a flow regulating fan 37 is provided on the flow regulating air duct 109. The flow regulating fan 37 draws the hot air from the left chamber of the high-temperature cracking chamber 3 to the right chamber.

[0062] The feeding system includes a loading chamber 1, a gas separator 13, a push blower 14, a feeding box 15, a first conveyor belt 16 and a feeding platform 17. One end of the first conveyor belt 16 is arranged in the feeding box 15, and the other end is arranged on the loading chamber 1. A second conveyor belt 110 is arranged in the loading chamber 1, and the end of the second conveyor belt 110 is close to the feeding platform 17. The gas separator 13 is connected to the push blower 14, and the outlet of the push blower 14 is arranged on the feeding platform 17. The feeding platform 17 is connected to the feeding port of the pyrolysis gasification chamber 2.

[0063] The gas separator 13 uses membrane separation technology to separate nitrogen from the air. The other gases after separation are mainly oxygen-containing and enter the pyrolysis gasification chamber 2 through the push blower 14. The air volume entering the pyrolysis gasification chamber 2 through the air inlet pipe 26 is 0.15-0.35 times the air volume of the push blower 14. A positioning plate 19 is provided above the feed inlet of the pyrolysis gasification chamber 2 and the second conveyor belt 110 in the loading chamber 1, and a baffle plate 18 is provided above the feed inlet of the pyrolysis gasification chamber 2.

[0064] The gas separator 13 separates nitrogen from the air, and the feed box 15 of the feed system conveys the organic solid waste to the loading chamber 1 through the first conveyor belt 16, and then transports the organic solid waste to the feeding platform 17 through the second conveyor belt 110 inside the loading chamber 1, and blows the organic waste into the one-way grate 20 of the pyrolysis gasification chamber 2 through the push blower 14; the organic waste in the pyrolysis gasification chamber 2 is pyrolyzed at 300-500°C, and the generated combustible gas enters the high-temperature cracking chamber 3 through the primary air outlet 27 and is high-temperature cracked for 3-5 seconds at 850-1000°C. During the high-temperature cracking process, the left chamber of the high-temperature cracking chamber 3 is added with an oxidant through the oxidant inlet 30, and the right chamber is added with a biomass additive through the additive adding port 39; the first air duct 40 between the high-temperature cracking chamber 3 and the high-pressure steam room 4 is added with a biomass additive through the additive adding port 39.

[0065] The bottom of the left chamber of the high-temperature cracking chamber 3 is cleaned every 2-6 hours through a dust removal fan 33. The dust cover 34 is connected by a spring and is opened only when cleaning to discharge the dust into a dust storage pit 35. The bottom of the right chamber is cleaned every 12-18 hours through a dust discharge port 32, and the ash is discharged into a dust storage tank 36. The high-pressure steam room 4, the low-pressure steam room 5 and the hot water room 6 are cleaned every 2-4 days.

[0066] The biomass carbonization system includes a carbonization chamber 65, a first feeding system 66 and a carbonizer 67. A first feed port 104 and a plurality of hot air inlets 73 are provided on the side wall of the carbonization chamber 65. The first feed port 104 and the plurality of hot air inlets 73 are arranged opposite to each other. The first feed port 104 is connected to the first feeding system 66. A plurality of biomass gas outlets 72 are provided on the top of the carbonization chamber 65. A cooling gas inlet 87 is provided on the bottom of the carbonization chamber 65. The tail gas cooling The pipe 63 is connected to the cooling gas inlet 87, and a carbonization plate 76 is arranged inside the carbonization chamber 65. Rollers 84 are arranged at both ends of the carbonization plate 76, and the rollers 84 are connected to the driver 86. The front end of the carbonization plate 76 is close to the first feed port 104, and the end is close to the aggregate pit 75. A push-pull plate 85 is arranged above the aggregate pit 75, and the aggregate pit 75 is connected to the carbonizer 67. A heat collecting plate 74 is arranged above the carbonization plate 76, and the upper end of the heat collecting plate 74 is open.

[0067] The spacing between the multiple hot air inlets 73 is 0.5-1.0m, and the hot air inlet 73 is inclined at an angle of 5-10 degrees toward the first feed port 104. The heat collecting plate 74 is an arched structure, and the opening distance from the first feed port 104 is 0.2-0.4 times the length of the space in the carbonization chamber 65. There are three biomass gas outlets 72, one of which is located above the opening of the heat collecting plate 74, and the other two are located at both ends of the top of the carbonization chamber 65.

[0068] The first feeding system 66 includes a feeding table 77, a feeding bucket 78, a feeding platform 79, a feeding belt 80, a feeding hopper 81, a pushing system 82 and a reel 83. Reels 83 are arranged on both sides of the feeding belt 80. One end of the feeding belt 80 is arranged in the feeding hopper 81, and the other end is arranged on the feeding platform 79. A feeding bucket 78 is arranged at one end of the feeding platform 79. The feeding bucket 78 is located above the feeding table 77. The feeding bucket 78 is a feeding rotating eccentric form. A pushing system 82 is arranged in the feeding platform 79, and the output end of the pushing system 82 is arranged on the feeding table 77. The feeding table 77 is connected to the first feeding port 104.

[0069] The upper hopper 81, through the top reel 83, under the action of the motor, sends the processed material into the feed bucket 78 through the loading platform 79. The feed bucket 78 is a feeding rotating eccentric type. After the material falls on the feeding platform 77 below, it is sent to the carbonization plate 76 through the pushing system 82. The driver 86 is turned on, and the upper side of the carbonization plate 76 is covered with agricultural and forestry biomass waste under the drive of the front and rear rollers 84, and the driver 86 is closed at the same time.

[0070] Open the hot air inlet control valve 88, and the hot air enters the carbonization chamber 65. After an interval of 3-8 minutes, open the biomass gas control valve 89, and the combustible gas enters the pyrolysis gasification chamber 2 through the biomass gas reflux pipe 71. After the carbonization is completed and the tail gas is introduced for cooling, open the driver 86 to pull open the push-pull plate 85 to discharge the carbonized biochar material into the aggregate pit 75.

[0071] The metal pyrolysis recovery system includes a metal recovery pyrolysis chamber 90, a slag discharger 93 and a second feeding system 105. A second feed port 106 and a plurality of hot air inlets 73 are provided on the side wall of the metal recovery pyrolysis chamber 90. The second feed port 106 and the plurality of hot air inlets 73 are arranged opposite to each other. The second feed port 106 is connected to the second feeding system 105. A plurality of gas outlets 94 are provided on the top of the metal recovery pyrolysis chamber 90. A two-way grate 95 is provided inside the metal recovery pyrolysis chamber 90. The two-way grate 95 is connected to a driver 86. The front end of the two-way grate 95 is close to the second feed port 106, and the end is close to a receiving trough 96. A push-pull plate 85 is provided above the receiving trough 96. 0.55-0.85 times of the capacity of water is injected into the receiving trough 96. The receiving trough 96 is connected to the slag discharger 93.

[0072] The spacing between the multiple hot air inlets 73 is 0.3-0.5m, and the hot air inlet 73 is inclined at an angle of 3-8 degrees toward the second feed port 106 . There are two gas outlets 94 , which are located at both ends of the top of the metal recovery pyrolysis chamber 90 .

[0073] The second feeding system 105 includes a spiral feed hopper 91, a feeding plate 92, a feed trough 97 and a feeding screw 98. One end of the feeding plate 92 is arranged in the feed trough 97, and the other end is arranged on the spiral feed hopper 91. A feeding screw 98 is arranged in the spiral feed hopper 91, and the feeding screw 98 is connected to the second feed port 106.

[0074] The metal-containing waste in the feed trough 97 is transported to the spiral feed hopper 91 through the loading plate 92, and the processed metal-containing waste is sent to the two-way grate 95 under the action of the feed screw rod 98. The driver 86 is opened to cover the upper side of the grate with the metal-containing waste, and the driver 86 is closed at the same time; the hot air intake control valve 88 is opened, and the hot air enters the metal recovery pyrolysis chamber 90 to carbonize the metal-containing waste. At the same time, the biomass gas control valve 89 is opened, and the combustible gas enters the pyrolysis gasification chamber 2 through the biomass gas reflux pipe 71; after the carbonization is completed, the hot air intake control valve 88 is closed, and the driver 86 is opened to pull open the push-pull plate 85 to discharge the carbonized metal-containing waste into the receiving trough 96.

[0075] The hot air in the high-temperature cracking chamber 3 enters the carbonization chamber 65 and / or the metal recovery pyrolysis chamber 90 through the hot air pipe 68 and the hot air inlet 73, the combustible gas generated in the carbonization chamber 65 enters the pyrolysis gasification chamber 2 through the biomass gas outlet 72 and the biomass gas reflux pipe 71, and the combustible gas generated in the metal recovery pyrolysis chamber 90 enters the pyrolysis gasification chamber 2 through the gas outlet 94 and the biomass gas reflux pipe 71.

[0076] The thermal energy conversion of organic solid waste is completed through the pyrolysis gasification chamber 2, the high-temperature cracking chamber 3, the high-pressure steam room 4, the low-pressure steam room 5 and the hot water room 6, the carbonization process of agricultural and forestry biomass is completed through the carbonization chamber 65, and the separation of metal waste is completed through the metal recovery pyrolysis chamber 90. The solid waste heat treatment system can be operated simultaneously with the biomass carbonization system and the metal pyrolysis recovery system, and the solid waste heat treatment system can also be operated simultaneously with the biomass carbonization system or the metal pyrolysis recovery system alone.

[0077] Organic solid waste enters the pyrolysis gasification chamber 2 through the feeding system, and the generated pyrolysis gas enters the high-temperature cracking chamber 3 through the primary air outlet 27. After completing the internal circulation of the system through the secondary air outlet 29, it enters the high-pressure steam room 4, the low-pressure steam room 5, the hot water room 6 and the cyclone dust collector 7 in turn. The hot water room 6 regularly replenishes the hot water loss in the low-pressure steam room 5 through the hot water return pipe 62.

[0078] The cyclone dust collector 7 includes a cyclone dust chamber 42 and an ash collecting chamber 43. The exhaust pipe 44 is arranged in the cyclone dust chamber 42. The exhaust pipe 44 is a structure with a larger upper part and a smaller lower part. A dust removal hole 46 is arranged at the bottom of the cyclone dust chamber 42. The dust removal hole 46 is located in the ash collecting chamber 43. A dust removal plate 45 is arranged above the dust removal hole 46. Dust falls into the ash collecting chamber 43 through the dust removal hole 46.

[0079] The spray denitrification and denitration chamber 8 includes a spray chamber 49, a desulfurization chamber 54 and a denitration chamber 56. The spray chamber 49 is connected to a connecting pipe 48. A water tank is provided in the spray chamber 49. A plurality of nozzles 50 are connected to the lower part of the water tank. A waste liquid collection port 52 is provided at the bottom of the spray chamber 49. A waste water collection barrel 51 is provided below the waste liquid collection port 52. The spray chamber 49 is connected to the desulfurization chamber 54 through a desulfurization inlet 53. The desulfurization chamber 54 is connected to the denitration chamber 56 through a denitration inlet 55. The denitration chamber 56 is connected to the water bath purification chamber 9 through a second exhaust pipe 102. The desulfurization chamber 54 uses activated carbon material, and the denitration chamber 56 uses a mixture of activated carbon and iron oxide. Tap water is injected into the water tank, and the waste water entering the waste water collection barrel 51 through the waste liquid collection port 52 is evaporated and then reused in the spray chamber 49.

[0080] Under the action of the induced draft fan 47, the exhaust gas enters the spray denitrification and denitrification chamber 8 through the exhaust pipe 44 and the connecting pipe 48 of the cyclone dust collector 7, and after the dust is reduced by the spraying of the nozzle 50, it enters the desulfurization room 54 through the desulfurization inlet 53, and then enters the denitrification room 56 through the denitrification inlet 55. The gas after desulfurization and denitrification passes through the water bath purification chamber 9 and the electrostatic precipitator 10 in turn, and then enters the gas collector 12 through the tail gas collection pipe 57 to collect carbon dioxide. A part of the remaining tail gas enters the pyrolysis gasification chamber 2 through the tail gas reflux pipe 59, and the remaining gas enters the carbonization chamber 65 for completing the carbonization operation through the tail gas cooling and utilization pipe 63 or is discharged through the tail gas discharge port 60.

[0081] After the carbonization of the agricultural and forestry biomass waste in the carbonization chamber 65 is completed, the carbonization chamber 65 is opened to connect the exhaust gas cooling utilization control valve 64 on the exhaust gas cooling utilization pipe 63, and the exhaust gas external discharge control valve 61 and the gas reflux valve 58 are closed at the same time. After the temperature in the carbonization chamber 65 is lower than 200°C, the exhaust gas cooling utilization control valve 64 is closed, and the exhaust gas external discharge control valve 61 and the gas reflux valve 58 are opened at the same time to complete the cooling of the carbonization chamber 65; when the carbonization chamber 65 is cooled, the push-pull plate 85 and the driver 86 are opened, and the roller 84 drives the carbonization plate 76 to transport the carbonized agricultural and forestry biomass carbon material to the aggregate pit 75, and then the carbon discharge machine 67 is opened to complete the slag removal.

[0082] The tail gas collection pipe 57 is provided with a tail gas monitoring box 11, and a variety of different gas monitoring probes are provided in the tail gas monitoring box 11, and data is collected once every 20-120 minutes. The biomass carbonization system, the metal pyrolysis recovery system, the high-pressure steam room 4, and the left and right chambers of the high-temperature cracking chamber 3 are all provided with 2-6 pressure monitoring meters 69 and 2-6 temperature monitoring meters 70, and the pyrolysis gasification chamber 2, the low-pressure steam room 5 and the hot water room 6 are all provided with 2-6 temperature monitoring meters 70, and the third exhaust pipe 41 is provided with 1-2 temperature monitoring meters 70.

[0083] The gas collector 12 collects carbon dioxide by combining an upward exhaust method and an activated carbon pressure swing adsorption method. The upward exhaust method is first used to obtain carbon dioxide gas with a concentration higher than 50%, and then the activated carbon pressure swing adsorption method is used to obtain carbon dioxide gas with a concentration higher than 80%. The remaining tail gas enters the exhaust pipe 103.

[0084] The outer side of the pyrolysis gasification chamber 2 and the high-temperature cracking chamber 3 is a steel plate, and four layers of high-temperature resistant insulation layers are arranged from the outside to the inside, namely, refractory wool, refractory bricks, refractory cement and refractory coating. The rated steam pressure of the high-pressure steam room 4 is 2.0-3.0MPa, and the steam pressure of the low-pressure steam room 5 is 1.0-2.0MPa. The equipment realizes the energy utilization of textile waste, Chinese medicine residue, and urban sludge particles, realizes the preparation of straw biochar, the preparation of branch fuel charcoal, and realizes the recycling of metal zippers and aluminum metal. The equipment achieves an operating load of 0.5 to 5.0 tons / hour and achieves near-zero emissions of pollutants. Compared with similar equipment, the advantages are very obvious. The tail gas monitoring pollutant emission indicators are shown in Table 1. NOx, HCl, and total volatile organic compounds are all below the detection limit, the monitoring indicators are shown as zero, and other indicators are lower than the national standard limits.

[0085] Table 1 List of tail gas emission indicators

[0086]

[0087] Note: The national standard limit values ​​for total volatile organic compounds adopt the limits of other industry indicators in the "Volatile Organic Compound Emission Control Standards for Industrial Enterprises" (DB12 / 524-2020), and other indicators adopt the limits in the "Pollution Control Standards for the Incineration of Municipal Waste" (GB18485-2014).

[0088] Example 2: Taking textile waste steam utilization and metal zipper recycling as an example

[0089] like Figure 1 , Figure 2 and Figure 4As shown, the device includes a feeding system, a solid waste heat treatment system, a steam utilization system, a tail gas purification and recovery system and a metal pyrolysis recovery system, wherein the solid waste heat treatment system includes a pyrolysis gasification chamber 2 and a high-temperature cracking chamber 3, the steam utilization system includes a high-pressure steam room 4, a low-pressure steam room 5 and a hot water room 6, and the tail gas purification and recovery system includes a cyclone dust collector 7, a spray denitrification and denitrification chamber 8, a water bath purification chamber 9, an electrostatic precipitator 10, a tail gas monitoring box 11 and a gas collector 12. The metal pyrolysis recovery system includes a metal recovery pyrolysis chamber 90, a spiral feed hopper 91, a loading plate 92, a feed trough 97, a feeding screw rod 98 and a slag discharger 93; the feeding system includes a loading chamber 1, a gas separator 13, a push blower 14, a feeding box 15, a first conveyor belt 16, a feeding platform 17, a baffle plate 18 and a positioning plate 19, and the pyrolysis gasification chamber 2 is provided with a one-way grate 20, a discharge port 21, a front baffle plate 22, a rear baffle plate 23, a discharge plate 24, a discharge plate 25, a discharge plate 26, a discharge plate 27, a discharge plate 28, a discharge plate 29, a discharge plate 30, a discharge plate 31, a discharge plate 32, a discharge plate 33, a discharge plate 34, a discharge plate 35, a discharge plate 36, a discharge plate 37, a discharge plate 38, a discharge plate 39, a discharge plate 40, a discharge plate 41, a discharge plate 42, a discharge plate 43, a discharge plate 44, a discharge plate 45, a discharge plate 46, a discharge plate 47, a discharge plate 48, a discharge plate 49, a discharge plate 50, a discharge plate 51, a discharge plate 52, a discharge plate 53, a discharge plate 54, a discharge plate 55, a discharge plate 56, a discharge plate 57, a discharge plate 58, a discharge plate 59, a discharge plate 50, a discharge plate 5 The silo 24 and the air inlet 25 are connected to the pyrolysis gasification chamber 2 and the high-temperature cracking chamber 3 through a primary air vent 27. The high-temperature cracking chamber 3 is divided into two spaces, a left chamber and a right chamber. The left chamber is provided with an oxidant inlet 30, an exhaust port 31 and a dust outlet 32. The right chamber is provided with a dust outlet 32, an air inlet 38 and an additive inlet 39. The left chamber and the right chamber are connected through a secondary air vent 29. The high-temperature cracking chamber 3 and the high-pressure steam room 4 are connected through a first air duct 40. The low-pressure steam room 5 and the hot water room 6 are connected through the second air duct 99, the hot water room 6 and the cyclone dust collector 7 are connected through the third smoke exhaust pipe 41, the cyclone dust collector 7 and the spray denitrification and denitrification chamber 8 are connected through the connecting pipe 48, the spray denitrification and denitrification chamber 8 and the water bath purification chamber 9 are connected through the smoke exhaust pipe, the water bath purification chamber 9 and the electrostatic precipitator 10 are connected through the second smoke exhaust pipe 102, and the electrostatic precipitator 10 and the gas collector 12 are connected through the exhaust gas collection pipe 57. An exhaust gas monitoring box 11 is provided on the exhaust gas collecting pipe 57, and the gas collecting machine 12 is connected to the high-temperature cracking chamber 3 and the return fan 28 through the exhaust gas return pipe 59, and the return fan 28 is connected to the air inlet 25 of the pyrolysis gasification chamber 2 through the air inlet pipe 26; the metal recovery pyrolysis chamber 90 includes a hot air inlet 73, a push-pull plate 85, a driver 86, a gas outlet 94, a two-way grate 95 and a receiving trough 96, and the hot air in the high-temperature cracking chamber 3 enters the metal recovery pyrolysis chamber 90 through the hot air pipe 68 and the hot air inlet 73, and the combustible gas generated by the metal recovery pyrolysis chamber 90 enters the pyrolysis gasification chamber 2 through the gas outlet 94 and the biomass gas return pipe 71; the solid waste thermal treatment system processes textile waste, and the metal pyrolysis recovery system processes metal waste as zippers of clothing.

[0090] The pyrolysis gas generated by the textile waste entering the pyrolysis gasification chamber 2 through the feeding system enters the high-temperature cracking chamber 3 through the primary air outlet 27, and then enters the high-pressure steam room 4, the low-pressure steam room 5, the hot water room 6 and the cyclone dust collector 7 in sequence after completing the internal circulation of the system through the secondary air outlet 29. The hot water room 6 regularly supplies the low-pressure steam room 5 through the hot water return pipe 62; under the action of the induced draft fan 47, the exhaust gas enters the spray denitrification and denitration chamber 8 through the exhaust pipe 44 and the connecting pipe 48 of the cyclone dust collector 7, and enters the desulfurization room 54 through the desulfurization inlet 53 after the dust is reduced by the spraying of the nozzle 50, and then enters the denitration room 56 through the denitration inlet 55. The gas after desulfurization and denitration passes through the water bath purification chamber 9 and the electrostatic precipitator 10 in sequence, and then enters the gas collector 12 through the tail gas collection pipe 57 to collect carbon dioxide. A part of the remaining tail gas enters the pyrolysis gasification chamber 2 through the tail gas return pipe 59, and the remaining gas is discharged through the tail gas discharge port 60, and the position of the tail gas discharge port 60 is a three-way pipe.

[0091] The gas separator 13 separates nitrogen from the air, and the feed box 15 of the feed system conveys the textile waste to the loading chamber 1 through the first conveyor belt 16, and then the textile waste is transported to the feeding platform 17 through the second conveyor belt 110 inside the loading chamber 1, and the textile waste is blown into the one-way grate 20 of the pyrolysis gasification chamber 2 through the push blower 14; the textile waste in the pyrolysis gasification chamber 2 is pyrolyzed at 300-500°C, and the generated combustible gas enters the high-temperature cracking chamber 3 through the primary air outlet 27 and is high-temperature cracked for 3 seconds at 850-900°C. During the high-temperature cracking process, the left chamber is added with an oxidant through the oxidant inlet 30, and the right chamber is added with a biomass additive through the additive adding port 39; the first air duct 40 between the high-temperature cracking chamber 3 and the high-pressure steam room 4 is added with a biomass additive through the additive adding port 39.

[0092] The bottom of the left chamber of the high-temperature cracking chamber 3 is cleaned every 2 hours through a dust removal fan 33, and the dust cover 34 is connected by a spring and is opened only when cleaning to discharge the dust into a dust storage pit 35; the bottom of the right chamber is cleaned every 12 hours through a dust discharge port 32, and the ash is discharged into a dust storage tank 36; the high-pressure steam room 4, the low-pressure steam room 5 and the hot water room 6 are cleaned every 2 days; the cyclone dust collector 7 includes a cyclone dust removal chamber 42 and an ash collection chamber 43, the exhaust pipe 44 in the cyclone dust removal chamber 42 is large at the top and small at the bottom, and the dust falls into the ash collection chamber 43 through the dust removal hole 46, and the dust removal plate 45 is above the dust removal hole 46; the desulfurization room 54 uses activated carbon material, and the denitrification room 56 uses a mixture of activated carbon and iron oxide; probes for different monitoring gases are arranged in the exhaust gas monitoring box 11, and data are collected once every 20 minutes, and the gas collector 12 collects carbon dioxide.

[0093] The outer sides of the pyrolysis gasification chamber 2 and the high temperature cracking chamber 3 are steel plates, and four high temperature resistant insulation layers are arranged from the outside to the inside, namely, refractory wool, refractory bricks, refractory cement and refractory coating; the combustion aid inlet 30 is added with a gas containing more than 95% oxygen, and the added amount is 0.2-35m 3 / h; the additive added to the additive adding port 39 is a mixture of modified biochar, diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, gravel, volcanic rock, activated carbon and river sand, and the mixing ratio is 1:0.03:0.15:0.10:0.03:0.06:0.03:0.05:0.35:0.08; the modified biochar is a mixture of iron oxide modified biochar and potassium permanganate modified biochar, and the mixing ratio is 1:0.2, The particle sizes are all 0.5-2mm; the particle sizes of the diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, sandstone, volcanic rock, activated carbon and river sand are 0.1-1.0mm, 0.01-0.1mm, 0.25-2.0mm, 0.25-1.0mm, 0.1-1.0mm, 0.25-5.0mm, 0.5-2.0mm, 0.1-2.0mm, and 0.1-1.0mm respectively, and the activated carbon is coal-based activated carbon.

[0094] The hot air inlet 73 of the metal recovery pyrolysis chamber 90 is set at a spacing of 0.3m and is inclined at an angle of 3 degrees in the feeding direction of the metal recovery pyrolysis chamber 90; the gas outlet 94 is set at two ends of the top of the metal recovery pyrolysis chamber 90; the metal-containing waste in the feed trough 97 is transported to the spiral feed hopper 91 through the loading plate 92, and the processed metal-containing waste is sent to the two-way grate 95 under the action of the feeding screw rod 98, and the driver 86 is opened to cover the upper side of the grate with metal-containing waste, and the driver 86 is closed at the same time; the hot air intake control valve 88 is opened, and the hot air enters the metal recovery pyrolysis chamber 90 to separate the metal-containing waste, and the biomass gas control valve 89 is opened at the same time, and the combustible gas enters the pyrolysis gasification chamber 2 through the biomass gas reflux pipe 71; after the separation is completed, the hot air intake control valve 88 is closed, and the driver 86 is opened to pull the push-pull plate 85 to discharge the separated metal-containing waste into the receiving trough 96, and the receiving trough 96 is injected with 0.55 times the capacity of water.

[0095] The metal recovery pyrolysis chamber 90 is provided with two pressure monitoring gauges 69 and two temperature monitoring gauges 70, the pyrolysis gasification chamber 2 is provided with two temperature monitoring gauges 70, the left chamber and the right chamber of the high-temperature cracking chamber 3 are provided with two pressure monitoring gauges 69 and two temperature monitoring gauges 70, the high-pressure steam room 4 is provided with two pressure monitoring gauges 69 and two temperature monitoring gauges 70, the hot water room 6 is provided with two temperature monitoring gauges 70, and the third smoke exhaust pipe 41 between the water bath purification chamber 9 and the electrostatic precipitator 10 is provided with one temperature monitoring gauge 70.

[0096] The secondary air volume entering the pyrolysis gasification chamber 2 through the air inlet pipe 26 is 0.15 times the air volume of the push blower 14. The amount of reflux gas in the gas collector 12 and the left and right chambers of the high-temperature cracking chamber 3 is controlled by the gas reflux valve 58; the hot water in the hot water room 6 is replenished through the hot water reflux pipe 62 to replenish the hot water loss in the high-pressure steam room 4 and the low-pressure steam room 5.

[0097] The water content of the textile waste is 15-20% and the calorific value is 4000-4500 kcal / kg, and the water content of the metal waste is less than 10%; the flow rate of the flow regulating fan 37 is 50m 3 / h, the hot air from the left chamber of the high-temperature cracking chamber 3 is pumped to the right chamber; tap water is injected into the spray chamber 49, and the waste water entering the wastewater collection barrel 51 through the waste liquid collection port 52 is evaporated and reused in the spray chamber 49; the exhaust port 31 in the right chamber of the high-temperature cracking chamber 3 is located on the right side, and the exhaust port 31 in the left chamber is located in the middle and on the right side, and the exhaust flow rate of the hot air discharged from the exhaust port 31 in the left chamber is 1.5 times that of the right chamber; the return air volume of the gas collector 12 is 0.15 times that of the high-temperature cracking chamber 3, and the flow rate of the air inlet pipe 26 in the pyrolysis gasification chamber 2 is 100m 3 / h; the gas separator 13 adopts membrane separation technology to remove nitrogen from the air, and the oxygen content of the separated gas is 90-95%, and enters the pyrolysis gasification chamber 2 under the action of the push blower 14; the gas collector 12 adopts a method combining upward exhaust method and activated carbon pressure swing adsorption method, firstly performing upward exhaust method to obtain CO2 gas with a concentration higher than 50%, and then using activated carbon pressure swing adsorption method to obtain CO2 gas with a concentration higher than 80%; the rated steam pressure of the high-pressure steam room 4 is 2.5MPa, and the steam pressure of the low-pressure steam room 5 is 1.5MPa.

[0098] The operating load of the device in this embodiment is 0.5 tons / hour, and the volume of the pyrolysis gasification chamber 2 is 4.5m 3 , and other equipment is matched with it; the experimental results show that the thermal energy conversion rate of textile waste is as high as 86%-93%, the metal content after purification is 89%-92%, the device can reduce the exhaust gas generation by 30-35%, reduce the exhaust gas treatment cost by 80-85%, reduce the CO2 recovery cost in the exhaust gas by 30-36%, and improve the operating efficiency by 40-45%, meeting the conditions for continuous operation. The exhaust gas monitoring pollutant emission indicators are shown in Table 2. NOx, HCl, and total volatile organic compounds are all below the detection limit, the monitoring indicators are zero, and other indicators are also below the national standard limits.

[0099] Table 2 List of exhaust emission indicators

[0100]

[0101]

[0102] Note: The national standard limit values ​​for total volatile organic compounds adopt the limits of other industry indicators in the "Volatile Organic Compound Emission Control Standards for Industrial Enterprises" (DB12 / 524-2020), and other indicators adopt the limits in the "Pollution Control Standards for the Incineration of Municipal Waste" (GB18485-2014).

[0103] Example 3: Taking steam utilization of traditional Chinese medicine residue and preparation of straw biochar as an example

[0104] like Figure 1 , Figure 2 and Figure 3As shown, the device includes a feeding system, a solid waste heat treatment system, a steam utilization system, an exhaust gas purification and recovery system and a biomass carbonization system, wherein the solid waste heat treatment system includes a pyrolysis gasification chamber 2 and a high-temperature cracking chamber 3, the steam utilization system includes a high-pressure steam room 4, a low-pressure steam room 5 and a hot water room 6, the exhaust gas purification and recovery system includes a cyclone dust collector 7, a spray denitrification and denitrification chamber 8, a water bath purification chamber 9, an electrostatic precipitator 10, an exhaust gas monitoring box 11 and a gas collector 12, the biomass carbonization system includes a feeding system 66, a carbonization chamber 65 and a carbon discharger 67; the feeding system includes a feeding chamber 1, a gas separator 13, a push blower 14, a feeding box 15, a conveyor belt, an inlet The pyrolysis and gasification chamber 2 is provided with a one-way grate 20, a discharge port 21, a front baffle 22, a rear baffle 23, a discharge bin 24 and an air inlet 25. The pyrolysis and gasification chamber 2 is connected with the high-temperature cracking chamber 3 through a primary air outlet 27. The high-temperature cracking chamber 3 is divided into two spaces, a left chamber and a right chamber. The left chamber is provided with an combustion-supporting agent inlet 30, an exhaust port 31 and a dust outlet 32. The right chamber is provided with a dust outlet 32, an air inlet 38 and an additive addition port 39. The left chamber and the right chamber are connected through a secondary air outlet 29; the high-temperature cracking chamber 3 and the high-pressure steam room 4 are connected through a first air duct 40, and the low-pressure steam room 5 and the hot water room 6 are connected through a second air duct 40. The hot water room 6 and the cyclone dust collector 7 are connected through the first smoke exhaust pipe 101, the cyclone dust collector 7 and the spray denitrification and denitrification chamber 8 are connected through the connecting pipe 48, the spray denitrification and denitrification chamber 8 and the water bath purification chamber 9 are connected through the second smoke exhaust pipe 102, the water bath purification chamber 9 and the electrostatic precipitator 10 are connected through the third smoke exhaust pipe 41, and the electrostatic precipitator 10 and the gas collector 12 are connected through the tail gas collection pipe 57; the tail gas collection pipe 57 is provided with a tail gas monitoring box 11, the gas collector 12 is connected with the high temperature cracking chamber 3 and the reflux fan 28 through the tail gas return pipe 59, and the reflux fan 28 is connected with the air inlet 25 of the pyrolysis gasification chamber 2 through the air inlet pipe 26; The carbonization chamber 65 includes a biomass gas outlet 72, a hot air inlet 73, a heat collecting plate 74, a collection pit 75, a carbonization plate 76, a roller 84, a push-pull plate 85, a driver 86 and a cooling gas inlet 87; the feeding system 66 includes a feeding platform 77, a feeding bucket 78, a feeding platform 79, a feeding belt 80, a feeding bucket 81, a pushing system 82 and a scroll 83. The hot air in the high-temperature cracking chamber 3 enters the carbonization chamber 65 through the hot air pipe 68 and the hot air inlet 73, and the combustible gas generated in the carbonization chamber 65 enters the pyrolysis gasification chamber 2 through the biomass gas outlet 72 and the biomass gas reflux pipe 71; the solid waste thermal treatment system processes Chinese medicine residue, and the carbonization chamber 65 processes corn stalks.

[0105] The Chinese medicine residue enters the pyrolysis gasification chamber 2 through the feeding system, and the pyrolysis gas generated enters the high-temperature cracking chamber 3 through the primary air outlet 27, and then enters the high-pressure steam room 4, the low-pressure steam room 5, the hot water room 6 and the cyclone dust collector 7 in sequence after completing the internal circulation of the system through the secondary air outlet 29. The hot water room 6 regularly supplies the low-pressure steam room 5 through the hot water return pipe 62; under the action of the induced draft fan 47, the exhaust gas enters the spray denitrification and denitration chamber 8 through the exhaust pipe 44 and the connecting pipe 48 of the cyclone dust collector 7, and after the dust is reduced by the spray of the nozzle 50, it enters the desulfurization room 54 through the desulfurization inlet 53, and then enters the denitration room 56 through the denitration inlet 55. The gas after desulfurization and denitration passes through the water bath purification chamber 9 and the electrostatic precipitator 10 in sequence, and then enters the gas collector 12 through the tail gas collection pipe 57 to collect carbon dioxide, and a part of the remaining tail gas passes through the tail gas return pipe 59 Entering the pyrolysis gasification chamber 2, the remaining gas enters the carbonization chamber 65 where the carbonization operation is completed through the tail gas cooling and utilization pipe 63 or is discharged through the tail gas discharge port 60, and the tail gas discharge port 60 is located as a three-way pipe; after the carbonization of the corn stalks in the carbonization chamber 65 is completed, the tail gas cooling and utilization control valve 64 connected to the tail gas cooling and utilization pipe 63 of the carbonization chamber 65 is opened, and the tail gas discharge control valve 61 and the gas reflux valve 58 are closed at the same time, and the tail gas cooling and utilization control valve 64 is closed after the temperature in the carbonization chamber 65 is lower than 200°C, and the tail gas discharge control valve 61 and the gas reflux valve 58 are opened at the same time to complete the cooling of the carbonization chamber 65; when the carbonization chamber 65 is cooled, the push-pull plate 85 and the driver 86 are opened, and the roller 84 drives the carbonization plate 76 to transport the carbonized corn stalk biochar material to the aggregate pit 75, and then the carbon discharger 67 is opened to complete the slag removal.

[0106] The gas separator 13 separates nitrogen from the air, the feed box 15 of the feed system conveys the Chinese medicine residue to the loading chamber 1 through the first conveyor belt 16, and then transports the Chinese medicine residue to the feeding platform 17 through the second conveyor belt 110 inside the loading chamber 1, and blows the organic waste into the one-way grate 20 of the pyrolysis gasification chamber 2 through the push blower 14; the organic waste in the pyrolysis gasification chamber 2 is pyrolyzed at 300-500°C, and the generated combustible gas enters the high-temperature cracking chamber 3 through the primary air outlet 27 and is pyrolyzed at 900-1000°C for 5 seconds. During the high-temperature cracking process, the left chamber is added with an oxidant through the oxidant inlet 30, and the right chamber is added with a biomass additive through the additive inlet 39; the first air duct 40 between the high-temperature cracking chamber 3 and the high-pressure steam room 4 is added with a biomass additive through the additive inlet 39.

[0107] The bottom of the left chamber of the high-temperature cracking chamber 3 is cleaned every 6 hours through a dust removal fan 33, and the dust cover 34 is connected by a spring and is opened only when cleaning to discharge the dust into a dust storage pit 35; the bottom of the right chamber is cleaned every 18 hours through a dust discharge port 32, and the ash is discharged into a dust storage tank 36; the high-pressure steam room 4, the low-pressure steam room 5 and the hot water room 6 are cleaned every 4 days; the cyclone dust collector 7 includes a cyclone dust removal chamber 42 and an ash collection chamber 43, the exhaust pipe 44 in the cyclone dust removal chamber 42 is large at the top and small at the bottom, and the dust falls into the ash collection chamber 43 through the dust removal hole 46, and the dust removal plate 45 is above the dust removal hole 46; the desulfurization room 54 uses activated carbon material, and the denitrification room 56 uses a mixture of activated carbon and iron oxide; probes for different monitoring gases are arranged in the exhaust gas monitoring box 11, and data are collected once every 60 minutes, and the gas collector 12 collects carbon dioxide.

[0108] The outer sides of the pyrolysis gasification chamber 2 and the high-temperature cracking chamber 3 are steel plates, and four layers of high-temperature resistant insulation layers are arranged from the outside to the inside, namely, refractory wool, refractory bricks, refractory cement and refractory coating; the combustion aid inlet 30 adds a combustion aid of pine biochar powder with a calorific value of 5000-7500 kcal / kg, and the addition amount is 0.2-0.45 kg / min; the additive inlet 39 adds an additive of a mixture of modified biochar, diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, sand, volcanic rock, activated carbon and river sand, and the mixing ratio is 1:0.04:0.2:0.15:0.04:0.08:0.05: 0.1:0.45:0.09; the modified biochar is a mixture of iron oxide modified biochar and potassium permanganate modified biochar, the mixing ratio is 1:0.4, and the particle size is 0.5-2mm; the particle sizes of the diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, sandstone, volcanic rock, activated carbon and river sand are 0.1-1.0mm, 0.01-0.1mm, 0.25-2.0mm, 0.25-1.0mm, 0.1-1.0mm, 0.25-5.0mm, 0.5-2.0mm, 0.1-2.0mm, 0.1-1.0mm, respectively, and the activated carbon is coal-based activated carbon.

[0109] The hot air inlet 73 of the carbonization chamber 65 is arranged at a spacing of 0.5m and is inclined at an angle of 10 degrees toward the feed port of the carbonization chamber 65; the heat collecting plate 74 is arranged in an arch shape, and the outlet is 0.2 times the length of the space in the carbonization chamber 65 from the feed side; three biomass gas outlets 72 are arranged, one is located above the outlet of the heat collecting plate 74, and the other two are located at both ends of the top of the carbonization chamber 65; the upper hopper 81 sends the processed material through the upper platform 79 into the feed tipping bucket 78 under the action of the motor through the scroll 83 at the top, and the feed tipping bucket 78 is a feeding rotating bucket In an eccentric form, the material falls onto the feeding table 77 below and is fed to the carbonization plate 76 through the pushing system 82. The driver 86 is turned on, and the upper carbonization plate 76 is covered with corn stalks driven by the front and rear rollers 84, and the driver 86 is closed at the same time. The hot air intake control valve 88 is opened, and the hot air enters the carbonization chamber 65. After an interval of 3 minutes, the biomass gas control valve 89 is opened, and the combustible gas enters the pyrolysis gasification chamber 2 through the biomass gas reflux pipe 71. After the carbonization is completed, the tail gas is introduced for cooling, and the driver 86 is opened to pull open the push-pull plate 85 to discharge the carbonized biochar material into the aggregate pit 75.

[0110] The carbonization chamber 65 is provided with two pressure monitoring gauges 69 and two temperature monitoring gauges 70, the pyrolysis gasification chamber 2 is provided with two temperature monitoring gauges 70, the left chamber and the right chamber of the high-temperature cracking chamber 3 are provided with two pressure monitoring gauges 69 and two temperature monitoring gauges 70, the high-pressure steam room 4 is provided with two pressure monitoring gauges 69 and two temperature monitoring gauges 70, the hot water room 6 is provided with two temperature monitoring gauges 70, and the third smoke exhaust pipe 41 between the water bath purification chamber 9 and the electrostatic precipitator 10 is provided with one temperature monitoring gauge 70.

[0111] The secondary air volume entering the pyrolysis gasification chamber 2 through the air inlet pipe 26 is 0.35 times the air volume of the push blower 14. The amount of reflux gas in the gas collector 12 and the left and right chambers of the high-temperature cracking chamber 3 is controlled by the gas reflux valve 58; the hot water in the hot water room 6 is replenished through the hot water reflux pipe 62 to replenish the hot water loss in the high-pressure steam room 4 and the low-pressure steam room 5.

[0112] The water content of the traditional Chinese medicine residue is 12-18% and the calorific value is 3200-3500 kcal / kg. The agricultural and forestry biomass waste corn stalks are first pressed into particles, and the particle size is 10-30 mm when prepared into biochar; the water content of the agricultural and forestry biomass waste prepared into biochar raw materials is less than 20%, and they are first prepared into particles and then dried.

[0113] The flow rate of the flow regulating fan 37 is 150m 3 / h, the hot air from the left chamber of the high-temperature cracking chamber 3 is pumped to the right chamber; tap water is injected into the spray chamber 49, and the wastewater entering the wastewater collection barrel 51 through the waste liquid collection port 52 is evaporated and reused in the spray chamber 49; the exhaust port 31 in the right chamber of the high-temperature cracking chamber 3 is located on the right side, and the exhaust port 31 in the left chamber is located in the middle and on the right side, and the exhaust flow rate of the hot air discharged from the exhaust port 31 in the left chamber is 2.2 times that of the right chamber; the return air volume of the gas collector 12 is 0.25 times that of the high-temperature cracking chamber 3, and the flow rate of the air inlet pipe 26 in the pyrolysis gasification chamber 2 is 300m 3 / h; the gas separator 13 adopts membrane separation technology to remove nitrogen from the air, and the oxygen content of the separated gas is 92-97%, and enters the pyrolysis gasification chamber 2 under the action of the push blower 14; the gas collector 12 adopts a method combining upward exhaust method and activated carbon pressure swing adsorption method, firstly performing upward exhaust method to obtain carbon dioxide gas with a concentration higher than 50%, and then using activated carbon pressure swing adsorption method to obtain carbon dioxide gas with a concentration higher than 80%; the rated steam pressure of the high-pressure steam room 4 is 2.0MPa, and the steam pressure of the low-pressure steam room 5 is 1.0MPa.

[0114] The operating load of the device in this embodiment is 1.0 ton / hour, and the volume of the pyrolysis gasification chamber 2 is 8.0m 3 , and other equipment is matched with it; the experimental results show that the thermal energy conversion rate of Chinese medicine residue is as high as 85%-90%, the biochar yield is 32-35%, the device can reduce the exhaust gas generation by 32-39%, reduce the cost of carbon dioxide recovery in the exhaust gas by 35-45%, improve the operating efficiency by 40-49%, reduce the exhaust gas treatment cost by 85-92%, and achieve continuous operation. The exhaust gas monitoring pollutant emission indicators are shown in Table 3. NOx, SO2, HCl, and total volatile organic compounds are all below the detection limit, the monitoring indicators are zero, and other indicators are also below the national standard limits.

[0115] Table 3 List of tail gas emission indicators

[0116]

[0117] Note: The national standard limit values ​​for total volatile organic compounds adopt the limits of other industry indicators in the "Volatile Organic Compound Emission Control Standards for Industrial Enterprises" (DB12 / 524-2020), and other indicators adopt the limits in the "Pollution Control Standards for the Incineration of Municipal Waste" (GB18485-2014).

[0118] Example 4: Taking the steam utilization of municipal sludge particles and the preparation of tree branch fuel charcoal as an example

[0119] like Figure 1 , Figure 2 and Figure 3As shown, the device includes a feeding system, a solid waste heat treatment system, a steam utilization system, an exhaust gas purification and recovery system and a biomass carbonization system. The solid waste heat treatment system includes a pyrolysis gasification chamber 2 and a high-temperature cracking chamber 3. The steam utilization system includes a high-pressure steam room 4, a low-pressure steam room 5 and a hot water room 6. The exhaust gas purification and recovery system includes a cyclone dust collector 7, a spray denitrification and denitrification chamber 8, a water bath purification chamber 9, an electrostatic precipitator 10, an exhaust gas monitoring box 11 and a gas collector 12. The biomass carbonization system includes a feeding system 66, a carbonization chamber 65 and a carbon discharger 67; the feeding system includes a feeding chamber 1, a gas separator 13, a push blower 14, a feeding box 15, a conveyor belt, and a feeding platform 17. , baffle plate 18 and positioning plate 19, the pyrolysis gasification chamber 2 is provided with a one-way grate 20, a discharge port 21, a front baffle plate 22, a rear baffle plate 23, a slag discharge bin 24 and an air inlet 25, the pyrolysis gasification chamber 2 and the high-temperature cracking chamber 3 are connected through a primary air outlet 27, the high-temperature cracking chamber 3 is divided into two spaces, a left chamber and a right chamber, the left chamber is provided with an combustion-supporting agent inlet 30, an exhaust port 31 and a dust outlet 32, the right chamber is provided with a dust outlet 32, an air inlet 38 and an additive addition port 39, the left chamber and the right chamber are connected through a secondary air outlet 29; the high-temperature cracking chamber 3 and the high-pressure steam room 4 are connected through a first air duct 40, and the low-pressure steam room 5 and the hot water room 6 are connected through a second air duct 99, The hot water room 6 and the cyclone dust collector 7 are connected through the first exhaust pipe 101, the cyclone dust collector 7 and the spray denitrification and denitrification chamber 8 are connected through the connecting pipe 48, the spray denitrification and denitrification chamber 8 and the water bath purification chamber 9 are connected through the second exhaust pipe 102, the water bath purification chamber 9 and the electrostatic precipitator 10 are connected through the third exhaust pipe 41, and the electrostatic precipitator 10 and the gas collector 12 are connected through the tail gas collection pipe 57; the tail gas collection pipe 57 is provided with a tail gas monitoring box 11, the gas collector 12 is connected to the high temperature cracking chamber 3 and the reflux fan 28 through the tail gas return pipe 59, and the reflux fan 28 is connected to the air inlet 25 of the pyrolysis gasification chamber 2 through the air inlet pipe 26; the carbonization chamber 65 includes a biomass Gas outlet 72, hot air inlet 73, heat collecting plate 74, aggregate pit 75, carbonization plate 76, roller 84, push-pull plate 85, driver 86 and cooling gas inlet 87; feeding system 66 includes feeding platform 77, feeding bucket 78, feeding platform 79, feeding belt 80, feeding bucket 81, pushing system 82 and scroll 83. The hot air in high temperature cracking chamber 3 enters carbonization chamber 65 through hot air pipe 68 and hot air inlet 73. The combustible gas generated by carbonization chamber 65 enters pyrolysis gasification chamber 2 through biomass gas outlet 72 and biomass gas reflux pipe 71. The solid waste thermal treatment system treats urban sludge particles, and the agricultural and forestry biomass waste treated by carbonization chamber 65 is pine branches.

[0120] The municipal sludge particles enter the pyrolysis gasification chamber 2 through the feeding system, and the pyrolysis gas generated enters the high-temperature cracking chamber 3 through the primary air outlet 27, and then enters the high-pressure steam room 4, the low-pressure steam room 5, the hot water room 6 and the cyclone dust collector 7 in turn after completing the internal circulation of the system through the secondary air outlet 29. The hot water room 6 regularly supplies the low-pressure steam room 5 through the hot water return pipe 62; under the action of the induced draft fan 47, the exhaust gas enters the spray denitrification and denitrification chamber 8 through the exhaust pipe 44 and the connecting pipe 48 of the cyclone dust collector 7, and after the dust is reduced by the spray of the nozzle 50, it enters the desulfurization room 54 through the desulfurization inlet 53, and then enters the denitrification room 56 through the denitrification inlet 55. The gas after desulfurization and denitrification passes through the water bath purification chamber 9 and the electrostatic precipitator 10 in turn, and then enters the gas collector 12 through the tail gas collection pipe 57 to collect carbon dioxide, and a part of the remaining tail gas passes through the tail gas return pipe 59 enters the pyrolysis gasification chamber 2, and the remaining gas enters the carbonization chamber 65 where the carbonization operation is completed through the tail gas cooling and utilization pipe 63 or is discharged through the tail gas discharge port 60, and the position of the tail gas discharge port 60 is a three-way pipe; after the carbonization of the pine branches in the carbonization chamber 65 is completed, the tail gas cooling and utilization control valve 64 connected to the tail gas cooling and utilization pipe 63 of the carbonization chamber 65 is opened, and the tail gas discharge control valve 61 and the gas reflux valve 58 are closed at the same time, and after the temperature in the carbonization chamber 65 is lower than 200°C, the tail gas cooling and utilization control valve 64 is closed, and the tail gas discharge control valve 61 and the gas reflux valve 58 are opened at the same time to complete the cooling of the carbonization chamber 65; when the carbonization chamber 65 is cooled, the push-pull plate 85 and the driver 86 are opened, and the roller 84 drives the carbonization plate 76 to transport the carbonized pine branch fuel carbon material to the aggregate pit 75, and then the carbon discharger 67 is opened to complete the slag removal.

[0121] The gas separator 13 is used to separate nitrogen from the air. The feed box 15 of the feed system conveys the municipal sludge particles to the loading chamber 1 through the first conveyor belt 16, and then transports the municipal sludge particles to the feeding platform 17 through the second conveyor belt 110 inside the loading chamber 1, and blows the municipal sludge particles into the one-way grate 20 of the pyrolysis gasification chamber 2 through the push blower 14; the municipal sludge particles in the pyrolysis gasification chamber 2 are pyrolyzed at 300-500°C, and the generated combustible gas enters the high-temperature cracking chamber 3 through the primary air outlet 27 and is pyrolyzed at 850-950°C for 4 seconds. During the high-temperature cracking process, the left chamber is added with an oxidant through the oxidant inlet 30, and the right chamber is added with a biomass additive through the additive adding port 39; the first air duct 40 between the high-temperature cracking chamber 3 and the high-pressure steam room 4 is added with a biomass additive through the additive adding port 39.

[0122] The bottom of the left chamber of the high-temperature cracking chamber 3 is cleaned every 3 hours through a dust removal fan 33, and the dust cover 34 is connected by a spring and is opened only when cleaning to discharge the dust into a dust storage pit 35; the bottom of the right chamber is cleaned every 15 hours through a dust discharge port 32, and the ash is discharged into a dust storage tank 36; the high-pressure steam room 4, the low-pressure steam room 5 and the hot water room 6 are cleaned every 3 days; the cyclone dust collector 7 includes a cyclone dust removal chamber 42 and an ash collection chamber 43, the exhaust pipe 44 in the cyclone dust removal chamber 42 is large at the top and small at the bottom, and the dust falls into the ash collection chamber 43 through the dust removal hole 46, and the dust removal plate 45 is above the dust removal hole 46; the desulfurization room 54 uses activated carbon material, and the denitrification room 56 uses a mixture of activated carbon and iron oxide; probes for different monitoring gases are arranged in the exhaust gas monitoring box 11, and data are collected once every 120 minutes, and the gas collector 12 collects carbon dioxide.

[0123] The outer sides of the pyrolysis gasification chamber 2 and the high-temperature cracking chamber 3 are steel plates, and four layers of high-temperature resistant insulation layers are arranged from the outside to the inside, namely, refractory wool, refractory bricks, refractory cement and refractory coating; the combustion aid inlet 30 adds a combustion aid of coke powder with a calorific value of 7000-9000kcal / kg, and the addition amount is 0.35-0.85kg / min; the additive added at the additive adding port 39 is a mixture of modified biochar, diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, sandstone, volcanic rock, activated carbon and river sand, and the mixing ratio is 1:0.08:0.35:0.25:0.05:0.09:0.08:0 .12:0.55:0.12; the modified biochar is a mixture of iron oxide modified biochar and potassium permanganate modified biochar, the mixing ratio is 1:0.5, and the particle size is 0.5-2mm; the particle sizes of the diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, sandstone, volcanic rock, activated carbon and river sand are 0.1-1.0mm, 0.01-0.1mm, 0.25-2.0mm, 0.25-1.0mm, 0.1-1.0mm, 0.25-5.0mm, 0.5-2.0mm, 0.1-2.0mm, 0.1-1.0mm, respectively, and the activated carbon is coal-based activated carbon.

[0124] The hot air inlet 73 of the carbonization chamber 65 is arranged at a spacing of 1.0m and is inclined at an angle of 5 degrees in the direction of the feed port of the carbonization chamber 65; the heat collecting plate 74 is arranged in an arch shape, and the outlet is 0.4 times the length of the space in the carbonization chamber 65 from the feed side; the biomass gas outlet 72 is arranged in three, one is located above the outlet of the heat collecting plate 74, and the other two are located at both ends of the top of the carbonization chamber 65; the upper hopper 81 sends the processed material through the upper platform 79 into the feed tipping bucket 78 under the action of the motor through the top reel 83, and the feed tipping bucket 78 is a feeding rotating eccentric In the form of, after the material falls onto the feeding table 77 below, it is sent to the carbonization plate 76 through the pushing system 82, the driver 86 is turned on, and the upper carbonization plate 76 is covered with agricultural and forestry biomass waste under the drive of the front and rear rollers 84, and the driver 86 is closed at the same time; the hot air intake control valve 88 is opened, and the hot air enters the carbonization chamber 65. After an interval of 8 minutes, the biomass gas control valve 89 is opened, and the combustible gas enters the pyrolysis gasification chamber 2 through the biomass gas reflux pipe 71; after the carbonization is completed and the tail gas is cooled, the driver 86 is opened to pull open the push-pull plate 85 to discharge the carbonized biochar material into the aggregate pit 75.

[0125] The carbonization chamber 65 is provided with 4 pressure monitoring meters 69 and 4 temperature monitoring meters 70, the pyrolysis gasification chamber 2 is provided with 4 temperature monitoring meters 70, the left chamber and the right chamber of the high-temperature cracking chamber 3 are provided with 4 pressure monitoring meters 69 and 4 temperature monitoring meters 70, the high-pressure steam room 4 is provided with 4 pressure monitoring meters 69 and 4 temperature monitoring meters 70, the hot water room 6 is provided with 4 temperature monitoring meters 70, and the third smoke exhaust pipe 41 between the water bath purification chamber 9 and the electrostatic precipitator 10 is provided with 1 temperature monitoring meter 70.

[0126] The secondary air volume entering the pyrolysis gasification chamber 2 through the air inlet pipe 26 is 0.25 times the air volume of the push blower 14. The amount of reflux gas in the gas collector 12 and the left and right chambers of the high-temperature cracking chamber 3 is controlled by the gas reflux valve 58; the hot water in the hot water room 6 is supplied to the hot water loss in the high-pressure steam room 4 and the low-pressure steam room 5 through the hot water reflux pipe 62.

[0127] The urban sludge particles have a moisture content of 10-15% and a calorific value of 2000-3100 kcal / kg. The agricultural and forestry biomass waste is first pressed into a particle size of 20-50 mm, and a columnar diameter and length of 20-80 mm and 100-300 mm respectively; the agricultural and forestry biomass waste is prepared into fuel charcoal raw materials with a moisture content of less than 20%, first prepared into particles, and then dried.

[0128] The flow rate of the flow regulating fan 37 is 300m 3 / h, the hot air from the left chamber of the high-temperature cracking chamber 3 is pumped to the right chamber; tap water is injected into the spray chamber 49, and the wastewater entering the wastewater collection barrel 51 through the waste liquid collection port 52 is evaporated and reused in the spray chamber 49; the exhaust port 31 in the right chamber of the high-temperature cracking chamber 3 is located on the right side, and the exhaust port 31 in the left chamber is located in the middle and on the right side, and the exhaust flow rate of the hot air discharged from the exhaust port 31 in the left chamber is 2.0 times that of the right chamber; the return air volume of the gas collector 12 is 0.2 times that of the high-temperature cracking chamber 3, and the flow rate of the air inlet pipe 26 in the pyrolysis gasification chamber 2 is 500m 3 / h; the gas separator 13 adopts membrane separation technology to remove nitrogen from the air, and the oxygen content of the separated gas is 95-99%, and enters the pyrolysis gasification chamber 2 under the action of the push blower 14; the gas collector 12 adopts a method combining upward exhaust method and activated carbon pressure swing adsorption method, firstly performing upward exhaust method to obtain carbon dioxide gas with a concentration higher than 50%, and then using activated carbon pressure swing adsorption method to obtain carbon dioxide gas with a concentration higher than 80%; the rated steam pressure of the high-pressure steam room 4 is 3.0MPa, and the steam pressure of the low-pressure steam room 5 is 1.99MPa.

[0129] The operating load of the device in this embodiment is 2.0 tons / hour, and the volume of the pyrolysis gasification chamber 2 is 18m 3 , and other equipment is matched with it; the experimental results show that the thermal energy conversion rate of urban sludge particles is as high as 85%-87%, the calorific value of fuel carbon is as high as 4500-5300kcal / kg, the device can reduce the exhaust gas generation by 32-37%, reduce the exhaust gas treatment cost by 81-89%, reduce the CO2 recovery cost in the exhaust gas by 32-36%, and improve the operating efficiency by 43-50%, meeting the conditions for continuous operation. The exhaust gas monitoring pollutant emission indicators are shown in Table 4. NOx, HCl, and total volatile organic compounds are all below the detection limit, the monitoring indicators are zero, and other indicators are also much lower than the national standard limits.

[0130] Table 4 List of tail gas emission indicators

[0131]

[0132] Note: The national standard limit values ​​for total volatile organic compounds adopt the limits of other industry indicators in the "Volatile Organic Compound Emission Control Standards for Industrial Enterprises" (DB12 / 524-2020), and other indicators adopt the limits in the "Pollution Control Standards for the Incineration of Municipal Waste" (GB18485-2014).

[0133] Example 5: Taking textile waste steam utilization, sunflower straw biochar preparation and aluminum metal recovery as examples

[0134] like Figures 1 to 4As shown, the device includes a feeding system, a solid waste heat treatment system, a steam utilization system, an exhaust gas purification and recovery system, a biomass carbonization system and a metal pyrolysis recovery system, wherein the solid waste heat treatment system includes a pyrolysis gasification chamber 2 and a high-temperature cracking chamber 3, the steam utilization system includes a high-pressure steam room 4, a low-pressure steam room 5 and a hot water room 6, the exhaust gas purification and recovery system includes a cyclone dust collector 7, a spray denitrification and denitrification chamber 8, a water bath purification chamber 9, an electrostatic precipitator 10, an exhaust gas monitoring box 11 and a gas collector 12, the biomass carbonization system includes a feeding system 66, a carbonization chamber 65 and a charcoal discharger 67, the metal pyrolysis recovery system The system includes a metal recovery pyrolysis chamber 90, a spiral feed hopper 91, a loading plate 92, a feed trough 97, a feeding screw rod 98 and a slag discharger 93; the feeding system includes a loading chamber 1, a gas separator 13, a push blower 14, a feed box 15, a conveyor belt, a feed platform 17, a baffle plate 18 and a positioning plate 19, and the pyrolysis gasification chamber 2 is provided with a one-way grate 20, a discharge port 21, a front baffle 22, a rear baffle 23, a slag discharge bin 24 and an air inlet 25. The pyrolysis gasification chamber 2 and the high-temperature cracking chamber 3 are connected through a primary air outlet 27. The high-temperature cracking chamber 3 is divided into two spaces, a left chamber and a right chamber. The left chamber is provided with The combustion-supporting agent inlet 30, the exhaust port 31 and the dust exhaust port 32 are arranged in the right chamber, the dust exhaust port 32, the air inlet 38 and the additive adding port 39 are arranged, and the left chamber and the right chamber are connected through the secondary air port 29; the high-temperature cracking chamber 3 and the high-pressure steam room 4 are connected through the first air duct 40, the low-pressure steam room 5 and the hot water room 6 are connected through the second air duct 99, the hot water room 6 and the cyclone dust collector 7 are connected through the first exhaust pipe 101, the cyclone dust collector 7 and the spray denitrification and denitrification chamber 8 are connected through the connecting pipe 48, the spray denitrification and denitrification chamber 8 and the water bath purification chamber 9 are connected through the second exhaust pipe 102, and the water bath purification chamber 9 is connected through the second exhaust pipe 103. 9 is connected to the electrostatic precipitator 10 through the third smoke exhaust pipe 41, and the electrostatic precipitator 10 and the gas collector 12 are connected through the tail gas collection pipe 57; the tail gas collection pipe 57 is provided with a tail gas monitoring box 11, the gas collector 12 is connected to the high temperature cracking chamber 3 and the return fan 28 through the tail gas return pipe 59, and the return fan 28 is connected to the air inlet 25 of the pyrolysis gasification chamber 2 through the air inlet pipe 26; the carbonization chamber 65 includes a biomass gas discharge port 72, a hot air inlet 73, a heat collecting plate 74, a collection pit 75, a carbonization plate 76, a roller 84, a push-pull plate 85, a driver 86 and a cooling gas inlet 87;The feeding system 66 includes a feeding table 77, a feeding bucket 78, a feeding platform 79, a feeding belt 80, a feeding bucket 81, a pushing system 82 and a reel 83. The metal recovery pyrolysis chamber 90 includes a hot air inlet 73, a push-pull plate 85, a driver 86, a gas outlet 94, a two-way grate 95 and a receiving trough 96. The hot air in the high-temperature cracking chamber 3 enters the carbonization chamber 65 and the metal recovery pyrolysis chamber 90 through the hot air pipe 68 and the hot air inlet 73. The combustible gas generated in the carbonization chamber 65 passes through the hot air pipe 68 and the hot air inlet 73. The biomass gas enters the pyrolysis gasification chamber 2 through the biomass gas outlet 72 and the biomass gas return pipe 71, and the combustible gas generated by the metal recovery pyrolysis chamber 90 enters the pyrolysis gasification chamber 2 through the gas outlet 94 and the biomass gas return pipe 71; the device completes the thermal energy conversion of textile waste through the pyrolysis gasification chamber 2, the high-temperature cracking chamber 3, the high-pressure steam room 4, the low-pressure steam room 5 and the hot water room 6, completes the sunflower straw carbonization process through the carbonization chamber 65, and completes the separation of aluminum metal waste through the metal recovery pyrolysis chamber 90. ;

[0135] The textile waste enters the pyrolysis gasification chamber 2 through the feeding system. The pyrolysis gas generated enters the high-temperature cracking chamber 3 through the primary air outlet 27, and then enters the high-pressure steam room 4, the low-pressure steam room 5, the hot water room 6 and the cyclone dust collector 7 in turn after completing the internal circulation of the system through the secondary air outlet 29. The hot water room 6 regularly supplies the low-pressure steam room 5 through the hot water return pipe 62; under the action of the induced draft fan 47, the exhaust gas enters the spray denitrification and denitration chamber 8 through the exhaust pipe 44 and the connecting pipe 48 of the cyclone dust collector 7, and after the dust is reduced by the spray of the nozzle 50, it enters the desulfurization room 54 through the desulfurization inlet 53, and then enters the denitration room 56 through the denitration inlet 55. The gas after desulfurization and denitration passes through the water bath purification chamber 9 and the electrostatic precipitator 10 in turn, and then enters the gas collector 12 through the tail gas collection pipe 57 to collect carbon dioxide, and a part of the remaining tail gas passes through the tail gas return pipe 5 9 enters the pyrolysis gasification chamber 2, and the remaining gas enters the carbonization chamber 65 where the carbonization operation is completed through the tail gas cooling and utilization pipe 63 or is discharged through the tail gas discharge port 60, and the tail gas discharge port 60 is located as a three-way pipe; after the carbonization of the sunflower straw in the carbonization chamber 65 is completed, the tail gas cooling and utilization control valve 64 connected to the tail gas cooling and utilization pipe 63 of the carbonization chamber 65 is opened, and the tail gas discharge control valve 61 and the gas reflux valve 58 are closed at the same time, and the tail gas cooling and utilization control valve 64 is closed after the temperature in the carbonization chamber 65 is lower than 200°C, and the tail gas discharge control valve 61 and the gas reflux valve 58 are opened at the same time to complete the cooling of the carbonization chamber 65; when the carbonization chamber 65 is cooled, the push-pull plate 85 and the driver 86 are opened, and the roller 84 drives the carbonization plate 76 to transport the carbonized sunflower straw biochar material to the aggregate pit 75, and then the carbon discharger 67 is opened to complete the slag removal.

[0136] The gas separator 13 is used to separate nitrogen from the air. The feed box 15 of the feed system conveys the textile waste to the loading chamber 1 through the first conveyor belt 16, and then transports the textile waste to the feeding platform 17 through the second conveyor belt 110 inside the loading chamber 1, and blows the textile waste into the one-way grate 20 of the pyrolysis gasification chamber 2 through the push blower 14; the textile waste in the pyrolysis gasification chamber 2 is pyrolyzed at 300-500°C, and the generated combustible gas enters the high-temperature cracking chamber 3 through the primary air outlet 27 and is pyrolyzed at 850-950°C for 3.5 seconds. During the high-temperature cracking process, the left chamber is added with an oxidant through the oxidant inlet 30, and the right chamber is added with a biomass additive through the additive inlet 39; the first air duct 40 between the high-temperature cracking chamber 3 and the high-pressure steam room 4 is added with a biomass additive through the additive inlet 39.

[0137] The bottom of the left chamber of the high-temperature cracking chamber 3 is cleaned every 3 hours through a dust removal fan 33, and the dust cover 34 is connected by a spring and is opened only when cleaning to discharge the dust into a dust storage pit 35; the bottom of the right chamber is cleaned every 18 hours through a dust discharge port 32, and the ash is discharged into a dust storage tank 36; the high-pressure steam room 4, the low-pressure steam room 5 and the hot water room 6 are cleaned every 3.5 days; the cyclone dust collector 7 includes a cyclone dust removal chamber 42 and an ash collection chamber 43, the exhaust pipe 44 in the cyclone dust removal chamber 42 is large at the top and small at the bottom, and the dust falls into the ash collection chamber 43 through the dust removal hole 46, and the dust removal plate 45 is above the dust removal hole 46; the desulfurization room 54 uses activated carbon material, and the denitrification room 56 uses a mixture of activated carbon and iron oxide; probes for different monitoring gases are arranged in the exhaust gas monitoring box 11, and data are collected once every 100 minutes, and the gas collector 12 collects carbon dioxide.

[0138] The outer sides of the pyrolysis gasification chamber 2 and the high-temperature cracking chamber 3 are steel plates, and four layers of high-temperature resistant insulation layers are arranged from the outside to the inside, namely, refractory wool, refractory bricks, refractory cement and refractory coating; the combustion aid added to the combustion aid inlet 30 is a gas containing more than 95% oxygen, and the additive added to the additive inlet 39 is a mixture of modified biochar, diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, sandstone, volcanic rock, activated carbon and river sand, and the mixing ratio is 1:0.05:0.19:0.16:0.04:0.07:0.06:0.09:0.38:0.09; The modified biochar is a mixture of iron oxide modified biochar and potassium permanganate modified biochar, with a mixing ratio of 1:0.42 and a particle size of 0.5-2mm; the particle sizes of the diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, sandstone, volcanic rock, activated carbon and river sand are 0.1-1.0mm, 0.01-0.1mm, 0.25-2.0mm, 0.25-1.0mm, 0.1-1.0mm, 0.25-5.0mm, 0.5-2.0mm, 0.1-2.0mm and 0.1-1.0mm respectively, and the activated carbon is coal-based activated carbon.

[0139] The hot air inlet 73 of the carbonization chamber 65 is arranged at a spacing of 0.8m and is inclined at an angle of 8 degrees toward the feed port of the carbonization chamber 65; the heat collecting plate 74 is arranged in an arch shape, and the outlet distance from the feed side is 0.3 times the length of the space in the carbonization chamber 65; the biomass gas outlet 72 is arranged in three, one is located above the outlet of the heat collecting plate 74, and the other two are located at both ends of the top of the carbonization chamber 65; the upper hopper 81 sends the processed material into the feed tipping hopper 78 through the upper platform 79 under the action of the motor through the scroll 83 at the top, The feed tipping bucket 78 is a feeding rotating eccentric type. After the material falls on the feeding table 77 below, it is sent to the carbonization plate 76 through the pushing system 82. The driver 86 is turned on. Driven by the front and rear rollers 84, the upper carbonization plate 76 is covered with agricultural and forestry biomass waste, and the driver 86 is closed at the same time; the hot air inlet control valve 88 is opened, and the hot air enters the carbonization chamber 65. After an interval of 3-8 minutes, the biomass gas control valve 89 is opened, and the combustible gas enters the pyrolysis gasification chamber 2 through the biomass gas return pipe 71; after the carbonization is completed, the tail gas is cooled, and the drive is opened. The actuator 86 pulls open the push-pull plate 85 to discharge the carbonized biochar material into the aggregate pit 75; the hot air inlet 73 of the metal recovery pyrolysis chamber 90 is set at a spacing of 0.5m and is inclined at an angle of 8 degrees in the direction of the feed inlet of the metal recovery pyrolysis chamber 90; the gas outlet 94 is set at two ends of the top of the metal recovery pyrolysis chamber 90; the metal-containing waste in the feed trough 97 is transported to the spiral feed hopper 91 through the loading plate 92, and the processed metal-containing waste is sent to the two-way grate 95 under the action of the feeding screw rod 98, and the metal-containing waste is opened. The driver 86 is used to cover the upper side of the grate with metal-containing waste, and the driver 86 is closed at the same time; the hot air intake control valve 88 is opened, and the hot air enters the metal recovery pyrolysis chamber 90 to separate the metal-containing waste. At the same time, the biomass gas control valve 89 is opened, and the combustible gas enters the pyrolysis gasification chamber 2 through the biomass gas reflux pipe 71; after the separation is completed, the hot air intake control valve 88 is closed, and the driver 86 is opened to pull open the push-pull plate 85 to discharge the separated metal-containing waste into the receiving trough 96, and the receiving trough 96 is filled with 0.85 times the capacity of water.

[0140] The carbonization chamber 65 and the metal recovery pyrolysis chamber 90 are provided with 6 pressure monitoring meters 69 and 6 temperature monitoring meters 70, the pyrolysis gasification chamber 2 is provided with 6 temperature monitoring meters 70, the left chamber and the right chamber of the high-temperature cracking chamber 3 are provided with 6 pressure monitoring meters 69 and 6 temperature monitoring meters 70, the high-pressure steam room 4 is provided with 6 pressure monitoring meters 69 and 6 temperature monitoring meters 70, the hot water room 6 is provided with 6 temperature monitoring meters 70, and the third smoke exhaust pipe 41 between the water bath purification chamber 9 and the electrostatic precipitator 10 is provided with 2 temperature monitoring meters 70.

[0141] The secondary air volume entering the pyrolysis gasification chamber 2 through the air inlet pipe 26 is 0.30 times the air volume of the push blower 14. The amount of reflux gas in the gas collector 12 and the left and right chambers of the high-temperature cracking chamber 3 is controlled by the gas reflux valve 58; the hot water in the hot water room 6 is supplied to the hot water loss in the high-pressure steam room 4 and the low-pressure steam room 5 through the hot water reflux pipe 62.

[0142] The textile waste has a moisture content of 15-25% and a calorific value of 3300-4100 kcal / kg, and the aluminum metal waste has a moisture content of less than 10%; the sunflower straw is first pressed into particles, and the particle size is 10-30 mm when prepared into biochar; the sunflower straw is prepared into biochar with a moisture content of less than 20%, and is first prepared into particles and then dried.

[0143] The flow rate of the flow regulating fan 37 is 500m 3 / h, the hot air from the left chamber of the high-temperature cracking chamber 3 is pumped to the right chamber; tap water is injected into the spray chamber 49, and the wastewater entering the wastewater collection barrel 51 through the waste liquid collection port 52 is evaporated and reused in the spray chamber 49; the exhaust port 31 in the right chamber of the high-temperature cracking chamber 3 is located on the right side, and the exhaust port 31 in the left chamber is located in the middle and on the right side, and the exhaust flow rate of the hot air discharged from the exhaust port 31 in the left chamber is 1.8 times that of the right chamber; the return air volume of the gas collector 12 is 0.24 times that of the high-temperature cracking chamber 3, and the flow rate of the air inlet pipe 26 in the pyrolysis gasification chamber 2 is 800m 3 / h; the gas separator 13 adopts membrane separation technology to remove nitrogen from the air, and the oxygen content of the separated gas is 89-96%, and enters the pyrolysis gasification chamber 2 under the action of the push blower 14; the gas collector 12 adopts a method combining upward exhaust method and activated carbon pressure swing adsorption method, firstly performing upward exhaust method to obtain carbon dioxide gas with a concentration higher than 50%, and then using activated carbon pressure swing adsorption method to obtain carbon dioxide gas with a concentration higher than 80%; the rated steam pressure of the high-pressure steam room 4 is 2.5MPa, and the steam pressure of the low-pressure steam room 5 is 1.5MPa.

[0144] The operating load of the device in this embodiment is 4.0 tons / hour, and the volume of the pyrolysis gasification chamber 2 is 35m 3 , and other matching; the experimental results show that: the thermal energy conversion rate of textile waste is as high as 85%-89%, the biochar yield of sunflower straw exceeds 32-37%, the aluminum content after purification exceeds 80-85%, the exhaust gas generation is reduced by 34-39%, the exhaust gas treatment cost is reduced by 83-87%, the cost of carbon dioxide recovery in the exhaust gas is reduced by 35-42%, and the operating efficiency is increased by 45-52%; it meets the conditions for continuous operation. The exhaust gas monitoring pollutant emission indicators are shown in Table 5. NOx, HCl, and total volatile organic compounds are all below the detection limit, the monitoring indicators show zero, and other indicators are also much lower than the national standard limits.

[0145] Table 5 List of tail gas emission indicators

[0146]

[0147]

[0148] Note: The national standard limit values ​​for total volatile organic compounds adopt the limits of other industry indicators in the "Volatile Organic Compound Emission Control Standards for Industrial Enterprises" (DB12 / 524-2020), and other indicators adopt the limits in the "Pollution Control Standards for the Incineration of Municipal Waste" (GB18485-2014).

[0149] The embodiments of the present invention disclosed above are only used to help illustrate the present invention. The embodiments do not describe all the details in detail, nor do they limit the invention to the specific implementation methods described. According to the content of this specification, many modifications and changes can be made. This specification selects and specifically describes these embodiments in order to better explain the principles and practical applications of the present invention, so that those skilled in the art can understand and use the present invention well.

Claims

1. An integrated device for organic solid waste treatment, metal recovery and carbon material preparation, characterized in that: It comprises a feeding system, a solid waste heat treatment system, a steam utilization system, a tail gas purification and recovery system, a biomass carbonization system and a metal pyrolysis recovery system. The solid waste heat treatment system comprises a pyrolysis gasification chamber (2) and a high temperature cracking chamber (3). The high temperature cracking chamber (3) is divided into a left chamber and a right chamber. The steam utilization system comprises a high pressure steam chamber (4), a low pressure steam chamber (5) and a hot water chamber (6). The tail gas purification and recovery system comprises a cyclone dust collector (7), a spray denitrification and denitrification chamber (8), a water bath purification chamber (9), an electrostatic precipitator (10) and a gas collector (12). The feeding system is connected to the feed inlet of the pyrolysis gasification chamber (2). The pyrolysis gasification chamber (2) is connected to the left chamber of the high temperature cracking chamber (3) through a primary air outlet (27). The left chamber of the high-temperature cracking chamber (3) is connected to the right chamber through a secondary air outlet (29), the right chamber of the high-temperature cracking chamber (3) is connected to the high-pressure steam room (4) through a first air outlet (40), the high-pressure steam room (4) is connected to the low-pressure steam room (5), the low-pressure steam room (5) is connected to the hot water room (6) through a second air outlet (99), the upper end of the hot water room (6) is connected to the low-pressure steam room (5) through a hot water return pipe (62), a return valve (100) is provided on the hot water return pipe (62), the hot water room (6) is connected to the cyclone dust collector (7) through a first smoke exhaust pipe (101), and the exhaust pipe (44) of the cyclone dust collector (7) is connected to the spray denitrification and denitration chamber (8) through a connecting pipe (48). The connecting pipe (48) is provided with an induced draft fan (47); the spray denitrification and denitration chamber (8) is connected to the water bath purification chamber (9) through the second smoke exhaust pipe (102); the water bath purification chamber (9) is connected to the electrostatic precipitator (10) through the third smoke exhaust pipe (41); the electrostatic precipitator (10) is connected to the gas collector (12) through the tail gas collection pipe (57); the gas collector (12) is connected to the discharge pipe (103); the discharge pipe (103) is connected to a tail gas return pipe (59) and a tail gas cooling and utilization pipe (63); the end of the discharge pipe (103) is a tail gas discharge port (60); the discharge pipe (103) is provided with a tail gas external discharge control valve (61); the tail gas return pipe (59) is connected to the high The left chamber and the right chamber of the warm cracking chamber (3) are connected to a return fan (28); the return fan (28) is connected to an air inlet (25) of the pyrolysis gasification chamber (2) via an air inlet pipe (26); the tail gas cooling and utilization pipe (63) is connected to a biomass carbonization system; a tail gas cooling and utilization control valve (64) is provided on the tail gas cooling and utilization pipe (63); hot air inlets (73) are provided in the biomass carbonization system and the metal pyrolysis recovery system; two hot air pipes (68) are connected to both sides of the first air duct (40); the two hot air pipes (68) are respectively connected to the hot air inlets (73) in the biomass carbonization system and the metal pyrolysis recovery system; and the two hot air pipes (68) are respectively provided with hot air inlet control valves (88);The biomass carbonization system is provided with a biomass gas outlet (72), and the metal pyrolysis recovery system is provided with a fuel gas outlet (94). The biomass gas outlet (72) and the fuel gas outlet (94) are respectively connected to the pyrolysis gasification chamber (2) through a biomass gas return pipe (71), and a biomass gas control valve (89) is provided on the biomass gas return pipe (71).

2. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The biomass carbonization system comprises a carbonization chamber (65), a first feeding system (66) and a carbon discharger (67). A first feed port (104) and a plurality of hot air inlets (73) are provided on the side wall of the carbonization chamber (65). The first feed port (104) and the plurality of hot air inlets (73) are arranged opposite to each other. The first feed port (104) is connected to the first feeding system (66). A plurality of biomass gas outlets (72) are provided on the top of the carbonization chamber (65). A cooling gas inlet (87) is provided on the bottom of the carbonization chamber (65). The tail gas is cooled by a pipe ( 63) is connected to the cooling gas inlet (87), a carbonization plate (76) is arranged inside the carbonization chamber (65), rollers (84) are arranged at both ends of the carbonization plate (76), the rollers (84) are connected to the driver (86), the front end of the carbonization plate (76) is close to the first feed inlet (104), and the end is close to the aggregate pit (75), a push-pull plate (85) is arranged above the aggregate pit (75), the aggregate pit (75) is connected to the carbon discharger (67), a heat collecting plate (74) is arranged above the carbonization plate (76), and the upper end of the heat collecting plate (74) is open.

3. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 2, characterized in that: The spacing between the multiple hot air inlets (73) is 0.5-1.0m, and the hot air inlet (73) is inclined at an angle of 5-10 degrees in the direction of the first feed inlet (104). The heat collecting plate (74) is an arched structure, and the distance from the opening to the first feed inlet (104) is 0.2-0.4 times the length of the space in the carbonization chamber (65). The number of the biomass gas exhaust ports (72) is three, one of which is located above the opening of the heat collecting plate (74), and the other two are located at both ends of the top of the carbonization chamber (65).

4. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 2, characterized in that: The first feeding system (66) comprises a feeding table (77), a feeding bucket (78), a feeding platform (79), a feeding belt (80), a feeding bucket (81), a pushing system (82) and a reel (83). Reels (83) are arranged on both sides of the feeding belt (80). One end of the feeding belt (80) is arranged in the feeding bucket (81), and the other end is arranged on the feeding platform (79). A feeding bucket (78) is arranged at one end of the feeding platform (79). The feeding bucket (78) is located above the feeding table (77). The feeding bucket (78) is of a feeding rotating eccentric type. A pushing system (82) is arranged in the feeding platform (79). The output end of the pushing system (82) is arranged on the feeding table (77). The feeding table (77) is connected to the first feeding port (104).

5. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The metal pyrolysis recovery system comprises a metal recovery pyrolysis chamber (90), a slag discharger (93) and a second feeding system (105); a second feed port (106) and a plurality of hot air inlets (73) are provided on the side wall of the metal recovery pyrolysis chamber (90); the second feed port (106) and the plurality of hot air inlets (73) are arranged opposite to each other; the second feed port (106) is connected to the second feeding system (105); a plurality of hot air inlets (73) are provided on the top of the metal recovery pyrolysis chamber (90); A gas outlet (94) is provided inside the metal recovery pyrolysis chamber (90), and a bidirectional grate (95) is arranged inside the metal recovery pyrolysis chamber (90), and the bidirectional grate (95) is connected to the driver (86), and the front end of the bidirectional grate (95) is close to the second feed port (106), and the rear end is close to the receiving trough (96), and a push-pull plate (85) is arranged above the receiving trough (96), and 0.55-0.85 times of the capacity of water is injected into the receiving trough (96), and the receiving trough (96) is connected to the slag discharger (93).

6. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 5, characterized in that: The spacing between the multiple hot air inlets (73) is 0.3-0.5m, and the hot air inlet (73) is inclined at an angle of 3-8 degrees in the direction of the second feed port (106). The number of the gas outlets (94) is two, and the two gas outlets (94) are located at both ends of the top of the metal recovery pyrolysis chamber (90).

7. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 5, characterized in that: The second feeding system (105) includes a spiral feeding hopper (91), a feeding plate (92), a feeding trough (97) and a feeding spiral rod (98); one end of the feeding plate (92) is arranged in the feeding trough (97), and the other end is arranged on the spiral feeding hopper (91); a feeding spiral rod (98) is arranged in the spiral feeding hopper (91), and the feeding spiral rod (98) is connected to the second feeding port (106).

8. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: A one-way grate (20) is arranged in the pyrolysis gasification chamber (2), the front end of the one-way grate (20) is close to the feeding system, and the rear end is close to the discharge port (21), a discharge bin (24) is arranged below the discharge port (21), a front baffle (22) and a rear baffle (23) are arranged above the one-way grate (20), the front baffle (22) and the rear baffle (23) are both arc-shaped structures, and the air inlet (25) is opened between the front baffle (22) and the rear baffle (23).

9. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: Two exhaust ports (31) are arranged above the left chamber of the high-temperature cracking chamber (3), and the two exhaust ports (31) of the left chamber are located in the middle and on the right side of the left chamber. One exhaust port (31) is arranged above the right chamber of the high-temperature cracking chamber (3), and the exhaust port (31) of the right chamber is located on the right side of the right chamber. The left chamber and the right chamber of the high-temperature cracking chamber (3) exhaust hot air through the exhaust ports (31), and all the exhaust ports (31) are connected to the tail gas return pipe (59) through an exhaust connection pipe, and a gas return valve (58) is arranged on the exhaust connection pipe and the tail gas return pipe (59).

10. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 9, characterized in that: The hot air flow rate discharged from the left chamber of the high-temperature cracking chamber (3) is 1.5-2.2 times that of the right chamber, and the air volume refluxed by the gas collector (12) through the tail gas reflux pipe (59) is 0.15-0.25 times the hot air volume discharged from the high-temperature cracking chamber (3).

11. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The top of the left chamber of the high-temperature cracking chamber (3) is provided with an inlet for combustion-supporting agent (30), and the first air duct (40), the top and side wall of the right chamber of the high-temperature cracking chamber (3) are provided with an additive adding port (39).

12. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 11, characterized in that: The combustion-supporting agent inlet (30) is used to add a combustion-supporting agent, wherein the combustion-supporting agent is a gas containing more than 95% oxygen or a solid fuel with a calorific value of 5000-9000 kcal / kg.

13. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 11, characterized in that: The additive inlet (39) is used to add additives, wherein the additives are a mixture of modified biochar, diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, gravel, volcanic rock, activated carbon and river sand, and the mixing ratio is 1: (0.03-0.08): (0.15-0.35): (0.10-0.25): (0.03-0.05): (0.06-0.09): (0.03-0.08): (0.05-0.12): (0.35-0.55): (0.08-0.12).

14. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 13, characterized in that: The modified biochar is a mixture of iron oxide modified biochar and potassium permanganate modified biochar, the mixing ratio is 1: (0.2-0.5), the particle size is 0.5-2mm, the particle size of the diatomaceous earth, ceramic powder, quartz sand, manganese sand, bluestone powder, sandstone, volcanic rock, activated carbon and river sand are 0.1-1.0mm, 0.01-0.1mm, 0.25-2.0mm, 0.25-1.0mm, 0.1-1.0mm, 0.25-5.0mm, 0.5-2.0mm, 0.1-2.0mm, 0.1-1.0mm, respectively, and the activated carbon is coal-based activated carbon.

15. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The bottoms of the left and right chambers of the high-temperature cracking chamber (3), the high-pressure steam chamber (4), the low-pressure steam chamber (5) and the hot water chamber (6) are all provided with dust discharge ports (32); the dust discharge port (32) at the bottom of the left chamber of the high-temperature cracking chamber (3) is connected to a dust storage pit (35) via a dust pipe (107); a dust removal fan (33) is provided on the dust pipe (107); a dust cover (34) is provided at the end of the dust pipe (107); the dust cover (34) is connected by a spring; and a dust storage tank (36) is provided below the dust discharge port (32) at the bottom of the right chamber of the high-temperature cracking chamber (3).

16. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: An air outlet (108) is provided at the lower part of the left chamber of the high-temperature cracking chamber (3), and an air inlet (38) is provided at the lower part of the right chamber of the high-temperature cracking chamber (3). The air outlet (108) and the air inlet (38) are connected via a flow regulating air duct (109), and a flow regulating fan (37) is provided on the flow regulating air duct (109).

17. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The feeding system comprises a feeding chamber (1), a gas separator (13), a push blower (14), a feeding box (15), a first conveyor belt (16) and a feeding platform (17); one end of the first conveyor belt (16) is arranged in the feeding box (15), and the other end is arranged on the feeding chamber (1); a second conveyor belt (110) is arranged in the feeding chamber (1), and the end of the second conveyor belt (110) is close to the feeding platform (17); the gas separator (13) is connected to the push blower (14); the outlet of the push blower (14) is arranged on the feeding platform (17); and the feeding platform (17) is connected to the inlet of the pyrolysis gasification chamber (2).

18. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 17, characterized in that: The gas separator (13) uses membrane separation technology to separate nitrogen from the air, and other gases in the air enter the pyrolysis gasification chamber (2) through the push blower (14).

19. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 18, characterized in that: The air volume entering the pyrolysis gasification chamber (2) through the air inlet pipe (26) is 0.15-0.35 times the air volume of the push blower (14).

20. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 17, characterized in that: A positioning plate (19) is provided above the material inlet of the pyrolysis gasification chamber (2) and the second conveyor belt (110) in the loading chamber (1), and a material blocking plate (18) is provided above the material inlet of the pyrolysis gasification chamber (2).

21. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The cyclone dust collector (7) comprises a cyclone dust chamber (42) and an ash collecting chamber (43); the exhaust pipe (44) is arranged in the cyclone dust chamber (42); the exhaust pipe (44) is a structure with a larger upper portion and a smaller lower portion; a dust removal hole (46) is arranged at the bottom of the cyclone dust chamber (42); the dust removal hole (46) is located in the ash collecting chamber (43); and a dust removal plate (45) is arranged above the dust removal hole (46).

22. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The spray denitrification and denitrification chamber (8) comprises a spray chamber (49), a desulfurization chamber (54) and a denitrification chamber (56). The spray chamber (49) is connected to a connecting pipe (48). A water tank is arranged in the spray chamber (49). A plurality of nozzles (50) are connected to the lower part of the water tank. A waste liquid collection port (52) is arranged at the bottom of the spray chamber (49). A waste water collection bucket (51) is arranged below the waste liquid collection port (52). The spray chamber (49) is connected to the desulfurization chamber (54) through a desulfurization inlet (53). The desulfurization chamber (54) is connected to the denitrification chamber (56) through a denitrification inlet (55). The denitrification chamber (56) is connected to a water bath purification chamber (9) through a second smoke exhaust pipe (102).

23. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 22, characterized in that: The desulfurization chamber (54) uses activated carbon material, and the denitrification chamber (56) uses a mixture of activated carbon and iron oxide.

24. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The exhaust gas collection pipe (57) is provided with an exhaust gas monitoring box (11), and a plurality of gas monitoring probes are provided in the exhaust gas monitoring box (11).

25. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The biomass carbonization system, the metal pyrolysis recovery system, the high-pressure steam room (4), and the left and right chambers of the high-temperature cracking chamber (3) are each provided with 2-6 pressure monitoring gauges (69) and 2-6 temperature monitoring gauges (70); the pyrolysis gasification chamber (2), the low-pressure steam room (5), and the hot water room (6) are each provided with 2-6 temperature monitoring gauges (70); and the third smoke exhaust pipe (41) is provided with 1-2 temperature monitoring gauges (70).

26. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The gas collector (12) collects carbon dioxide by combining an upward exhaust method with an activated carbon pressure swing adsorption method, and the remaining tail gas enters an exhaust pipe (103).

27. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The outer sides of the pyrolysis gasification chamber (2) and the high-temperature cracking chamber (3) are steel plates, and refractory wool, refractory bricks, refractory cement and refractory coating are arranged in sequence from the outside to the inside.

28. The integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The rated steam pressure of the high-pressure steam room (4) is 2.0-3.0 MPa, and the steam pressure of the low-pressure steam room (5) is 1.0-2.0 MPa.

29. A method for using the integrated device for organic solid waste treatment, metal recovery and carbon material preparation as claimed in claim 1, characterized in that: The organic solid waste enters the pyrolysis gasification chamber (2) through the feeding system, and the generated pyrolysis gas enters the left chamber of the high-temperature cracking chamber (3) through the primary air outlet (27), and enters the right chamber of the high-temperature cracking chamber (3) through the secondary air outlet (29). After completing the internal circulation of the solid waste heat treatment system, the gas enters the high-pressure steam room (4), the low-pressure steam room (5) and the hot water room (6) in sequence, and completes the thermal energy conversion of the organic solid waste through the solid waste heat treatment system and the steam utilization system; The solid waste heat treatment system is operated simultaneously with the biomass carbonization system and / or the metal pyrolysis recovery system. The hot air in the high-temperature cracking chamber (3) enters the biomass carbonization system and / or the metal pyrolysis recovery system through the hot air pipe (68). Agricultural and forestry biomass waste is placed in the biomass carbonization system, and the agricultural and forestry biomass waste is carbonized by the biomass carbonization system to prepare biochar or fuel charcoal. Metal waste is placed in the metal pyrolysis recovery system, and the metal waste is separated by the metal pyrolysis recovery system to achieve metal recovery. The combustible gas generated by the biomass carbonization system enters the pyrolysis gasification chamber (2) through the biomass gas outlet (72) and the biomass gas reflux pipe (71), and the combustible gas generated by the metal pyrolysis recovery system enters the pyrolysis gasification chamber (2) through the gas outlet (94) and the biomass gas reflux pipe (71). The tail gas discharged from the hot water room (6) enters the cyclone dust collector (7), and enters the spray denitrification and denitrification chamber (8) under the action of the induced draft fan (47). After the dust reduction, denitrification and denitrification treatment, the tail gas enters the water bath purification chamber (9), the electrostatic precipitator (10) and the gas collector (12) in sequence. Carbon dioxide is collected in the gas collector (12). The remaining part of the tail gas enters the pyrolysis gasification chamber (2) through the tail gas return pipe (59), and the remaining tail gas enters the biomass carbonization system that completes the carbonization operation through the tail gas cooling and utilization pipe (63) or is discharged through the discharge pipe (103).

30. The method for using the integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to claim 1, characterized in that: The organic solid waste has a moisture content of less than 25% and a calorific value of more than 2000 kcal / kg, the metal waste has a moisture content of less than 10%, and the agricultural and forestry biomass waste has a moisture content of less than 20%. It is first prepared into particles and then dried. When prepared into biochar, the particle size is 10-30 mm, and when prepared into fuel charcoal, the particle size is 20-50 mm or the columnar diameter and length are 20-80 mm and 100-300 mm respectively.

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