An integrated device for organic solid waste treatment, metal recovery and carbon material preparation and a method of using the same

Abstract

The application provides an integrated device for organic solid waste treatment, metal recovery and carbon material preparation and a use method thereof, and belongs to the field of environmental science and engineering. The problems of low heat energy utilization rate of organic solid waste, low metal-containing waste recovery rate, low carbon material yield and low quality of agricultural and forestry biomass waste 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 recovery system. The solid waste heat treatment system comprises a pyrolysis gasification chamber and a high-temperature pyrolysis chamber. The high-temperature pyrolysis chamber is divided into a left chamber and a right chamber. The steam utilization system comprises a high-pressure steam room, a low-pressure steam room and a hot water room. The tail gas purification and recovery system comprises a cyclone dust collector, a spraying denitration chamber, a water bath purification chamber, an electrostatic precipitator and a gas collection machine. The integrated device is mainly used for organic solid waste treatment, metal recovery and carbon material preparation.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of environmental science and engineering, and particularly relates to an integrated device for organic solid waste treatment, metal recovery and carbon material preparation and a use method thereof. BACKGROUND

[0002] Heat energy conversion is an important utilization form of organic solid waste, pyrolysis recovery is an important form of metal purification, and carbon material preparation is an important utilization form of agricultural and forestry organic solid waste. Due to the complex composition of organic solid waste, especially industrial solid waste, different raw material sources lead to complex composition, and it is difficult to achieve full combustion by traditional methods, resulting in low heat energy conversion rate, and further leading to the generation of a large amount of complex gas, and high tail gas treatment cost. The traditional metal pyrolysis recovery produces a large amount of waste gas which is difficult to treat and has high cost, especially the oxidation of metal leads to low utilization rate, and the traditional method of agricultural and forestry biomass waste for preparing biochar and fuel carbon has low yield and low energy utilization rate. At present, the heat energy utilization rate of organic solid waste is low, the recovery rate of metal-containing waste is low, and the yield of carbon material prepared from agricultural and forestry biomass waste is low and the quality is not high, thus restricting the high-value utilization of organic solid waste, efficient recovery of metal and development of carbon material. Therefore, it is of great significance to develop an integrated device for high-temperature pyrolysis treatment of organic solid waste, metal recovery and carbon material preparation, to realize high-value utilization of heat energy of organic solid waste, high recovery rate of metal and high yield of carbon material.

[0003] At present, organic solid waste heat energy conversion, metal recovery and carbon material preparation are treated separately, resulting in a large amount of tail gas, high treatment cost, low heat energy utilization rate and low equipment operation efficiency. In addition, there is currently a lack of pyrolysis treatment link for the gas generated by solid waste, especially dioxin generated by plastic in organic solid waste. Due to insufficient high-temperature pyrolysis, a large amount of dioxin tail gas is generated. In addition, dioxin is resynthesized during the cooling process of the tail gas, and the resynthesis rate is high by the current cooling method, resulting in high tail gas treatment cost. The existing organic solid waste pyrolysis is not sufficient, the heat energy utilization rate is low, and the tail gas production is large and the composition is complex, thereby resulting in low resource utilization rate. Since most metal waste contains a high content of plastic, the tail gas treatment cost is high after pyrolysis recovery, and the collection of biomass gas generated by carbon material preparation is difficult, and there is a safety risk in storage. The existing metal recovery method lacks a strict oxygen-free environment, resulting in a high loss rate of metal oxidation, and the use of nitrogen and inert gases increases the cost of metal; the preparation of biochar requires a strict environment, and the conventional heating method has low efficiency and high cost. SUMMARY

[0004] Therefore, the present application aims to provide an integrated device for organic solid waste treatment, metal recovery and carbon material preparation and a use method thereof, to solve the series of problems of low heat energy utilization rate of organic solid waste, low recovery rate of metal-containing waste, low yield and low quality of carbon material prepared from agricultural and forestry biomass waste, and high tail gas purification cost.

[0005] In order to achieve the above object, the present application adopts the following technical scheme: An integrated device for organic solid waste treatment, metal recovery and carbon material preparation, comprising 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 comprising a pyrolysis gasification chamber and a high-temperature pyrolysis chamber, the high-temperature pyrolysis chamber being divided into a left chamber and a right chamber, the steam utilization system comprising a high-pressure steam room, a low-pressure steam room and a hot water room, the tail gas purification and recovery system comprising a cyclone dust collector, a spray denitration chamber, a water bath purification chamber, an electrostatic precipitator and a gas collection machine, the feeding system being connected with the feeding port of the pyrolysis gasification chamber, the pyrolysis gasification chamber being communicated with the left chamber of the high-temperature pyrolysis chamber through a primary over-fire port, the left chamber of the high-temperature pyrolysis chamber being communicated with the right chamber through a secondary over-fire port, the right chamber of the high-temperature pyrolysis chamber being connected with the high-pressure steam room through a first over-fire pipe, the high-pressure steam room being connected with the low-pressure steam room, the low-pressure steam room being connected with the hot water room through a second over-fire pipe, the upper end of the hot water room being connected with the low-pressure steam room through a hot water return pipe, a water return valve being arranged on the hot water return pipe, the hot water room being connected with the cyclone dust collector through a first flue gas discharge pipe, the exhaust pipe of the cyclone dust collector being connected with the spray denitration chamber through a connecting pipe, an induced draft fan being arranged on the connecting pipe, the spray denitration chamber being connected with the water bath purification chamber through a second flue gas discharge pipe, the water bath purification chamber being connected with the electrostatic precipitator through a third flue gas discharge pipe, the electrostatic precipitator being connected with the gas collection machine through a tail gas collection pipe, the gas collection machine being connected with a discharge pipe, the discharge pipe being connected with a tail gas return pipe and a tail gas cooling utilization pipe, the discharge pipe being provided with a tail gas exhaust control valve, the tail gas return pipe being connected with the left chamber and the right chamber of the high-temperature pyrolysis chamber and a return air fan, the return air fan being connected with the air inlet of the pyrolysis gasification chamber through an air inlet pipe, the tail gas cooling utilization pipe being connected with the biomass carbonization system, the tail gas cooling utilization pipe being provided with a tail gas cooling utilization control valve, the biomass carbonization system and the metal pyrolysis recovery system being provided with hot air inlets, two hot air pipes being connected with the two sides of the first over-fire pipe, the two hot air pipes being connected with the hot air inlets of the biomass carbonization system and the metal pyrolysis recovery system respectively, the two hot air pipes being provided with hot air inlet control valves respectively, the biomass gas discharge port being arranged in the biomass carbonization system, the fuel gas outlet being arranged in the metal pyrolysis recovery system, the biomass gas return pipe being connected with the pyrolysis gasification chamber, the biomass gas return pipe being provided with a biomass gas control valve.

[0006] Further, the biomass carbonization system comprises a carbonization chamber, a first feeding system and a carbon discharging machine, a first feeding port and a plurality of hot air inlets are arranged on the side wall of the carbonization chamber, the first feeding port and the plurality of hot air inlets are oppositely arranged, the first feeding port is connected with the first feeding system, a plurality of biomass gas outlets are arranged on the top of the carbonization chamber, a cooling gas inlet is arranged on the bottom of the carbonization chamber, the tail gas cooling utilization pipe is connected with the cooling gas inlet, a carbonization plate is arranged in the carbonization chamber, rollers are arranged at both ends of the carbonization plate, the rollers are connected with a driver, the front end of the carbonization plate is close to the first feeding port, and the tail end of the carbonization plate is close to a material collecting pit, a push-pull plate is arranged above the material collecting pit, the material collecting pit is connected with the carbon discharging machine, a heat collecting plate is arranged above the carbonization plate, and an opening is arranged at the upper end of the heat collecting plate.

[0007] Further, the interval of the plurality of hot air inlets is 0.5-1.0 m, the hot air inlets are inclined by an angle of 5-10 degrees to the direction of the first feeding port, the heat collecting plate is in an arched structure, the opening distance from the first feeding port side is 0.2-0.4 times the length of the space in the carbonization chamber, and the number of the biomass gas outlets is three, one of which is above the opening of the heat collecting plate, and the other two are at both ends of the top of the carbonization chamber.

[0008] Further, the first feeding system comprises a feeding table, a feeding hopper, a feeding platform, a feeding belt, a feeding hopper, a pushing system and a reel, the feeding belt is provided with a reel at both sides, one end of the feeding belt is arranged in the feeding hopper, and the other end is arranged on the feeding platform, the feeding platform is provided with the feeding hopper at one end, the feeding hopper is above the feeding table, the feeding hopper is in a feeding rotation eccentric form, the pushing system is arranged in the feeding platform, the output end of the pushing system is arranged on the feeding table, and the feeding table is connected with the first feeding port.

[0009] Further, the metal pyrolysis recovery system comprises a metal recovery pyrolysis chamber, a slag discharging machine and a second feeding system, a second feeding port and a plurality of hot air inlets are arranged on the side wall of the metal recovery pyrolysis chamber, the second feeding port and the plurality of hot air inlets are oppositely arranged, the second feeding port is connected with the second feeding system, a plurality of gas outlets are arranged on the top of the metal recovery pyrolysis chamber, a bidirectional grate is arranged in the metal recovery pyrolysis chamber, the bidirectional grate is connected with a driver, the front end of the bidirectional grate is close to the second feeding port, and the tail end of the bidirectional grate is close to a material collecting groove, a push-pull plate is arranged above the material collecting groove, 0.55-0.85 times the capacity of water is injected into the material collecting groove, and the material collecting groove is connected with the slag discharging machine.

[0010] Further, the interval of the plurality of hot air inlets is 0.3-0.5 m, the hot air inlets are inclined by an angle of 3-8 degrees to the direction of the second feeding port, the number of the gas outlets is two, and the two gas outlets are at both ends of the top of the metal recovery pyrolysis chamber.

[0011] Further, the second feeding system comprises a spiral feeding hopper, a feeding plate, a feeding groove and a feeding screw, one end of the feeding plate is arranged in the feeding groove, the other end is arranged on the spiral feeding hopper, the spiral feeding hopper is provided with a feeding screw, and the feeding screw is connected with the second feeding port.

[0012] Further, the pyrolysis gasification chamber is provided with a one-way grate, the front end of the one-way grate is close to the feeding system, and the tail end is close to the discharge port, a discharge bin is arranged below the discharge port, a front baffle and a rear baffle are arranged above the one-way grate, the front baffle and the rear baffle are both arc-shaped structures, and the gas inlet is arranged between the front baffle and the rear baffle.

[0013] Further, two exhaust ports are arranged above the left chamber of the high-temperature cracking chamber, the two exhaust ports of the left chamber are located in the middle and the right side of the left chamber, one 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, all the exhaust ports are connected with the tail gas reflux pipe through an exhaust connection pipeline, and gas reflux valves are arranged on the exhaust connection pipeline and the tail gas reflux pipe.

[0014] Further, the hot air flow 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 of the gas collection machine refluxed through the tail gas reflux pipe is 0.15-0.25 times the hot air volume discharged from the high-temperature cracking chamber.

[0015] Further, a combustion-supporting agent inlet is arranged on the top of the left chamber of the high-temperature cracking chamber, and additive adding ports are arranged on the top and the side wall of the right chamber of the high-temperature cracking chamber and the first air passing pipe.

[0016] Further, the combustion-supporting agent inlet adds combustion-supporting agent, and the combustion-supporting agent is a gas with oxygen content of more than 95% or a solid fuel with a calorific value of 5000-9000kcal / kg.

[0017] Further, the additive adding port adds additive, and the additive is a mixture of modified biochar, diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand, 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] Further, 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 diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand, volcanic rock, activated carbon and river sand is 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] Further, the bottom of the left chamber and the right chamber of the high-temperature cracking chamber, the high-pressure steam chamber, the low-pressure steam chamber and the hot water chamber is provided with a dust outlet, the dust outlet at the bottom of the left chamber of the high-temperature cracking chamber is connected with a dust storage pit through a dust pipeline, a dust removal fan is arranged on the dust pipeline, a dust cover is arranged at the end of the dust pipeline, the dust cover is spring-connected, and a dust storage tank is arranged below the dust outlet at the bottom of the right chamber of the high-temperature cracking chamber.

[0020] Further, the lower part of the left chamber of the high-temperature cracking chamber is provided with an air outlet, the lower part of the right chamber of the high-temperature cracking chamber is provided with an air inlet, and the air outlet and the air inlet are connected through a flow regulating air duct, and a flow regulating fan is arranged on the flow regulating air duct.

[0021] Further, the feeding system comprises a feeding chamber, a gas separator, a pushing air blower, a feeding box, a first conveying belt and a feeding platform, one end of the first conveying belt is arranged in the feeding box, the other end is arranged on the feeding chamber, a second conveying belt is arranged in the feeding chamber, the end of the second conveying belt is close to the feeding platform, the gas separator is connected with the pushing air blower, the outlet of the pushing air blower is arranged on the feeding platform, and the feeding platform is connected with the feeding inlet of the pyrolysis gasification chamber.

[0022] Further, the gas separator separates nitrogen in the air by using membrane separation technology, and other gases in the air enter the pyrolysis gasification chamber through the pushing air blower.

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

[0024] Further, the feeding inlet of the pyrolysis gasification chamber and the upper part of the second conveying belt in the feeding chamber are provided with positioning plates, and a material blocking plate is arranged above the feeding inlet of the pyrolysis gasification chamber.

[0025] Further, the cyclone dust collector comprises a cyclone dust removal chamber and a dust collecting chamber, the exhaust pipe is arranged in the cyclone dust removal chamber, the exhaust pipe has a structure of large at the top and small at the bottom, a dust falling hole is arranged at the bottom of the cyclone dust removal chamber, the dust falling hole is located in the dust collecting chamber, and a dust falling plate is arranged above the dust falling hole.

[0026] Further, the spray denitration chamber comprises a spray chamber, a desulfurization interval and a denitration interval, the spray chamber is connected with the connecting pipe, a water tank is arranged in the spray chamber, a plurality of spray heads 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 communicated with the desulfurization interval through a desulfurization inlet, the desulfurization interval is communicated with the denitration interval through a denitration inlet, and the denitration interval is connected with the water bath purification chamber through a second exhaust pipe.

[0027] Further, the desulfurization interval adopts active carbon material, and the denitration interval adopts a mixture of active carbon and iron oxide.

[0028] Further, a tail gas monitoring box is arranged on the tail gas collecting pipe, and a plurality of gas monitoring probes are arranged in the tail gas monitoring box.

[0029] Further, 2-6 pressure monitoring tables and 2-6 temperature monitoring tables are arranged on the biomass carbonization system, the metal pyrolysis recovery system, the high-pressure steam interval, the left chamber and the right chamber of the high-temperature cracking chamber, 2-6 temperature monitoring tables are arranged on the pyrolysis gasification chamber, the low-pressure steam interval and the hot water interval, and 1-2 temperature monitoring tables are arranged on the third exhaust pipe.

[0030] Further, the gas collecting machine adopts a method combining upward exhaust and active carbon pressure swing adsorption to collect carbon dioxide, and the remaining tail gas enters the exhaust pipe.

[0031] Further, the outer sides of the pyrolysis gasification chamber and the high-temperature cracking chamber are made of steel plates, and from outside to inside, fireproof cotton, fireproof bricks, fireproof cement and fireproof paint are arranged in sequence.

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

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

[0034] The organic solid waste enters the pyrolysis gasification chamber through the feeding system, the generated pyrolysis gas enters the left chamber of the high-temperature cracking chamber through the primary over-fire port, enters the right chamber of the high-temperature cracking chamber through the secondary over-fire port, and then enters the high-pressure steam room, the low-pressure steam room and the hot water room in turn after completing the internal circulation of the solid waste heat treatment system, and the organic solid waste heat energy conversion is completed through the solid waste heat treatment system and the steam utilization system.

[0035] The solid waste heat treatment system is simultaneously operated 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, the agricultural and forestry biomass waste is placed in the biomass carbonization system, the carbonization of the agricultural and forestry biomass waste is completed through the biomass carbonization system, and the biochar or fuel carbon is prepared, the metal waste is placed in the metal pyrolysis recovery system, the metal waste is separated through the metal pyrolysis recovery system, and the metal recovery is realized; the combustible gas generated by the biomass carbonization system enters the pyrolysis gasification chamber through the biomass gas exhaust port and the biomass gas return pipe, and the combustible gas generated by the metal pyrolysis recovery system enters the pyrolysis gasification chamber through the fuel gas outlet and the biomass gas return pipe;

[0036] The tail gas discharged from the hot water room enters the cyclone dust collector, enters the spray denitrification and denitrification chamber under the action of the induced draft fan, and then enters the water bath purification chamber, the electrostatic precipitator and the gas collection machine in turn after the tail gas is treated by dust removal, denitrification and denitrification, carbon dioxide is collected in the gas collection machine, a part of the remaining tail gas enters the pyrolysis gasification chamber through the tail gas return pipe, and the remaining tail gas enters the biomass carbonization system which has completed the carbonization operation through the tail gas cooling utilization pipe or is discharged through the discharge pipe.

[0037] Further, the water content of the organic solid waste is less than 25% and the calorific value is higher than 2000kcal / kg, the water content of the metal waste is less than 10%, and the water content of the agricultural and forestry biomass waste is less than 20%, which is first prepared into particles, then dried, and prepared into biochar with a particle size of 10-30mm or fuel carbon with a particle size of 20-50mm or a columnar diameter and length of 20-80mm and 100-300mm respectively.

[0038] Compared with the prior art, the present application has the beneficial effects that: the present application provides an integrated device for organic solid waste treatment, metal recovery and carbon material preparation and a use method thereof, which can realize integrated treatment of organic solid waste utilization, metal recovery and carbon material preparation, solve problems such as low heat energy utilization rate of organic solid waste, high pollutant generation rate and high metal oxidation loss rate of metal waste, low carbon yield and high waste gas yield of biochar, low carbon dioxide concentration of tail gas and difficult recovery, realize high heat energy conversion rate of organic solid waste of more than 85%, high metal content of more than 80% after purification, high carbon yield of biochar of more than 30%, and high calorific value of fuel carbon of 4200-5400kcal / kg; realize reduction of carbon dioxide recovery cost of tail gas by more than 30%, and improvement of operation efficiency by more than 40%; realize reduction of tail gas generation amount by more than 30%, and reduction of tail gas treatment cost by more than 80%; the device realizes continuous operation, high production efficiency, large output and high industrialization degree; the device has low energy consumption, consumes no energy except a small amount of electric energy, and has low cost.

[0039] The present application realizes integrated treatment of organic solid waste, metal recovery and carbon material preparation, efficient utilization of tail gas for metal recovery and carbon material preparation, and reduction of tail gas treatment cost.

[0040] The present application realizes full combustion of the system through efficient heat preservation, combustion-supporting agent addition and special structure system, completes multi-stage cracking, fully decomposes dioxin, reduces dioxin resynthesis, realizes effective removal of dioxin through special additives, and has low tail gas purification cost.

[0041] The present application realizes full combustion of organic solid waste through high-temperature multi-stage cracking, improves heat energy utilization efficiency, reduces waste gas generation, and further reduces tail gas treatment cost; improves metal waste recovery rate through full carbonization; improves carbon yield of biochar through full carbonization; can realize integrated treatment of high-efficiency heat energy utilization of organic solid waste, high-efficiency metal recovery and high-efficiency biochar preparation, has simple process, low energy consumption, small environmental impact, and high popularization and application value. BRIEF DESCRIPTION OF DRAWINGS

[0042] The accompanying drawings, which form a part of this application, are included to provide a further understanding of the application, and are incorporated in and constitute a part of this application. The embodiments illustrated in the drawings are provided to explain the present application and should not be considered limiting of the present application. In the drawings:

[0043] Figure 1 A facade sectional view structural schematic diagram of an integrated device for organic solid waste treatment, metal recovery and carbon material preparation according to the present application;

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

[0045] Figure 3 A sectional view structural schematic diagram of a biomass carbonization system according to the present application;

[0046] Figure 4 A sectional view structural schematic diagram of a metal pyrolysis recovery system according to the present application.

[0047] In the figure:

[0048] 1 - loading chamber, 2 - pyrolysis gasification chamber, 3 - high-temperature cracking chamber, 4 - high-pressure steam chamber, 5 - low-pressure steam chamber, 6 - hot water chamber, 7 - cyclone dust collector, 8 - spray denitration chamber, 9 - water bath purification chamber, 10 - electrostatic dust collector, 11 - tail gas monitoring box, 12 - gas collection machine, 13 - gas separation machine, 14 - pushing air blower, 15 - feeding box, 16 - first conveying belt, 17 - feeding platform, 18 - blocking 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 passage, 28 - backflow fan, 29 - secondary air passage, 30 - combustion-supporting agent inlet, 31 - air 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 air outlet, 39 - additive inlet, 40 - first air passage, 41 - third flue, 42 - cyclone dust removal chamber, 43 - dust collection chamber, 44 - exhaust pipe, 45 - dust fall plate, 46 - dust fall hole, 47 - induced draft fan, 48 - connecting pipe, 49 - spray chamber, 50 - spray head, 51 - waste water collection bucket, 52 - waste liquid collection port, 53 - desulfurization inlet, 54 - desulfurization chamber, 55 - denitration inlet, 56 - denitration chamber, 57 - tail gas collection pipe, 58 - tail gas backflow valve, 59 - tail gas backflow pipe, 60 - tail gas discharge port, 61 - tail gas discharge control valve, 62 - hot water backflow 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 table, 70 - temperature monitoring table, 71 - biomass gas backflow pipe, 72 - biomass gas discharge port, 73 - hot air inlet, 74 - heat collecting plate, 75 - material collecting pit, 76 - carbonization plate, 77 - feeding table, 78 - feeding hopper, 79 - feeding platform, 80 - feeding belt, 81 - feeding hopper, 82 - pushing system, 83 - reel, 84 - roller, 85 - push-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 feeding hopper, 92 - feeding plate, 93 - slag discharge machine, 94 - fuel gas outlet, 95 - two-way grate, 96 - material collecting groove, 97 - feeding groove, 98 - feeding screw rod, 99 - second air passage, 100 - backwater valve, 101 - first flue, 102 - second flue, 103 - discharge pipe, 104 - first feeding port, 105 - second feeding system, 106 - second feeding port, 107 - dust pipe, 108 - air outlet, 109 - flow-regulating air duct, 110 - second conveying belt. DETAILED DESCRIPTION

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

[0050] Embodiment 1: see Figures 1-4The application discloses an integrated device for organic solid waste treatment, metal recovery and carbon material preparation, which 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 pyrolysis chamber 3. The high-temperature pyrolysis chamber 3 is divided into a left chamber and a right chamber. The steam utilization system comprises 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 comprises a cyclone dust collector 7, a spray denitration chamber 8, a water bath purification chamber 9, an electrostatic dust collector 10 and a gas collecting machine 12. The feeding system is connected with a feeding inlet of the pyrolysis gasification chamber 2. The pyrolysis gasification chamber 2 is communicated with the left chamber of the high-temperature pyrolysis chamber 3 through a primary over-fire port 27. The left chamber of the high-temperature pyrolysis chamber 3 is communicated with the right chamber through a secondary over-fire port 29. The right chamber of the high-temperature pyrolysis chamber 3 is connected with the high-pressure steam room 4 through a first over-fire pipe 40. The high-pressure steam room 4 is connected with the low-pressure steam room 5. The low-pressure steam room 5 is connected with the hot water room 6 through a second over-fire pipe 99. The upper end of the hot water room 6 is connected with the low-pressure steam room 5 through a hot water return pipe 62. A water return valve 100 is arranged on the hot water return pipe 62. The hot water room 6 is connected with the cyclone dust collector 7 through a first flue gas discharging pipe 101. The exhaust pipe 44 of the cyclone dust collector 7 is connected with the spray denitration chamber 8 through a connecting pipe 48. An air induction fan 47 is arranged on the connecting pipe 48. The spray denitration chamber 8 is connected with the water bath purification chamber 9 through a second flue gas discharging pipe 102. The water bath purification chamber 9 is connected with the electrostatic dust collector 10 through a third flue gas discharging pipe 41. The electrostatic dust collector 10 is connected with the gas collecting machine 12 through a tail gas collecting pipe 57. The gas collecting machine 12 is connected with a discharging pipe 103. The discharging pipe 103 is connected with a tail gas return pipe 59 and a tail gas cooling utilization pipe 63. The tail gas discharging port 60 is arranged at the tail end of the discharging pipe 103. A tail gas external discharging control valve 61 is arranged on the discharging pipe 103. The tail gas return pipe 59 is connected with the left chamber and the right chamber of the high-temperature pyrolysis chamber 3 and a return air fan 28. The return air fan 28 is connected with the air inlet 25 of the pyrolysis gasification chamber 2 through an air inlet pipe 26. The tail gas cooling utilization pipe 63 is connected with the biomass carbonization system. A tail gas cooling utilization control valve 64 is arranged on the tail gas cooling utilization pipe 63. Hot air inlets 73 are arranged in the biomass carbonization system and the metal pyrolysis recovery system. Two hot air pipes 68 are connected with the two hot air inlets 73 respectively. The two hot air pipes 68 are connected with the hot air inlets 73 of the biomass carbonization system and the metal pyrolysis recovery system respectively. Hot air inlet control valves 88 are arranged on the two hot air pipes 68 respectively. A biomass gas discharging port 72 is arranged in the biomass carbonization system. A fuel gas outlet 94 is arranged in the metal pyrolysis recovery system. The biomass gas discharging port 72 and the fuel gas outlet 94 are connected with the pyrolysis gasification chamber 2 through a biomass gas return pipe 71 respectively. A biomass gas control valve 89 is arranged on the biomass gas return pipe 71.

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

[0052] The organic solid waste enters the pyrolysis gasification chamber 2 through the feeding system, the generated pyrolysis gas enters the left chamber of the high-temperature cracking chamber 3 through the primary over-fire port 27, enters the right chamber of the high-temperature cracking chamber 3 through the secondary over-fire port 29, and then enters the high-pressure steam chamber 4, the low-pressure steam chamber 5 and the hot water chamber 6 in turn after completing the internal circulation of the solid waste heat treatment system, and the organic solid waste heat energy conversion is completed through the solid waste heat treatment system and the steam utilization system.

[0053] The solid waste heat treatment system is simultaneously operated 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, the agricultural and forestry biomass waste is placed in the biomass carbonization system, the carbonization of the agricultural and forestry biomass waste is completed through the biomass carbonization system, and the biochar or fuel carbon is prepared, the metal waste is placed in the metal pyrolysis recovery system, the metal waste is separated through the metal pyrolysis recovery system, and the metal recovery is realized; the combustible gas generated by the biomass carbonization system enters the pyrolysis gasification chamber 2 through the biomass gas exhaust port 72 and the biomass gas return pipe 71, and the combustible gas generated by the metal pyrolysis recovery system enters the pyrolysis gasification chamber 2 through the fuel gas outlet 94 and the biomass gas return pipe 71.

[0054] The tail gas discharged from the hot water chamber 6 enters the cyclone dust collector 7, and enters the spray denitration chamber 8 under the action of the induced draft fan 47, and then enters the water bath purification chamber 9, the electrostatic precipitator 10 and the gas collection machine 12 in turn after the tail gas is treated by dust removal, denitrification and denitration, carbon dioxide is collected in the gas collection machine 12, a part of the remaining 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 which has completed the carbonization operation through the tail gas cooling utilization pipe 63 or is discharged through the discharge pipe 103.

[0055] The embodiment is specifically described as follows:

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

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

[0058] Two exhaust ports 31 are arranged above the left chamber of the high-temperature pyrolysis chamber 3, the two exhaust ports 31 of the left chamber are located in the middle and the right side of the left chamber, one exhaust port 31 is arranged above the right chamber of the high-temperature pyrolysis chamber 3, 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 pyrolysis chamber 3 exhaust hot air through the exhaust port 31, all the exhaust ports 31 are connected with the tail gas backflow pipe 59 through the exhaust connection pipeline, the exhaust connection pipeline and the tail gas backflow pipe 59 are both provided with a gas backflow valve 58, the amount of backflow gas in the gas collection machine 12, the left chamber and the right chamber of the high-temperature pyrolysis chamber 3 is controlled through the gas backflow valve 58. The hot air flow of the left chamber of the high-temperature pyrolysis chamber 3 is 1.5-2.2 times that of the right chamber, and the air volume backflowed by the gas collection machine 12 through the tail gas backflow pipe 59 is 0.15-0.25 times the hot air volume discharged from the high-temperature pyrolysis chamber 3.

[0059] The high-temperature pyrolysis chamber 3 is provided with an auxiliary fuel inlet 30 at the top of the left chamber, the first overwind pipe 40, the top of the right chamber of the high-temperature pyrolysis chamber 3 and the sidewall are all provided with an additive adding port 39. The auxiliary fuel inlet 30 adds auxiliary fuel, the auxiliary fuel is a gas containing more than 95% oxygen or a solid fuel with a calorific value of 5000-9000 kcal / kg. The additive adding port 39 adds additives, the additives are a mixture of modified biochar, diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand, 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, and the mixing ratio is 1:(0.2-0.5), and the particle size is 0.5-2 mm. The particle sizes of diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand, volcanic rock, activated carbon and river sand are 0.1-1.0 mm, 0.01-0.1 mm, 0.25-2.0 mm, 0.25-1.0 mm, 0.1-1.0 mm, 0.25-5.0 mm, 0.5-2.0 mm, 0.1-2.0 mm, 0.1-1.0 mm, respectively. The activated carbon is coal-based activated carbon.

[0060] The bottom of the left chamber and the right chamber 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 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 with a dust storage pit 35 through a dust pipeline 107, a dust removal fan 33 is arranged on the dust pipeline 107, a dust cover 34 is arranged at the end of the dust pipeline 107, the dust cover 34 is spring-connected, and a dust storage tank 36 is arranged below the dust discharge port 32 at the bottom of the right chamber of the high-temperature cracking chamber 3.

[0061] The lower part of the left chamber of the high-temperature cracking chamber 3 is provided with an air outlet port 108, the lower part of the right chamber of the high-temperature cracking chamber 3 is provided with an air inlet port 38, the air outlet port 108 and the air inlet port 38 are connected through a flow regulating air duct 109, a flow regulating fan 37 is arranged on the flow regulating air duct 109, and the flow regulating fan 37 exhausts the hot air in the left chamber of the high-temperature cracking chamber 3 to the right chamber.

[0062] The feeding system comprises a feeding chamber 1, a gas separator 13, a pushing air blower 14, a feeding box 15, a first conveying belt 16 and a feeding platform 17, one end of the first conveying belt 16 is arranged in the feeding box 15, the other end is arranged on the feeding chamber 1, a second conveying belt 110 is arranged in the feeding chamber 1, the end of the second conveying belt 110 is close to the feeding platform 17, the gas separator 13 is connected with the pushing air blower 14, the outlet of the pushing air blower 14 is arranged on the feeding platform 17, and the feeding platform 17 is connected with the material inlet of the pyrolysis gasification chamber 2.

[0063] The gas separator 13 separates nitrogen in air by using membrane separation technology, and other separated gases are mainly oxygen, which enters the pyrolysis gasification chamber 2 through the pushing air blower 14. The air volume entering the pyrolysis gasification chamber 2 through the air inlet pipe 26 is 0.15-0.35 times of the air volume of the pushing air blower 14. The material inlet of the pyrolysis gasification chamber 2 and the upper part of the second conveying belt 110 in the feeding chamber 1 are provided with positioning plates 19, and the material inlet of the pyrolysis gasification chamber 2 is provided with a material blocking plate 18.

[0064] The gas separator 13 separates nitrogen in the air, the feeding tank 15 of the feeding system transports the organic solid waste to the feeding chamber 1 through the first conveying belt 16, then the organic solid waste is transported to the feeding platform 17 through the second conveying belt 110 in the feeding chamber 1, and the organic waste is blown onto the one-way grate 20 in the pyrolysis gasification chamber 2 through the pushing air blower 14; the organic waste in the pyrolysis gasification chamber 2 is pyrolyzed at 300-500℃, the generated combustible gas enters the high-temperature cracking chamber 3 through the primary over-fire port 27 and is high-temperature cracked at 850-1000℃ for 3-5 seconds, and the left chamber of the high-temperature cracking chamber 3 adds combustion-supporting agent through the combustion-supporting agent inlet 30 during the high-temperature cracking process, and the right chamber adds biomass additive through the additive adding port 39; the first over-fire pipe 40 between the high-temperature cracking chamber 3 and the high-pressure steam room 4 adds biomass additive through the additive adding port 39.

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

[0066] The biomass carbonization system comprises a carbonization chamber 65, a first feeding system 66 and a carbon discharge machine 67, a first feeding port 104 and a plurality of hot air inlets 73 are formed in the side wall of the carbonization chamber 65, the first feeding port 104 and the plurality of hot air inlets 73 are oppositely arranged, the first feeding port 104 is connected with the first feeding system 66, a plurality of biomass gas discharge ports 72 are formed in the top of the carbonization chamber 65, a cooling gas inlet 87 is formed in the bottom of the carbonization chamber 65, a tail gas cooling utilization pipe 63 is connected with the cooling gas inlet 87, a carbonization plate 76 is arranged in the carbonization chamber 65, rollers 84 are arranged at both ends of the carbonization plate 76, the rollers 84 are connected with a driver 86, the front end of the carbonization plate 76 is close to the first feeding port 104, and the tail end is close to a material collecting pit 75, a push-pull plate 85 is arranged above the material collecting pit 75, the material collecting pit 75 is connected with the carbon discharge machine 67, a heat collecting plate 74 is arranged above the carbonization plate 76, and an opening is formed in the upper end of the heat collecting plate 74.

[0067] The distance between the plurality of hot air inlets 73 is 0.5-1.0m, the hot air inlets 73 are inclined by an angle of 5-10 degrees to the direction of the first feeding port 104, the heat collecting plate 74 is in an arched structure, the opening distance from the side of the first feeding port 104 is 0.2-0.4 times the length of the space in the carbonization chamber 65, and the number of the biomass gas discharge 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.

[0068] The first feeding system 66 comprises a feeding table 77, a feeding hopper 78, a feeding platform 79, a feeding belt 80, a feeding hopper 81, a pushing system 82 and a reel 83, the feeding belt 80 is provided with a reel 83 on both sides, one end of the feeding belt 80 is arranged in the feeding hopper 81, the other end is arranged on the feeding platform 79, one end of the feeding platform 79 is provided with the feeding hopper 78, the feeding hopper 78 is above the feeding table 77, the feeding hopper 78 is in the form of a feeding rotating eccentric, the 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, and the feeding table 77 is connected with the first feeding port 104.

[0069] The feeding hopper 81 sends the processed material to the feeding hopper 78 through the reel 83 at the top under the action of the motor, the feeding hopper 78 is in the form of a feeding rotating eccentric, the material falls to the feeding table 77 below and is sent to the carbonization plate 76 through the pushing system 82, the drive 86 is opened, and the carbonization plate 76 is fully laid with the agricultural and forestry biomass waste on the upper side under the driving of the front and rear rollers 84, and the drive 86 is closed.

[0070] The hot air inlet control valve 88 is opened, the hot air enters the carbonization chamber 65, the biomass gas control valve 89 is opened after 3-8 minutes, and the combustible gas enters the pyrolysis gasification chamber 2 through the biomass gas return pipe 71; after the carbonization is completed and the tail gas is cooled, the drive 86 is opened to pull the push-pull plate 85 to discharge the carbonized biomass material into the material collecting pit 75.

[0071] The metal pyrolysis recycling system comprises a metal recycling pyrolysis chamber 90, a slagging machine 93 and a second feeding system 105, the sidewall of the metal recycling pyrolysis chamber 90 is provided with a second feeding port 106 and a plurality of hot air inlets 73, the second feeding port 106 and the plurality of hot air inlets 73 are oppositely arranged, the second feeding port 106 is connected with the second feeding system 105, the top of the metal recycling pyrolysis chamber 90 is provided with a plurality of gas outlets 94, the metal recycling pyrolysis chamber 90 is internally provided with a bidirectional grate 95, the bidirectional grate 95 is connected with the drive 86, the front end of the bidirectional grate 95 is close to the second feeding port 106, and the tail end is close to a material collecting groove 96, the material collecting groove 96 is provided with a push-pull plate 85 above, the material collecting groove 96 is filled with water with a capacity of 0.55-0.85 times, and the material collecting groove 96 is connected with the slagging machine 93.

[0072] The plurality of hot air inlets 73 are spaced apart by 0.3-0.5 m, the hot air inlets 73 are inclined by an angle of 3-8 degrees to the direction of the second feeding port 106, the number of the gas outlets 94 is two, and the two gas outlets 94 are located at the two ends of the top of the metal recycling pyrolysis chamber 90.

[0073] The second feeding system 105 includes a spiral feeding hopper 91, a feeding plate 92, a feeding groove 97 and a feeding screw 98, one end of the feeding plate 92 is arranged in the feeding groove 97, the other end is arranged on the spiral feeding hopper 91, the spiral feeding hopper 91 is provided with the feeding screw 98, and the feeding screw 98 is connected with the second feeding port 106.

[0074] The metal-containing waste in the feeding groove 97 is conveyed to the spiral feeding hopper 91 through the feeding plate 92, and the metal-containing waste is sent to the bidirectional grate 95 under the action of the feeding screw 98, the driver 86 is opened, the metal-containing waste is evenly distributed on the upper side of the grate, and the driver 86 is closed at the same time; the hot air inlet control valve 88 is opened, the hot air enters the metal recovery pyrolysis chamber 90 to carbonize the metal-containing waste, and the biomass gas control valve 89 is opened at the same time, the combustible gas enters the pyrolysis gasification chamber 2 through the biomass gas return pipe 71; after the carbonization is completed, the hot air inlet control valve 88 is closed, the driver 86 is opened, and the push-pull plate 85 is pulled away to discharge the carbonized metal-containing waste into the collecting groove 96.

[0075] The hot air in the high-temperature pyrolysis 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 by the carbonization chamber 65 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.

[0076] The organic solid waste heat energy conversion is completed through the pyrolysis gasification chamber 2, the high-temperature pyrolysis chamber 3, the high-pressure steam room 4, the low-pressure steam room 5 and the hot water room 6, the carbonization process of the agricultural and forestry biomass is completed through the carbonization chamber 65, and the metal waste separation 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.

[0077] The organic solid waste enters the pyrolysis gasification chamber 2 through the feeding system, the pyrolysis gas generated is introduced into the high-temperature pyrolysis chamber 3 through the primary over-fire port 27, and after completing the internal circulation through the secondary over-fire port 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, and the hot water room 6 regularly supplements the loss of hot water in the low-pressure steam room 5 through the hot water return pipe 62.

[0078] The cyclone dust collector 7 includes a cyclone dust removal chamber 42 and a dust collecting chamber 43, the exhaust pipe 44 is arranged in the cyclone dust removal chamber 42, the exhaust pipe 44 has a large upper part and a small lower part, the bottom of the cyclone dust removal chamber 42 is provided with a dust falling hole 46, the dust falling hole 46 is located in the dust collecting chamber 43, a dust falling plate 45 is arranged above the dust falling hole 46, and dust falls into the dust collecting chamber 43 through the dust falling hole 46.

[0079] The spray denitration and denitrification chamber 8 comprises a spray chamber 49 connected with the connecting pipe 48, a desulfurization chamber 54 and a denitration chamber 56. A water tank is arranged in the spray chamber 49. A plurality of spray heads 50 are connected to the lower part of the water tank. A waste liquid collecting port 52 is arranged at the bottom of the spray chamber 49. A waste water collecting barrel 51 is arranged below the waste liquid collecting port 52. The spray chamber 49 is communicated with the desulfurization chamber 54 through a desulfurization inlet 53. The desulfurization chamber 54 is communicated with the denitration chamber 56 through a denitration inlet 55. The denitration chamber 56 is connected with the water bath purification chamber 9 through a second exhaust pipe 102. The desulfurization chamber 54 adopts activated carbon material. The denitration chamber 56 adopts a mixture of activated carbon and iron oxide. Tap water is injected into the water tank. The waste water in the waste water collecting barrel 51 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 denitration and denitrification chamber 8 through the exhaust pipe 44 of the cyclone dust collector 7 and the connecting pipe 48. After dust removal under the action of the spray head 50, the exhaust gas enters the desulfurization chamber 54 through the desulfurization inlet 53, then enters the denitration chamber 56 through the denitration inlet 55. The gas after desulfurization and denitrification successively passes through the water bath purification chamber 9 and the electrostatic precipitator 10, then enters the gas collecting machine 12 through the tail gas collecting pipe 57 to collect carbon dioxide. The remaining tail gas enters the pyrolysis gasification chamber 2 through the tail gas reflux pipe 59. The remaining gas enters the carbonization chamber 65 which has completed carbonization operation through the tail gas cooling 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 tail gas cooling utilization control valve 64 connected with the tail gas cooling 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. When the temperature in the carbonization chamber 65 is lower than 200℃, the tail gas cooling utilization control valve 64 is closed, and the tail gas discharge control valve 61 and the gas reflux valve 58 are opened 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. The carbonization plate 76 driven by the roller shaft 84 transports the carbonized agricultural and forestry biomass carbon material into the material collecting pit 75, and then the slag removal is completed by opening the carbon discharge machine 67.

[0082] A tail gas monitoring box 11 is arranged on the tail gas collecting pipe 57. A plurality of different gas monitoring probes are arranged in the tail gas monitoring box 11. Data is collected once every 20-120 minutes. 2-6 pressure monitoring tables 69 and 2-6 temperature monitoring tables 70 are arranged on the biomass carbonization system, the metal pyrolysis recovery system, the high-pressure steam chamber 4, the left chamber and the right chamber of the high-temperature pyrolysis chamber 3. 2-6 temperature monitoring tables 70 are arranged on the pyrolysis gasification chamber 2, the low-pressure steam chamber 5 and the hot water chamber 6. 1-2 temperature monitoring tables 70 are arranged on the third exhaust pipe 41.

[0083] The gas collection machine 12 adopts the method of upward exhaust and activated carbon pressure swing adsorption to collect carbon dioxide. First, the upward exhaust method is 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 pyrolysis gasification chamber 2 and the high-temperature cracking chamber 3 are made of steel plates, and four high-temperature insulation layers of fireproof cotton, fireproof bricks, fireproof cement and fireproof paint are arranged from the outside to the inside. The rated steam pressure of the high-pressure steam chamber 4 is 2.0-3.0 MPa, and the steam pressure of the low-pressure steam chamber 5 is 1.0-2.0 MPa. The device realizes the energy utilization of textile waste, traditional Chinese medicine residue and municipal sludge particles, realizes the preparation of straw biochar and branch fuel carbon, and realizes the recycling of metal zippers and aluminum metal. The device realizes an operating load of 0.5-5.0 tons / hour, realizes near-zero emission of pollutants, and has obvious advantages compared with similar devices. The tail gas monitoring pollutant emission indexes are shown in Table 1. NOx, HCl and total volatile organic compounds are all below the detection limit, the monitoring indexes are zero, and other indexes are below the national standard limit.

[0085] Table 1: Exhaust gas emission index table

[0086]

[0087] Note: The national standard limit of total volatile organic compounds adopts the other industry index limit in the “Volatile Organic Compound Emission Control Standard for Industrial Enterprises” (DB12 / 524-2020), and other indexes adopt the limit in the “Standard for Pollution Control on Incineration of Domestic Waste” (GB18485-2014).

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

[0089] As 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, the tail gas purification and recovery system includes a cyclone dust collector 7, a spray denitration chamber 8, a water bath purification chamber 9, an electrostatic precipitator 10, a tail gas monitoring box 11, and a gas collection machine 12, and the metal pyrolysis recovery system includes a metal recovery pyrolysis chamber 90, a spiral feeding hopper 91, a feeding plate 92, a feeding groove 97, a feeding screw 98, and a slagging machine 93; the feeding system includes a feeding chamber 1, a gas separator 13, a pushing air blower 14, a feeding box 15, a first conveying belt 16, a feeding platform 17, a blocking plate 18, and a positioning plate 19, 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 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 over-fire port 27, the high-temperature cracking chamber 3 is divided into a left chamber and a right chamber, the left chamber is provided with a combustion-supporting agent inlet 30, an exhaust port 31, and a dust discharge port 32, the right chamber is provided with a dust discharge port 32, an air inlet 38, and an additive inlet 39, and the left chamber and the right chamber are connected through a secondary over-fire port 29; the high-temperature cracking chamber 3 and the high-pressure steam room 4 are connected through a first over-fire pipe 40, the low-pressure steam room 5 and the hot water room 6 are connected through a second over-fire pipe 99, the hot water room 6 and the cyclone dust collector 7 are connected through a third flue gas pipe 41, the cyclone dust collector 7 and the spray denitration chamber 8 are connected through a connecting pipe 48, the spray denitration chamber 8 and the water bath purification chamber 9 are connected through a flue gas pipe, the water bath purification chamber 9 and the electrostatic precipitator 10 are connected through a second flue gas pipe 102, and the electrostatic precipitator 10 and the gas collection machine 12 are connected through a tail gas collection pipe 57. The tail gas monitoring box 11 is arranged on the tail gas collection pipe 57, the gas collection machine 12 is connected with the high-temperature cracking chamber 3 and a backflow fan 28 through a tail gas backflow pipe 59, the backflow fan 28 is connected with the air inlet 25 of the pyrolysis gasification chamber 2 through an 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 fuel gas outlet 94, a two-way grate 95, and a material collection groove 96, hot air in the high-temperature cracking chamber 3 enters the metal recovery pyrolysis chamber 90 through a hot air pipe 68 and the hot air inlet 73, combustible gas generated by the metal recovery pyrolysis chamber 90 enters the pyrolysis gasification chamber 2 through the fuel gas outlet 94 and a biomass backflow pipe 71; the solid waste heat treatment system processes textile waste, and the metal pyrolysis recovery system processes metal-containing waste, such as a zipper, into clothes.

[0090] The textile waste enters the pyrolysis gasification chamber 2 through the feeding system, and the pyrolysis gas generated is introduced into the high-temperature cracking chamber 3 through the primary over-fire port 27, and then sequentially enters the high-pressure steam chamber 4, the low-pressure steam chamber 5, the hot water chamber 6 and the cyclone dust collector 7 after completing the internal circulation through the secondary over-fire port 29; the hot water chamber 6 is regularly supplied to the low-pressure steam chamber 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 then enters the desulfurization chamber 54 through the desulfurization inlet 53 after dust setting by the spray head 50, and then enters the denitration chamber 56 through the denitration inlet 55; the gas after desulfurization and denitration sequentially passes through the water bath purification chamber 9 and the electrostatic precipitator 10, and then enters the gas collection machine 12 through the tail gas collection pipe 57 to collect carbon dioxide, and 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; the tail gas discharge port 60 is a three-way pipe.

[0091] The gas separator 13 separates nitrogen from air, the feeding tank 15 of the feeding system transports the textile waste to the feeding platform 17 through the first conveying belt 16 and the second conveying belt 110 in the feeding chamber 1, and the textile waste is blown into the one-way grate 20 of the pyrolysis gasification chamber 2 by the pushing air blower 14; the textile waste in the pyrolysis gasification chamber 2 is pyrolyzed at 300-500℃, and the generated combustible gas enters the high-temperature cracking chamber 3 through the primary over-fire port 27 and is high-temperature cracked at 850-900℃ for 3 seconds; the left chamber of the high-temperature cracking chamber 3 adds combustion-supporting agent through the combustion-supporting agent inlet 30, and the right chamber adds biomass additive through the additive adding port 39.

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

[0093] The outer side of the pyrolysis gasification chamber 2 and the high-temperature cracking chamber 3 is a steel plate, and four high-temperature insulation layers of fire-resistant cotton, fire-resistant bricks, fire-resistant cement and fire-resistant paint are sequentially arranged from the outside to the inside; the combustion-supporting agent inlet 30 adds a combustion-supporting agent which is a gas containing more than 95% of oxygen, and the adding amount is 0.2-35 m 3 / h; the additive adding port 39 adds an additive which is a mixture of modified biochar, diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand, 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, and the particle size is 0.5-2 mm; the particle sizes of the diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand, volcanic rock, activated carbon and river sand are 0.1-1.0 mm, 0.01-0.1 mm, 0.25-2.0 mm, 0.25-1.0 mm, 0.1-1.0 mm, 0.25-5.0 mm, 0.5-2.0 mm, 0.1-2.0 mm and 0.1-1.0 mm respectively, and the activated carbon is coal-based activated carbon.

[0094] The hot air inlet 73 of the metal recovery pyrolysis chamber 90 is arranged at a distance of 0.3 m and is inclined by 3 degrees to the feeding direction of the metal recovery pyrolysis chamber 90; the fuel gas outlet 94 is arranged at two ends of the top of the metal recovery pyrolysis chamber 90; the metal-containing waste in the feeding groove 97 is conveyed to the screw feeding hopper 91 through the feeding plate 92, and the metal-containing waste is sent to the bidirectional grate 95 under the action of the feeding screw rod 98, the upper side of the grate is paved with the metal-containing waste by opening the driver 86, and the driver 86 is closed at the same time; the hot air enters the metal recovery pyrolysis chamber 90 to separate the metal-containing waste by opening the hot air inlet control valve 88, and the combustible gas enters the pyrolysis gasification chamber 2 through the biomass gas return pipe 71 by opening the biomass gas control valve 89; after the separation is completed, the hot air inlet control valve 88 is closed, the driver 86 is opened to pull the push-pull plate 85 to discharge the separated metal-containing waste into the collecting groove 96, and 0.55 times the capacity of water is injected into the collecting groove 96.

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

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

[0097] The textile waste has a water content of 15-20% and a calorific value of 4000-4500 kcal / kg, and the metal waste has a water content of less than 10%; the flow of the flow-regulating blower 37 is 50 m 3 / h, and the hot air in the left chamber of the high-temperature cracking chamber 3 is exhausted into the right chamber; tap water is injected into the spraying chamber 49, and the wastewater in the spraying chamber 49 is evaporated and treated in the wastewater collection barrel 51 through the wastewater collection port 52, and then is used in the spraying chamber 49 again; 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 flow of the hot air exhausted from the exhaust port 31 in the left chamber is 1.5 times that of the right chamber; the backflow amount of the gas collector 12 is 0.15 times that of the high-temperature cracking chamber 3, and the flow of the air inlet pipe 26 in the pyrolysis gasification chamber 2 is 100 m 3 / h; the gas separator 13 uses the membrane separation technology to remove nitrogen in the air, and the oxygen content of the separated gas is 90-95%, which enters the pyrolysis gasification chamber 2 under the action of the pushing air blower 14; the gas collector 12 uses the upward exhaust method combined with the activated carbon pressure swing adsorption method, first obtains CO2 gas with a concentration higher than 50% by the upward exhaust method, and then obtains CO2 gas with a concentration higher than 80% by the activated carbon pressure swing adsorption method; the rated steam pressure of the high-pressure steam room 4 is 2.5 MPa, and the steam pressure of the low-pressure steam room 5 is 1.5 MPa.

[0098] The running load of the device in this embodiment is 0.5 tons / hour, the volume of the pyrolysis gasification chamber 2 is 4.5 m 3 , and the other parameters are the same as those of the device in the first embodiment; the experimental results show that the textile waste thermal energy conversion rate is as high as 86%-93%, the metal content after purification is 89%-92%, the device realizes a reduction of 30-35% in the amount of tail gas, a reduction of 80-85% in the tail gas treatment cost, a reduction of 30-36% in the CO2 recovery cost in the tail gas, an increase of 40-45% in the running efficiency, and meets the conditions for continuous operation. The tail gas monitoring pollutant emission indexes are shown in Table 2, and the NOx, HCl and total volatile organic compounds are all lower than the detection limit, and the monitoring indexes are zero, and the other indexes are also lower than the national standard limit.

[0099] Table 2: Tail gas emission index list

[0100]

[0101]

[0102] Note: The national standard limit of total volatile organic compounds adopts the other industry index limit in "Industrial Enterprises Volatile Organic Compounds Emission Control Standard" (DB12 / 524-2020), and other indexes adopt the limit in "Domestic Waste Incineration Pollution Control Standard" (GB18485-2014).

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

[0104] As Figure 1 , Figure 2 and Figure 3As shown, the device includes a feed system, a solid waste heat treatment system, a steam utilization system, a tail 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 pyrolysis 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 tail gas purification and recovery system includes a cyclone dust collector 7, a spray denitration chamber 8, a water bath purification chamber 9, an electrostatic precipitator 10, a tail gas monitoring box 11, and a gas collection machine 12, and the biomass carbonization system includes a feeding system 66, a carbonization chamber 65, and a carbon discharge machine 67; the feed system includes a feeding chamber 1, a gas separator 13, a pushing air blower 14, a feed tank 15, a conveying belt, a feed platform 17, a material blocking plate 18, and a positioning plate 19, 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 discharge bin 24, and an air inlet 25, the pyrolysis gasification chamber 2 and the high-temperature pyrolysis chamber 3 are connected through a primary over-fire port 27, the high-temperature pyrolysis chamber 3 is divided into two spaces of a left chamber and a right chamber, the left chamber is provided with a combustion-supporting agent inlet 30, an exhaust port 31, and a dust discharge port 32, the right chamber is provided with a dust discharge port 32, an air inlet 38, and an additive inlet 39, and the left chamber and the right chamber are connected through a secondary over-fire port 29; the high-temperature pyrolysis chamber 3 and the high-pressure steam room 4 are connected through a first over-fire pipe 40, the low-pressure steam room 5 and the hot water room 6 are connected through a second over-fire pipe 99, the hot water room 6 and the cyclone dust collector 7 are connected through a first flue gas pipe 101, the cyclone dust collector 7 and the spray denitration chamber 8 are connected through a connecting pipe 48, the spray denitration chamber 8 and the water bath purification chamber 9 are connected through a second flue gas pipe 102, the water bath purification chamber 9 and the electrostatic precipitator 10 are connected through a third flue gas pipe 41, and the electrostatic precipitator 10 and the gas collection machine 12 are connected through a tail gas collection pipe 57; the tail gas monitoring box 11 is arranged on the tail gas collection pipe 57, the gas collection machine 12 is connected with the high-temperature pyrolysis chamber 3 and a backflow blower 28 through a tail gas backflow pipe 59, the backflow blower 28 is connected with the air inlet 25 of the pyrolysis gasification chamber 2 through an 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 material collecting pit 75, a carbonization plate 76, a roller shaft 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 hopper 78, a feeding platform 79, a feeding belt 80, a feeding hopper 81, a pushing system 82, and a reel shaft 83, hot air in the high-temperature pyrolysis chamber 3 enters the carbonization chamber 65 through a hot air pipe 68 and the hot air inlet 73, combustible gas generated by the carbonization chamber 65 enters the pyrolysis gasification chamber 2 through the biomass gas discharge port 72 and a biomass gas backflow pipe 71; the solid waste heat treatment system processes traditional Chinese medicine residues, and the carbonization chamber 65 processes corn stalks.

[0105] The pyrolysis gas generated by the traditional Chinese medicine residues entering the pyrolysis gasification chamber 2 through the feeding system enters the high-temperature cracking chamber 3 through the primary over-fire port 27, and completes the internal circulation through the secondary over-fire port 29, and then enters the high-pressure steam chamber 4, the low-pressure steam chamber 5, the hot water chamber 6 and the cyclone dust collector 7 in turn; the hot water chamber 6 is regularly supplied to the low-pressure steam chamber 5 through the hot water return pipe 62; under the action of the induced draft fan 47, the exhaust gas enters the spray denitration chamber 8 through the exhaust pipe 44 and the connecting pipe 48 of the cyclone dust collector 7, and then enters the desulfurization chamber 54 through the desulfurization inlet 53 after dust removal under the action of the spray head 50, and then enters the denitration chamber 56 through the denitration inlet 55; the gas after desulfurization and denitration enters the water bath purification chamber 9 and the electrostatic precipitator 10 in turn, and then enters the gas collection machine 12 through the tail gas collection pipe 57 to collect carbon dioxide, and the remaining tail gas enters the pyrolysis gasification chamber 2 through the tail gas return pipe 59, and the remaining gas enters the carbonization chamber 65 for carbonization operation through the tail gas cooling utilization pipe 63 or is discharged through the tail gas discharge port 60; the tail gas discharge port 60 is a three-way pipe; after the corn straw in the carbonization chamber 65 is carbonized, the tail gas cooling utilization control valve 64 connected to the tail gas cooling utilization pipe 63 of the carbonization chamber 65 is opened, and the tail gas discharge control valve 61 and the gas return valve 58 are closed at the same time; when the temperature in the carbonization chamber 65 is lower than 200℃, the tail gas cooling utilization control valve 64 is closed, and the tail gas discharge control valve 61 and the gas return valve 58 are opened at the same time to cool the carbonization chamber 65; when the carbonization chamber 65 is cooled, the push-pull plate 85 and the driver 86 are opened, the carbonization plate 76 driven by the roller shaft 84 transports the carbonized corn straw biomass carbon material to the material collecting pit 75, and then the carbon discharge machine 67 is opened to complete the residue removal.

[0106] The gas separator 13 separates nitrogen from air, the feeding tank 15 of the feeding system transports the traditional Chinese medicine residues to the feeding chamber 1 through the first conveying belt 16, and then transports the traditional Chinese medicine residues to the feeding platform 17 through the second conveying belt 110 in the feeding chamber 1; the organic waste is blown into the one-way grate 20 of the pyrolysis gasification chamber 2 by the pushing air blower 14; the organic waste in the pyrolysis gasification chamber 2 is pyrolyzed at 300-500℃, and the generated combustible gas enters the high-temperature cracking chamber 3 through the primary over-fire port 27 and is high-temperature cracked at 900-1000℃ for 5 seconds; the left chamber of the high-temperature cracking chamber 3 adds combustion-supporting agent through the combustion-supporting agent inlet 30, and the right chamber adds biomass additive through the additive adding port 39.

[0107] The high-temperature cracking chamber 3 left chamber bottom is cleaned by dust removal fan 33 every 6 hours, the dust cover 34 is spring connected, only open when cleaning, and the dust is discharged into the dust storage pit 35; the right chamber bottom is cleaned every 18 hours through the dust discharge port 32, and the ash is discharged into the 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 a dust collection chamber 43, the exhaust pipe 44 in the cyclone dust removal chamber 42 is large at the top and small at the bottom, the dust falls into the dust collection chamber 43 through the dust falling hole 46, and the dust falling plate 45 is above the dust falling hole 46; the desulfurization room 54 adopts activated carbon material, and the denitration room 56 adopts a mixture of activated carbon and iron oxide; the tail gas monitoring box 11 is provided with probes for monitoring different gases, data is collected every 60 minutes, and the gas collection machine 12 collects carbon dioxide.

[0108] The pyrolysis gasification chamber 2 and the high-temperature cracking chamber 3 are externally provided with four high-temperature insulation layers of refractory cotton, refractory bricks, refractory cement and refractory paint from outside to inside; the combustion-supporting agent inlet 30 adds combustion-supporting agent, which is pine biochar powder with a heat value of 5000-7500 kcal / kg, and the adding amount is 0.2-0.45 kg / min; the additive adding port 39 adds an additive, which is a mixture of modified biochar, diatomite, ceramic powder, quartz sand, manganese sand, green stone 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, and the mixing ratio is 1:0.4, and the particle size is 0.5-2 mm; the particle sizes of diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand, volcanic rock, activated carbon and river sand are 0.1-1.0 mm, 0.01-0.1 mm, 0.25-2.0 mm, 0.25-1.0 mm, 0.1-1.0 mm, 0.25-5.0 mm, 0.5-2.0 mm, 0.1-2.0 mm and 0.1-1.0 mm 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 distance of 0.5 m and is inclined by 10 degrees to the direction of the feed inlet of the carbonization chamber 65; the heat collecting plate 74 is arranged in an arch shape, and the distance from the outlet to the feed side is 0.2 times the length of the space in the carbonization chamber 65; the biomass gas outlet 72 is arranged in three, one above the outlet of the heat collecting plate 74, and the other two are at the two ends of the top of the carbonization chamber 65; the upper hopper 81 sends the processing material to the feed hopper 78 through the upper reel 83 under the action of the motor through the upper feed platform 79, the feed hopper 78 is in the form of a feeding rotary eccentric, and the material falls onto the feed table 77 below and is sent to the carbonization plate 76 through the pushing system 82, the drive 86 is opened, and the upper carbonization plate 76 is fully covered with corn stalks under the drive of the front and rear rollers 84, and the drive 86 is closed; the hot air inlet control valve 88 is opened, the hot air enters the carbonization chamber 65, the biomass gas control valve 89 is opened after 3 minutes, the combustible gas enters the pyrolysis gasification chamber 2 through the biomass gas return pipe 71; after the carbonization is completed and the tail gas is cooled, the drive 86 is opened to pull the push-pull plate 85 to discharge the carbonized biomass material into the material collecting pit 75.

[0110] The carbonization chamber 65 is provided with two pressure monitoring tables 69 and two temperature monitoring tables 70, the pyrolysis gasification chamber 2 is provided with two temperature monitoring tables 70, the left chamber and the right chamber of the high-temperature cracking chamber 3 are each provided with two pressure monitoring tables 69 and two temperature monitoring tables 70, the high-pressure steam interval 4 is provided with two pressure monitoring tables 69 and two temperature monitoring tables 70, the hot water interval 6 is provided with two temperature monitoring tables 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 table 70.

[0111] The amount of secondary air entering the pyrolysis gasification chamber 2 through the air inlet pipe 26 is 0.35 times the amount of air of the pushing air blower 14, and the amount of return gas in the gas collection machine 12, the left chamber and the right chamber of the high-temperature cracking chamber 3 is controlled by the gas return valve 58; the hot water in the hot water interval 6 supplements the hot water loss in the high-pressure steam interval 4 and the low-pressure steam interval 5 through the hot water return pipe 62.

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

[0113] The flow of the flow regulating fan 37 is 150m 3 / h, the hot air in the left chamber of the high-temperature pyrolysis chamber 3 is exhausted to the right chamber; tap water is injected into the spraying chamber 49, and the wastewater collected through the wastewater collection port 52 is evaporated and then reused in the spraying chamber 49; the exhaust port 31 in the right chamber of the high-temperature pyrolysis 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 hot air flow rate of the exhaust port 31 in the left chamber is 2.2 times that of the right chamber; the air collection machine 12 has a return air volume of 0.25 times that of the high-temperature pyrolysis chamber 3, and the air inlet pipe 26 in the pyrolysis gasification chamber 2 has a flow rate of 300 m 3 / h; the gas separation machine 13 uses membrane separation technology to remove nitrogen in the air, and the separated gas contains 92-97% oxygen, which enters the pyrolysis gasification chamber 2 under the action of the material pushing blower 14; the gas collection machine 12 uses a combination of upward exhaust method and activated carbon pressure swing adsorption method to obtain carbon dioxide gas with a concentration higher than 50% by the upward exhaust method, and then obtains carbon dioxide gas with a concentration higher than 80% by the activated carbon pressure swing adsorption method; the rated steam pressure of the high-pressure steam room 4 is 2.0 MPa, and the steam pressure of the low-pressure steam room 5 is 1.0 MPa.

[0114] The running load of the device in this embodiment is 1.0 tons / hour, and the volume of the pyrolysis gasification chamber 2 is 8.0 m 3 , and other supporting devices; the experimental results show that the thermal energy conversion rate of the traditional Chinese medicine residue is as high as 85%-90%, the carbon yield of the biochar is 32-35%, the device reduces the amount of tail gas by 32-39%, reduces the carbon dioxide recovery cost in the tail gas by 35-45%, increases the operation efficiency by 40-49%, reduces the tail gas treatment cost by 85-92%, and realizes continuous operation. The tail gas monitoring pollutant emission indexes are shown in Table 3, and NOx, SO2, HCl, and total volatile organic compounds are all below the detection limit, and the monitoring indexes are zero, and other indexes are also below the national standard limit.

[0115] Table 3: List of tail gas emission indexes

[0116]

[0117] Note: The national standard limit of total volatile organic compounds adopts the other industry index limit in the “Volatile Organic Compound Emission Control Standard for Industrial Enterprises” (DB12 / 524-2020), and other indexes adopt the limit in the “Domestic Waste Incineration Pollution Control Standard” (GB18485-2014).

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

[0119] As Figure 1 , Figure 2 and Figure 3As shown, the device includes a feed system, a solid waste heat treatment system, a steam utilization system, a tail 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 pyrolysis 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 tail gas purification and recovery system includes a cyclone dust collector 7, a spray denitration chamber 8, a water bath purification chamber 9, an electrostatic precipitator 10, a tail gas monitoring box 11, and a gas collection machine 12. The biomass carbonization system includes a feeding system 66, a carbonization chamber 65, and a carbon discharge machine 67. The feeding system includes a feeding chamber 1, a gas separator 13, a pushing air blower 14, a feeding tank 15, a conveying belt, a feeding platform 17, a material blocking plate 18, and a positioning plate 19. 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 pyrolysis chamber 3 are connected through a primary over-fire port 27. The high-temperature pyrolysis chamber 3 is divided into a left chamber and a right chamber. The left chamber is provided with a combustion-supporting agent inlet 30, an exhaust port 31, and a dust discharge port 32. The right chamber is provided with a dust discharge port 32, an air inlet 38, and an additive inlet 39. The left chamber and the right chamber are connected through a secondary over-fire port 29. The high-temperature pyrolysis chamber 3 and the high-pressure steam room 4 are connected through a first over-fire pipe 40. The low-pressure steam room 5 and the hot water room 6 are connected through a second over-fire pipe 99. The hot water room 6 and the cyclone dust collector 7 are connected through a first flue gas pipe 101. The cyclone dust collector 7 and the spray denitration chamber 8 are connected through a connecting pipe 48. The spray denitration chamber 8 and the water bath purification chamber 9 are connected through a second flue gas pipe 102. The water bath purification chamber 9 and the electrostatic precipitator 10 are connected through a third flue gas pipe 41. The electrostatic precipitator 10 and the gas collection machine 12 are connected through a tail gas collection pipe 57. The tail gas monitoring box 11 is arranged on the tail gas collection pipe 57. The gas collection machine 12 is connected with the high-temperature pyrolysis chamber 3 and a backflow blower 28 through a tail gas backflow pipe 59. The backflow blower 28 is connected with the air inlet 25 of the pyrolysis gasification chamber 2 through an 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 material collecting pit 75, a carbonization plate 76, a roller shaft 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 hopper 78, a feeding platform 79, a feeding belt 80, a feeding hopper 81, a pushing system 82, and a reel shaft 83. Hot air in the high-temperature pyrolysis chamber 3 enters the carbonization chamber 65 through a hot air pipe 68 and the hot air inlet 73. Combustible gas generated by the carbonization chamber 65 enters the pyrolysis gasification chamber 2 through the biomass gas discharge port 72 and a biomass gas backflow pipe 71. The solid waste heat treatment system processes municipal sludge particles. The agricultural and forestry biomass waste processed by the carbonization chamber 65 is pine branches.

[0120] The city sludge particles enter the pyrolysis gasification chamber 2 through the feeding system, and the pyrolysis gas generated by the pyrolysis gasification chamber 2 enters the high-temperature cracking chamber 3 through the primary over-fire port 27, and then sequentially enters the high-pressure steam chamber 4, the low-pressure steam chamber 5, the hot water chamber 6 and the cyclone dust collector 7 after completing the internal circulation of the system; the hot water chamber 6 is regularly supplied to the low-pressure steam chamber 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 then enters the desulfurization chamber 54 through the desulfurization inlet 53 after dust removal under the action of the spray head 50, and then enters the denitration chamber 56 through the denitration inlet 55; the gas after desulfurization and denitration sequentially passes through the water bath purification chamber 9 and the electrostatic precipitator 10, and then enters the gas collection machine 12 through the tail gas collection pipe 57 to collect carbon dioxide, and the remaining tail gas enters the pyrolysis gasification chamber 2 through the tail gas return pipe 59, and the remaining gas enters the carbonization chamber 65 for carbonization operation through the tail gas cooling utilization pipe 63 or is discharged through the tail gas discharge port 60; the tail gas discharge port 60 is a three-way pipe; after the pine branch in the carbonization chamber 65 is carbonized, the tail gas cooling utilization control valve 64 connected to the tail gas cooling utilization pipe 63 of the carbonization chamber 65 is opened, and the tail gas exhaust control valve 61 and the gas return valve 58 are closed; when the temperature in the carbonization chamber 65 is lower than 200℃, the tail gas cooling utilization control valve 64 is closed, and the tail gas exhaust control valve 61 and the gas return valve 58 are opened to cool the carbonization chamber 65; when the carbonization chamber 65 is cooled, the push-pull plate 85 and the driver 86 are opened, the carbonization plate 76 driven by the roller shaft 84 transports the carbonized pine branch fuel carbon material to the material collecting pit 75, and then the carbon discharge machine 67 is opened to complete the slag removal.

[0121] The gas separation machine 13 separates nitrogen in air; the feeding tank 15 of the feeding system transports the city sludge particle material to the feeding chamber 1 through the first conveying belt 16, and then transports the city sludge particles to the feeding platform 17 through the second conveying belt 110 in the feeding chamber 1; the city sludge particles in the pyrolysis gasification chamber 2 are pyrolyzed at 300-500℃, and the generated combustible gas enters the high-temperature cracking chamber 3 through the primary over-fire port 27 and is high-temperature cracked at 850-950℃ for 4 seconds; the left chamber of the high-temperature cracking chamber 3 adds combustion-supporting agent through the combustion-supporting agent inlet 30, and the right chamber adds biomass additive through the additive adding port 39.

[0122] The high-temperature cracking chamber 3 left chamber bottom is cleaned by dust removal fan 33 every 3 hours, the dust cover 34 is spring connected, only open when cleaning, and the dust is discharged into the dust storage pit 35; the right chamber bottom is cleaned every 15 hours through the dust discharge port 32, and the ash is discharged into the 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 a dust collection chamber 43, the exhaust pipe 44 in the cyclone dust removal chamber 42 is large at the top and small at the bottom, the dust falls into the dust collection chamber 43 through the dust falling hole 46, and the dust falling plate 45 is above the dust falling hole 46; the desulfurization room 54 adopts activated carbon material, and the denitration room 56 adopts a mixture of activated carbon and iron oxide; the tail gas monitoring box 11 is provided with probes for monitoring different gases, data is collected every 120 minutes, and the gas collection machine 12 collects carbon dioxide.

[0123] The pyrolysis gasification chamber 2 and the high-temperature cracking chamber 3 are externally provided with four high-temperature insulation layers of refractory cotton, refractory bricks, refractory cement and refractory paint from outside to inside; the combustion-supporting agent inlet 30 adds combustion-supporting agent, which is coke powder with a heat value of 7000-9000 kcal / kg, and the adding amount is 0.35-0.85 kg / min; the additive adding port 39 adds additive, which is a mixture of modified biochar, diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand gravel, 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, and the mixing ratio is 1:0.5, and the particle size is 0.5-2 mm; the particle sizes of diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand gravel, volcanic rock, activated carbon and river sand are 0.1-1.0 mm, 0.01-0.1 mm, 0.25-2.0 mm, 0.25-1.0 mm, 0.1-1.0 mm, 0.25-5.0 mm, 0.5-2.0 mm, 0.1-2.0 mm and 0.1-1.0 mm 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 distance of 1.0 m and is inclined by 5 degrees to the direction of the feed inlet of the carbonization chamber 65; the heat collecting plate 74 is arranged in an arch shape, and the distance from the outlet to the feed side is 0.4 times the length of the space in the carbonization chamber 65; the biomass gas outlet 72 is arranged in three, one above the outlet of the heat collecting plate 74, and the other two are at the two ends of the top of the carbonization chamber 65; the upper hopper 81 sends the processing material to the feed hopper 78 through the top reel 83 under the action of the motor through the upper feeding platform 79, the feed hopper 78 is in the form of a feeding eccentric rotation, and the material falls onto the feeding table 77 below and is sent to the carbonization plate 76 through the pushing system 82, the drive 86 is opened, and the upper carbonization plate 76 is fully covered with agricultural and forestry biomass waste under the drive of the front and rear rollers 84, and the drive 86 is closed at the same time; the hot air inlet control valve 88 is opened, the hot air enters the carbonization chamber 65, and after 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 and the tail gas is cooled, the drive 86 is opened to pull the push-pull plate 85 to discharge the carbonized biomass material into the material collecting pit 75.

[0125] The carbonization chamber 65 is provided with four pressure monitoring tables 69 and four temperature monitoring tables 70, the pyrolysis gasification chamber 2 is provided with four temperature monitoring tables 70, the left chamber and the right chamber of the high-temperature cracking chamber 3 are each provided with four pressure monitoring tables 69 and four temperature monitoring tables 70, the high-pressure steam interval 4 is provided with four pressure monitoring tables 69 and four temperature monitoring tables 70, the hot water interval 6 is provided with four temperature monitoring tables 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 table 70.

[0126] The secondary air quantity entering the pyrolysis gasification chamber 2 through the air inlet pipe 26 is 0.25 times the air quantity of the pushing air blower 14, and the air quantity of the gas return valve 58 controls the gas collecting machine 12 and the left chamber and the right chamber of the high-temperature cracking chamber 3; the hot water in the hot water interval 6 supplements the hot water loss in the high-pressure steam interval 4 and the low-pressure steam interval 5 through the hot water return pipe 62.

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

[0128] The flow of the flow regulating fan 37 is 300 m 3 / h, the hot air in the left chamber of the high-temperature pyrolysis chamber 3 is exhausted to the right chamber; tap water is injected into the spraying chamber 49, and the wastewater in the wastewater collection barrel 51 is evaporated and then used for spraying in the spraying chamber 49; the exhaust port 31 in the right chamber of the high-temperature pyrolysis 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 flow rate of the hot air exhausted from the left chamber is 2.0 times that of the right chamber; the air collection machine 12 has a return air volume of 0.2 times that of the high-temperature pyrolysis chamber 3, and the flow rate of the air inlet pipe 26 in the pyrolysis gasification chamber 2 is 500 m 3 / h; the gas separation machine 13 uses membrane separation technology to remove nitrogen in the air, and the oxygen content of the separated gas is 95-99%, which enters the pyrolysis gasification chamber 2 under the action of the pushing air blower 14; the gas collection machine 12 uses a combination of upward exhaust method and activated carbon pressure swing adsorption method, first uses the upward exhaust method to obtain carbon dioxide gas with a concentration higher than 50%, and then uses the 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 3.0 MPa, and the steam pressure of the low-pressure steam room 5 is 1.99 MPa.

[0129] The running load of the device in this embodiment is 2.0 tons / hour, and the volume of the pyrolysis gasification chamber 2 is 18 m 3 , and other supporting devices; the experimental results show that the thermal energy conversion rate of municipal sludge particles is as high as 85%-87%, and the fuel carbon heat value is as high as 4500-5300 kcal / kg, the device reduces the amount of tail gas by 32-37%, reduces the tail gas treatment cost by 81-89%, reduces the CO2 recovery cost in the tail gas by 32-36%, and improves the operation efficiency by 43-50%, which meets the conditions of continuous operation. The tail gas monitoring pollutant emission indexes are shown in Table 4, NOx, HCl, and total volatile organic compounds are all below the detection limit, the monitoring indexes are zero, and other indexes are also much lower than the national standard limit.

[0130] Table 4: List of tail gas emission indexes

[0131]

[0132] Note: The national standard limit of total volatile organic compounds adopts the other industry index limit in the “Volatile Organic Compound Emission Control Standard for Industrial Enterprises” (DB12 / 524-2020), and other indexes adopt the limit in the “Municipal Solid Waste Incineration Pollution Control Standard” (GB18485-2014).

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

[0134] For example Figures 1 to 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, 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 pyrolysis 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 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 biomass carbonization system includes a feeding system 66, a carbonization chamber 65, and a carbon discharge machine 67. The metal pyrolysis recovery system… The system includes a metal recycling pyrolysis chamber 90, a spiral feed hopper 91, a feeding plate 92, a feed trough 97, a feed screw 98, and a slag discharger 93; the feeding system includes a feeding chamber 1, a gas separator 13, a pusher blower 14, a feed box 15, a conveyor belt, a feeding platform 17, a baffle plate 18, and a positioning plate 19. The pyrolysis gasification chamber 2 is equipped with a unidirectional 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 pyrolysis chamber 3 are connected by a primary air inlet 27. The high-temperature pyrolysis chamber 3 is divided into two spaces: a left chamber and a right chamber. The left chamber is equipped with... Combustion aid inlet 30, exhaust vent 31, and dust outlet 32; the right chamber is equipped with dust outlet 32, air inlet 38, and additive inlet 39; the left and right chambers are connected by a secondary air inlet 29; the high-temperature pyrolysis chamber 3 and the high-pressure steam chamber 4 are connected by a first air duct 40; the low-pressure steam chamber 5 and the hot water chamber 6 are connected by a second air duct 99; the hot water chamber 6 and the cyclone dust collector 7 are connected by a first exhaust pipe 101; the cyclone dust collector 7 and the spray denitrification and denitrification chamber 8 are connected by a connecting pipe 48; the spray denitrification and denitrification chamber 8 and the water bath purification chamber 9 are connected by a second exhaust pipe 102; the water bath purification chamber... 9 and electrostatic precipitator 10 are connected through the third exhaust pipe 41. Electrostatic precipitator 10 and gas collector 12 are connected through exhaust gas collection pipe 57. Exhaust gas monitoring box 11 is installed on exhaust gas collection pipe 57. Gas collector 12 is connected to high temperature pyrolysis chamber 3 and return fan 28 through exhaust gas return pipe 59. Return fan 28 is connected to air inlet 25 of pyrolysis gasification chamber 2 through air inlet pipe 26. Carbonization chamber 65 includes biomass gas outlet 72, hot air inlet 73, heat collection plate 74, collection pit 75, carbonization plate 76, roller 84, push-pull plate 85, driver 86 and cooling gas inlet 87.The feeding system 66 includes a feeding table 77, a feeding hopper 78, a feeding platform 79, a feeding belt 80, a feeding hopper 81, a pushing system 82 and a reel 83, and the metal recovery pyrolysis chamber 90 includes a hot air inlet 73, a push-pull plate 85, a driver 86, a fuel gas outlet 94, a two-way grate 95 and a material collecting groove 96, the hot air in the high-temperature pyrolysis 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 enters the pyrolysis gasification chamber 2 through the biomass gas outlet 72 and the biomass gas return pipe 71, and the combustible gas generated in the metal recovery pyrolysis chamber 90 enters the pyrolysis gasification chamber 2 through the fuel gas outlet 94 and the biomass gas return pipe 71; the device completes the textile waste heat energy conversion through the pyrolysis gasification chamber 2, the high-temperature pyrolysis chamber 3, the high-pressure steam chamber 4, the low-pressure steam chamber 5 and the hot water chamber 6, completes the sunflower straw carbonization process through the carbonization chamber 65, and completes the aluminum metal waste separation through the metal recovery pyrolysis chamber 90.

[0135] The pyrolysis gas generated by the textile waste entering the pyrolysis gasification chamber 2 through the feeding system enters the high-temperature pyrolysis chamber 3 through the primary over-fire port 27, sequentially enters the high-pressure steam chamber 4, the low-pressure steam chamber 5, the hot water chamber 6 and the cyclone dust collector 7 after completing the internal circulation through the secondary over-fire port 29, and the hot water chamber 6 regularly supplies the low-pressure steam chamber 5 through the hot water return pipe 62; under the action of the induced draft fan 47, the exhaust gas enters the spray denitration chamber 8 through the exhaust pipe 44 of the cyclone dust collector 7 and the connecting pipe 48, is dusted under the action of the spray of the spray head 50, enters the desulfurization chamber 54 through the desulfurization inlet 53, then enters the denitration chamber 56 through the denitration inlet 55, and the gas after desulfurization and denitration sequentially passes through the water bath purification chamber 9 and the electrostatic precipitator 10, then enters the gas collection machine 12 through the tail gas collecting pipe 57 to collect carbon dioxide, part of the remaining tail gas enters the pyrolysis gasification chamber 2 through the tail gas return pipe 59, and the remaining gas enters the carbonization chamber 65 completing the carbonization operation through the tail gas cooling utilization pipe 63 or is discharged outside through the tail gas discharge port 60; the tail gas discharge port 60 is a three-way pipe; after the sunflower straw carbonization in the carbonization chamber 65 is completed, the tail gas cooling utilization control valve 64 connected with the tail gas cooling utilization pipe 63 of the carbonization chamber 65 is opened, and the tail gas discharge control valve 61 and the gas return valve 58 are closed at the same time, and after the temperature in the carbonization chamber 65 is lower than 200 DEG C, the tail gas cooling utilization control valve 64 is closed, and the tail gas discharge control valve 61 and the gas return valve 58 are opened at the same time, so that the cooling of the carbonization chamber 65 is completed; after the carbonization chamber 65 is cooled, the push-pull plate 85 and the driver 86 are opened, the carbonization plate 76 driven by the roller shaft 84 transports the carbonized sunflower straw biochar material to the material collecting pit 75, and then the carbon discharge machine 67 is opened to complete the slag removal.

[0136] The gas separator 13 separates nitrogen from air, the feeding system of the feeding tank 15 transports textile waste to the feeding chamber 1 through the first conveying belt 16, then transports the textile waste to the feeding platform 17 through the second conveying belt 110 inside the feeding chamber 1, and blows the textile waste into the one-way grate 20 of the pyrolysis gasification chamber 2 through the pushing air blower 14; the textile waste in the pyrolysis gasification chamber 2 is pyrolyzed at 300-500℃, the generated combustible gas enters the high-temperature cracking chamber 3 through the primary overflue 27 and is high-temperature cracked at 850-950℃ for 3.5 seconds, the left chamber of the high-temperature cracking chamber 3 adds combustion-supporting agent through the combustion-supporting agent inlet 30, and the right chamber adds biomass additive through the additive adding port 39.

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

[0138] The outer side of the pyrolysis gasification chamber 2 and the high-temperature cracking chamber 3 is a steel plate, and four high-temperature insulation layers of fire-resistant cotton, fire-resistant bricks, fire-resistant cement and fire-resistant paint are sequentially arranged from the outside to the inside; the combustion-supporting agent inlet 30 adds a combustion-supporting agent which is a gas containing more than 95% of oxygen; the additive adding port 39 adds an additive which is a mixture of modified biochar, diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand gravel, 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, and the mixing ratio is 1:0.42, and the particle size is 0.5-2mm; the particle sizes of the diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand gravel, 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.

[0139] The hot air inlet 73 of the carbonization chamber 65 is arranged at a distance of 0.8 m and is inclined by 8 degrees to the direction of the feed inlet of the carbonization chamber 65; the heat collecting plate 74 is arranged in an arch shape, and the distance from the outlet to 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 above the outlet of the heat collecting plate 74, and the other two are at the two ends of the top of the carbonization chamber 65; the upper hopper 81 sends the processed material to the feed hopper 78 through the top reel 83 under the action of the motor through the upper feed platform 79, the feed hopper 78 is in the form of a rotating eccentric feed, and after the material falls onto the feed table 77 below, it is sent to the carbonization plate 76 through the pushing system 82, the drive 86 is opened, and the upper carbonization plate 76 is fully covered with agricultural and forestry biomass waste under the drive of the front and rear rollers 84, and the drive 86 is closed; the hot air inlet control valve 88 is opened, hot air enters the carbonization chamber 65, and after 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 and the tail gas is cooled, the drive 86 is opened to pull away the push-pull plate 85 to discharge the carbonized biomass material into the material collecting pit 75; the hot air inlet 73 of the metal recovery pyrolysis chamber 90 is arranged at a distance of 0.5 m and is inclined by 8 degrees to the direction of the feed inlet of the metal recovery pyrolysis chamber 90; the fuel gas outlet 94 is arranged in two at the two ends of the top of the metal recovery pyrolysis chamber 90; the metal-containing waste in the feed chute 97 is conveyed to the screw feed hopper 91 through the feeding plate 92, and under the action of the feed screw rod 98, the processed metal-containing waste is sent to the bidirectional grate 95, the drive 86 is opened, and the upper side of the grate is fully covered with metal-containing waste, and the drive 86 is closed; the hot air inlet control valve 88 is opened, hot air enters the metal recovery pyrolysis chamber 90 to separate the metal-containing waste, and 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 separation is completed, the hot air inlet control valve 88 is closed, the drive 86 is opened to pull away the push-pull plate 85 to discharge the separated metal-containing waste into the material collecting chute 96, and 0.85 times the capacity of water is injected into the material collecting chute 96.

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

[0141] The secondary air amount entering the pyrolysis gasification chamber 2 through the air inlet pipe 26 is 0.30 times the air amount of the material pushing blower 14, and the amount of backflowing gas in the gas collecting machine 12 and the left and right chambers of the high-temperature cracking chamber 3 is controlled by the gas backflow valve 58; the hot water in the hot water room 6 replenishes the hot water loss in the high-pressure steam room 4 and the low-pressure steam room 5 through the hot water backflow pipe 62.

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

[0143] The flow of the flow-regulating blower 37 is 500 m 3 / h, and the hot air in the left chamber of the high-temperature cracking chamber 3 is exhausted to the right chamber; tap water is injected into the spraying chamber 49, and the wastewater in the wastewater collecting barrel 51 through the wastewater collecting port 52 is reused in the spraying chamber 49 after evaporation treatment; 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 flow of the hot air exhausted from the exhaust port 31 in the left chamber is 1.8 times that of the right chamber; the backflow amount of the gas collecting machine 12 is 0.24 times that of the high-temperature cracking chamber 3, and the flow of the air inlet pipe 26 in the pyrolysis gasification chamber 2 is 800 m 3 / h; the gas separating machine 13 uses membrane separation technology to remove nitrogen in air, and the oxygen content of the separated gas is 89-96%, which enters the pyrolysis gasification chamber 2 under the action of the material pushing blower 14; the gas collecting machine 12 uses a method combining upward exhaust method and activated carbon pressure swing adsorption method, first obtains carbon dioxide gas with a concentration higher than 50% by using the upward exhaust method, and then obtains carbon dioxide gas with a concentration higher than 80% by using the activated carbon pressure swing adsorption method; the rated steam pressure of the high-pressure steam room 4 is 2.5 MPa, and the steam pressure of the low-pressure steam room 5 is 1.5 MPa.

[0144] The running load of the device in this embodiment is 4.0 tons / hour, and the volume of the pyrolysis gasification chamber 2 is 35 m 3 , and the other components are the same as those of the device in the first embodiment; the experimental results show that the textile waste thermal energy conversion rate is as high as 85%-89%, the sunflower straw biochar carbon yield is more than 32-37%, the aluminum content after purification is more than 80-85%, the tail gas production amount is reduced by 34-39%, the tail gas treatment cost is reduced by 83-87%, the carbon dioxide recovery cost in the tail gas is reduced by 35-42%, and the running efficiency is improved by 45-52%; the continuous operation condition is met. The tail gas monitoring pollutant emission indexes are shown in Table 5, and NOx, HCl and total volatile organic compounds are all lower than the detection limit, and the monitoring indexes are zero, and the other indexes are also much lower than the national standard limit.

[0145] Table 5 Exhaust emission index list

[0146]

[0147]

[0148] Note: The national standard limit of total volatile organic compounds adopts the other industry index limit in "Volatile Organic Compounds Emission Control Standard for Industrial Enterprises" (DB12 / 524-2020), and other indexes adopt the limit in "Municipal Solid Waste Incineration Pollution Control Standard" (GB18485-2014).

[0149] The above disclosed embodiments of the present application are only used to help explain the present application. The embodiments do not describe all the details, nor limit the present application to only the specific embodiments described. Many modifications and variations can be made in light of the content of the present specification. The present specification selects and specifically describes these embodiments in order to better explain the principles and practical applications of the present application, so that those skilled in the art can well understand and utilize the present application.

Claims

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

2. The integrated device for organic solid waste treatment, metal recovery and carbon material production according to claim 1, characterized in that: The biomass carbonization system comprises a carbonization chamber (65), a first feeding system (66) and a carbon discharging machine (67), a first feeding port (104) and a plurality of hot air inlets (73) are arranged on the side wall of the carbonization chamber (65), the first feeding port (104) and the plurality of hot air inlets (73) are oppositely arranged, the first feeding port (104) is connected with the first feeding system (66), a plurality of biomass gas discharge outlets (72) are arranged on the top of the carbonization chamber (65), a cooling gas inlet (87) is arranged on the bottom of the carbonization chamber (65), a tail gas cooling utilization pipe (63) is connected with the cooling gas inlet (87), a carbonization plate (76) is arranged in the carbonization chamber (65), rollers (84) are arranged at both ends of the carbonization plate (76), the rollers (84) are connected with a driver (86), the carbonization plate (76) is arranged close to the first feeding port (104) at the front end and close to a material collecting pit (75) at the tail end, a push-pull plate (85) is arranged above the material collecting pit (75), the material collecting pit (75) is connected with the carbon discharging machine (67), a heat collecting plate (74) is arranged above the carbonization plate (76), and an opening is formed in the upper end of the heat collecting plate (74).

3. The integrated device of claim 2, wherein: The distance between the plurality of hot air inlets (73) is 0.5-1.0 m, the hot air inlets (73) are inclined by an angle of 5-10 degrees to the direction of the first feeding port (104), the heat collecting plate (74) is in an arched structure, the opening distance from the side of the first feeding port (104) is 0.2-0.4 times the length of the space in the carbonization chamber (65), and the number of the biomass gas discharge outlets (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 apparatus for organic solid waste treatment, metal recovery and carbon material production according to claim 2, characterized in that: The first feeding system (66) comprises a feeding table (77), a feeding hopper (78), a feeding platform (79), a feeding belt (80), a feeding hopper (81), a pushing system (82) and a roller (83), the feeding belt (80) is provided with the roller (83) on both sides, 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), one end of the feeding platform (79) is provided with the feeding hopper (78), the feeding hopper (78) is located above the feeding table (77), the feeding hopper (78) is in a feeding rotation eccentric form, the 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), and the feeding table (77) is connected with the first feeding port (104).

5. The integrated apparatus for organic solid waste treatment, metal recovery and carbon material production according to claim 1, characterized in that: The metal pyrolysis recycling system comprises a metal recycling pyrolysis chamber (90), a slagging machine (93) and a second feeding system (105), a second feeding port (106) and a plurality of hot air inlets (73) are arranged on the side wall of the metal recycling pyrolysis chamber (90), the second feeding port (106) and the plurality of hot air inlets (73) are oppositely arranged, the second feeding port (106) is connected with the second feeding system (105), a plurality of gas outlets (94) are arranged on the top of the metal recycling pyrolysis chamber (90), a bidirectional grate (95) is arranged in the metal recycling pyrolysis chamber (90), the bidirectional grate (95) is connected with a driver (86), the front end of the bidirectional grate (95) is close to the second feeding port (106), and the tail end is close to a material collecting groove (96), a push-pull plate (85) is arranged above the material collecting groove (96), 0.55-0.85 times the capacity of water is injected into the material collecting groove (96), and the material collecting groove (96) is connected with the slagging machine (93).

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

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

8. The integrated apparatus for organic solid waste treatment, metal recovery and carbon material production of claim 1, wherein: The pyrolysis gasification chamber (2) is provided with a unidirectional grate (20), the front end of the unidirectional grate (20) is close to the feeding system, the tail end is close to a discharge port (21), the discharge port (21) is provided with a discharge bin (24) below, the unidirectional grate (20) is provided with a front baffle (22) and a rear baffle (23) above, the front baffle (22) and the rear baffle (23) are both circular arc structures, and the gas inlet (25) is arranged between the front baffle (22) and the rear baffle (23).

9. The integrated apparatus for organic solid waste treatment, metal recovery and carbon material production according to claim 1, characterized in that: Two exhaust air inlets (31) are arranged above the left chamber of the high-temperature cracking chamber (3), the two exhaust air inlets (31) of the left chamber are located at the middle and the right side of the left chamber, one exhaust air inlet (31) is arranged above the right chamber of the high-temperature cracking chamber (3), the exhaust air inlet (31) of the right chamber is located at the right side of the right chamber, the left chamber and the right chamber of the high-temperature cracking chamber (3) discharge hot air through the exhaust air inlets (31), and all the exhaust air inlets (31) are connected with a tail gas reflux pipe (59) through exhaust air connection pipelines, and the exhaust air connection pipelines and the tail gas reflux pipe (59) are both provided with gas reflux valves (58).

10. The integrated apparatus for organic solid waste treatment, metal recovery and carbon material production according to claim 9, characterized in that: The left chamber of the high-temperature pyrolysis chamber (3) discharges hot air at a flow rate of 1.5-2.2 times that of the right chamber, and the air flow rate backflowed by the gas collection machine (12) through the tail gas backflow pipe (59) is 0.15-0.25 times that of the hot air discharged by the high-temperature pyrolysis chamber (3).

11. The integrated apparatus for organic solid waste treatment, metal recovery and carbon material production according to claim 1, characterized in that: The left chamber of the high-temperature pyrolysis chamber (3) is provided with a combustion-supporting agent inlet (30) at the top, and the first over-air pipe (40), the top of the right chamber of the high-temperature pyrolysis chamber (3) and the sidewall are all provided with additive adding ports (39).

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

13. The integrated apparatus for organic solid waste treatment, metal recovery and carbon material production of claim 11, wherein: The additive adding port (39) adds additive, which is a mixture of modified biochar, diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand, volcanic rock, activated carbon and river sand, with a mixing ratio of 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 apparatus for organic solid waste treatment, metal recovery and carbon material production according to claim 13, characterized in that: The modified biochar is a mixture of iron oxide modified biochar and potassium permanganate modified biochar, with a mixing ratio of 1:(0.2-0.5), and the particle sizes are both 0.5-2 mm; the particle sizes of the diatomite, ceramic powder, quartz sand, manganese sand, green stone powder, sand, volcanic rock, activated carbon and river sand are 0.1-1.0 mm, 0.01-0.1 mm, 0.25-2.0 mm, 0.25-1.0 mm, 0.1-1.0 mm, 0.25-5.0 mm, 0.5-2.0 mm, 0.1-2.0 mm and 0.1-1.0 mm, respectively; and the activated carbon is coal-based activated carbon.

15. The integrated apparatus for organic solid waste treatment, metal recovery and carbon material production of claim 1, wherein: The bottoms of the left and right chambers of the high-temperature pyrolysis 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 pyrolysis chamber (3) is connected to a dust storage pit (35) through a dust pipe (107), a dust removal fan (33) is arranged on the dust pipe (107), a dust cover (34) is arranged at the end of the dust pipe (107), the dust cover (34) is spring-connected, and a dust storage tank (36) is arranged below the dust discharge port (32) at the bottom of the right chamber of the high-temperature pyrolysis chamber (3).

16. The integrated apparatus for organic solid waste treatment, metal recovery and carbon material production of claim 1, wherein: The left chamber of the high-temperature pyrolysis chamber (3) is provided with an air outlet (108) at the lower part, the right chamber of the high-temperature pyrolysis chamber (3) is provided with an air inlet (38) at the lower part, and the air outlet (108) and the air inlet (38) are connected through a flow-regulating air duct (109), and a flow-regulating fan (37) is arranged on the flow-regulating air duct (109).

17. The integrated apparatus for organic solid waste treatment, metal recovery, and carbon material production of claim 1, wherein: The feeding system comprises a feeding chamber (1), a gas separator (13), a pushing air blower (14), a feeding box (15), a first conveying belt (16) and a feeding platform (17), one end of the first conveying belt (16) is arranged in the feeding box (15), the other end is arranged on the feeding chamber (1), a second conveying belt (110) is arranged in the feeding chamber (1), the end of the second conveying belt (110) is close to the feeding platform (17), the gas separator (13) is connected with the pushing air blower (14), the outlet of the pushing air blower (14) is arranged on the feeding platform (17), and the feeding platform (17) is connected with the feeding inlet of the pyrolysis gasification chamber (2).

18. The integrated apparatus for organic solid waste treatment, metal recovery and carbon material production according to claim 17, characterized in that: The gas separator (13) separates nitrogen in the air by using membrane separation technology, and other gases in the air enter the pyrolysis gasification chamber (2) through the pushing air blower (14).

19. The integrated apparatus for organic solid waste treatment, metal recovery and carbon material production 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 of the air volume of the pushing air blower (14).

20. The integrated apparatus for organic solid waste treatment, metal recovery and carbon material production of claim 17, wherein: The feeding inlet of the pyrolysis gasification chamber (2) and the upper side of the second conveying belt (110) in the feeding chamber (1) are provided with positioning plates (19), and the feeding inlet of the pyrolysis gasification chamber (2) is provided with a material blocking plate (18).

21. The integrated apparatus for organic solid waste treatment, metal recovery, and carbon material production of claim 1, wherein: The cyclone dust collector (7) comprises a cyclone dust removal chamber (42) and a dust collecting chamber (43), the exhaust pipe (44) is arranged in the cyclone dust removal chamber (42), the exhaust pipe (44) has a structure of large at the top and small at the bottom, the bottom of the cyclone dust removal chamber (42) is provided with a dust falling hole (46), the dust falling hole (46) is located in the dust collecting chamber (43), and a dust falling plate (45) is arranged above the dust falling hole (46).

22. The integrated apparatus for organic solid waste treatment, metal recovery, and carbon material production of claim 1, wherein: The spray denitrification and denitration chamber (8) comprises a spray chamber (49), a desulfurization room (54) and a denitration room (56), the spray chamber (49) is connected with a connecting pipe (48), a water tank is arranged in the spray chamber (49), a plurality of spray heads (50) are connected to the lower part of the water tank, a waste liquid collecting port (52) is arranged at the bottom of the spray chamber (49), a waste water collecting barrel (51) is arranged below the waste liquid collecting port (52), the spray chamber (49) is communicated with the desulfurization room (54) through a desulfurization inlet (53), the desulfurization room (54) is communicated with the denitration room (56) through a denitration inlet (55), and the denitration room (56) is connected with the water bath purification chamber (9) through a second exhaust pipe (102).

23. The integrated apparatus for organic solid waste treatment, metal recovery and carbon material production of claim 22, wherein: The desulfurization room (54) adopts activated carbon material, and the denitration room (56) adopts a mixture of activated carbon and iron oxide.

24. The integrated apparatus for organic solid waste treatment, metal recovery, and carbon material production of claim 1, wherein: The tail gas monitoring box (11) is arranged on the tail gas collecting pipe (57), and a plurality of gas monitoring probes are arranged in the tail gas monitoring box (11).

25. The integrated apparatus for organic solid waste treatment, metal recovery, and carbon material production of claim 1, wherein: The biomass carbonization system, metal pyrolysis recovery system, high-pressure steam room (4), left chamber and right chamber of high-temperature pyrolysis chamber (3) are provided with 2-6 pressure monitoring tables (69) and 2-6 temperature monitoring tables (70), the pyrolysis gasification chamber (2), low-pressure steam room (5) and hot water room (6) are provided with 2-6 temperature monitoring tables (70), and the third exhaust pipe (41) is provided with 1-2 temperature monitoring tables (70).

26. The integrated apparatus for organic solid waste treatment, metal recovery, and carbon material production of claim 1, wherein: The gas collection machine (12) adopts the method of upward exhaust and activated carbon pressure swing adsorption to collect carbon dioxide, and the remaining tail gas enters the exhaust pipe (103).

27. The integrated apparatus for organic solid waste treatment, metal recovery, and carbon material production of claim 1, wherein: The outer side of the pyrolysis gasification chamber (2) and the high-temperature pyrolysis chamber (3) is a steel plate, and from the outside to the inside, it is provided with fireproof cotton, firebrick, fireproof cement and fireproof paint.

28. The integrated apparatus for organic solid waste treatment, metal recovery, and carbon material production of claim 1, wherein: 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.

29. A 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 enters the pyrolysis gasification chamber (2) through the feeding system, the generated pyrolysis gas enters the left chamber of the high-temperature pyrolysis chamber (3) through the primary overfire port (27), enters the right chamber of the high-temperature pyrolysis chamber (3) through the secondary overfire port (29), and then enters the high-pressure steam room (4), the low-pressure steam room (5) and the hot water room (6) in sequence to complete the internal circulation of the solid waste heat treatment system and the organic solid waste heat energy conversion through the solid waste heat treatment system and the steam utilization system; The solid waste heat treatment system is simultaneously operated with the biomass carbonization system and / or the metal pyrolysis recovery system, the hot air in the high-temperature pyrolysis chamber (3) enters the biomass carbonization system and / or the metal pyrolysis recovery system through the hot air pipe (68), the agricultural and forestry biomass waste is placed in the biomass carbonization system, the carbonization of the agricultural and forestry biomass waste is completed through the biomass carbonization system to prepare biochar or fuel carbon, the metal waste is placed in the metal pyrolysis recovery system, the metal waste is separated through the metal pyrolysis recovery system to realize metal recovery, the combustible gas generated by the biomass carbonization system enters the pyrolysis gasification chamber (2) through the biomass gas exhaust port (72) and the biomass gas return pipe (71), and the combustible gas generated by the metal pyrolysis recovery system enters the pyrolysis gasification chamber (2) through the fuel gas outlet (94) and the biomass gas return pipe (71); The tail gas discharged from the hot water room (6) enters the cyclone dust collector (7), enters the spray denitration chamber (8) under the action of the induced draft fan (47), and then enters the water bath purification chamber (9), the electrostatic precipitator (10) and the gas collection machine (12) in sequence after dust removal, denitration and denitration treatment, carbon dioxide is collected in the gas collection machine (12), a part of the remaining 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 which has completed carbonization operation through the tail gas cooling utilization pipe (63) or is discharged through the exhaust pipe (103).

30. The method of using an integrated device for organic solid waste treatment, metal recovery, and carbon material production of claim 29, wherein: The organic solid waste has a water content of 25% or less and a heat value higher than 2000kcal / kg, the metal waste has a water content of less than 10%, and the agricultural and forestry biomass waste has a water content of less than 20%. The organic solid waste, the metal waste and the agricultural and forestry biomass waste are first prepared into granules, and then dried to prepare biochar with a particle size of 10-30mm, or fuel carbon with a particle size of 20-50mm, or a columnar shape with a diameter of 20-80mm and a length of 100-300mm.

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