Organic solid waste in-situ pyrolysis and oxidation carbon-steam integrated device and method

Abstract

The invention discloses an organic solid waste in-situ pyrolysis oxidized carbon-steam integrated device and method.The device comprises a pyrolysis oxidized carbon-steam integrated furnace, and the pyrolysis oxidized carbon-steam integrated furnace is divided into a pyrolysis carbonization chamber, a pyrolysis gas oxygen control combustion chamber and a pyrolysis gas peroxidation combustion chamber; the peroxidation incineration chamber is divided into a pyrolysis gas peroxidation incineration area and a steam generation area in the vertical direction, the pyrolysis gas oxygen control combustion chamber is located above the pyrolysis carbonization chamber and communicated with the interior of the pyrolysis gas peroxidation incineration area, and the pyrolysis carbonization chamber is divided into a pyrolysis area, an air activation area and a steam activation area in the material conveying direction; the pyrolysis gas oxygen control combustion chamber receives pyrolysis gas for oxygen control combustion, heat generated by combustion is radiated to the pyrolysis carbonization chamber to provide energy for pyrolysis activation in situ, the pyrolysis gas which is not completely combusted is subjected to peroxidation incineration in the pyrolysis gas peroxidation incineration area to obtain smoke, and heat carried by the smoke generates steam in the steam generation area and is supplied to the steam activation area. Equipment can be reduced, and the heat utilization rate is increased.

Description

Technical Field

[0001] The invention belongs to the technical field of organic solid waste resource treatment, and in particular relates to an organic solid waste in-situ pyrolysis oxidation carbon-steam integrated device and method. Background Art

[0002] In a typical traditional pyrolysis process, agricultural and forestry waste is pyrolyzed in an externally heated rotary pyrolysis furnace. The combustible components produced are not burned directly in the furnace, but are led out to a condenser or other separation device outside the furnace to achieve gas-liquid separation of combustible gas and tar. The combustible gas is burned in a hot air furnace to produce high-temperature flue gas that is introduced into the rotary pyrolysis furnace for pyrolysis. In the process of pyrolysis oil / gas being led out of the furnace for separation, due to factors such as the length of the transportation distance, external temperature changes, internal gas components, and pressure changes, some tar often condenses prematurely and adheres to the inner wall of the pipeline or inside the separation device, making it impossible to achieve complete separation.

[0003] At the same time, if steam activation is introduced into the traditional pyrolysis process, a total of five devices are required, including a rotary pyrolysis furnace, a condensation separator, a combustible gas combustion furnace, a steam boiler and an activation furnace. Whether it is the floor space, equipment cost or even process operation, it brings a burden to practical application.

[0004] Furthermore, the conventional waste heat utilization mode in the prior art is to transport the high-temperature flue gas to the steam boiler through the flue, that is, the heat source and the steam boiler are separated in two places, which also leads to the problem of increased floor space and reduced heat utilization efficiency. The reason is that the heat source and the steam boiler must be connected through the flue. In order to avoid increased heat loss due to the long transportation distance, the pipeline must be short, which has higher requirements for equipment layout and floor space; secondly, the pipeline will inevitably have heat loss, and the heat utilization rate is not as good as in-situ utilization.

[0005] To sum up, the traditional pyrolysis activation process requires a large number of equipment, the process route is long and complicated, and the overall thermal utilization rate still has room for improvement. Summary of the invention

[0006] In order to overcome the shortcomings of the above-mentioned prior art, the purpose of the present invention is to provide an integrated device and method for in-situ pyrolysis and oxidation of organic solid waste with carbon-steam, so as to reduce the number of equipment and avoid condensation of tar in the pyrolysis products in the equipment to cause blockage, while improving heat utilization and reducing overall costs.

[0007] In order to achieve the above object, the technical solution adopted by the present invention is:

[0008] An organic solid waste in-situ pyrolysis oxidized carbon-steam integrated device, comprising a pyrolysis oxidized carbon-steam integrated furnace, wherein the pyrolysis oxidized carbon-steam integrated furnace is divided into a pyrolysis carbonization chamber, a pyrolysis gas oxygen-controlled combustion chamber and a pyrolysis gas peroxygen incineration chamber according to the function, and the pyrolysis gas peroxygen incineration chamber is divided into a pyrolysis gas peroxygen incineration zone and a steam generation zone along the vertical direction; wherein the pyrolysis gas oxygen-controlled combustion chamber is located above the pyrolysis carbonization chamber, the pyrolysis gas oxygen-controlled combustion chamber is communicated with the inside of the pyrolysis gas peroxygen incineration chamber, and the steam generation zone is located above the pyrolysis gas peroxygen incineration zone;

[0009] The pyrolysis carbonization chamber is equipped with a horizontal stirring and conveying system. Along the material conveying direction, the pyrolysis carbonization chamber is divided into a pyrolysis zone, an air activation zone and a steam activation zone. The pyrolysis gas oxygen-controlled combustion chamber receives the pyrolysis gas generated by the pyrolysis carbonization chamber for oxygen-controlled combustion. The heat generated by the combustion is radiated to the pyrolysis carbonization chamber to provide energy for pyrolysis activation in situ.

[0010] The unburned pyrolysis gas in the pyrolysis gas oxygen-controlled combustion chamber enters the pyrolysis gas peroxygen combustion chamber, and is peroxygen-combusted in the pyrolysis gas peroxygen combustion zone to obtain flue gas. The heat carried by the flue gas is used to produce steam in the steam generation zone and supplied to the steam activation zone.

[0011] In one embodiment, a light oil burner is provided at the starting end of the pyrolysis carbonization chamber as an energy source for the initial startup of the device and energy supplement during operation. The pyrolysis carbonization-steam integrated furnace is provided with an induced draft fan, which is used to lead the pyrolysis gas generated in the pyrolysis carbonization chamber to the pyrolysis gas oxygen-controlled combustion chamber. The pyrolysis carbonization-steam integrated furnace maintains a slightly negative pressure state to prevent odor leakage.

[0012] In one embodiment, the pyrolysis oxidation carbon-steam integrated furnace is an internal heat horizontal stirring type, and the horizontal stirring and conveying system includes a pyrolysis activation conveying shaft.

[0013] In one embodiment, the pyrolysis oxidation carbon-steam integrated furnace is provided with a material inlet, a biochar outlet, an air supply inlet, a steam inlet and a pyrolysis gas combustion air supply inlet. The air supply inlet is provided corresponding to the air activation zone, the steam inlet is provided corresponding to the steam activation zone, and the pyrolysis gas combustion air supply inlet is provided corresponding to the pyrolysis gas oxygen-controlled combustion chamber.

[0014] In one embodiment, the steam generation zone is arranged with a plurality of steam pipes, which are arranged in a circle with a flue gas path in the middle. The flue gas heats the walls of the surrounding steam pipes to generate steam, and the generated steam is supplied to the steam activation zone.

[0015] In one embodiment, a pyrolysis gas combustion air supply inlet is provided corresponding to the pyrolysis gas peroxygen incineration zone, and its smoke outlet is communicated with the steam generation zone, so as to directly provide energy for steam generation in situ.

[0016] In one embodiment, the pyrolysis gas peroxygen combustion zone is arranged directly below the steam generation zone, and the smoke outlet of the pyrolysis gas peroxygen combustion zone is at the top and is directly connected to the steam generation zone through an induced draft fan.

[0017] In one embodiment, air is provided to the air activation zone, the pyrolysis gas oxygen-controlled combustion chamber and the pyrolysis gas over-oxygen incineration zone through an air supply system, and the air supply system is a valve and frequency conversion two-phase control of the air intake volume.

[0018] The present invention also provides a method for in-situ pyrolysis and oxidation of organic solid waste to carbon-steam, which is implemented based on the organic solid waste in-situ pyrolysis and oxidation of carbon-steam integrated device, and comprises the following steps:

[0019] Feeding the pyrolysis carbonization chamber with organic solid waste, controlling the temperature of the pyrolysis zone at 400-600°C, pyrolyzing and carbonizing the material; and igniting the generated pyrolysis gas at the starting end of the feeding;

[0020] Start the horizontal stirring and conveying system to convey the pyrolysis and carbonized materials to the air activation zone, control the temperature of the air activation zone at 800-900°C, and introduce air to activate the materials;

[0021] The air-activated material is then transferred to the steam activation zone, where the temperature is controlled at 800-900°C and steam is introduced to steam-activate the material.

[0022] The pyrolysis gas generated in the pyrolysis zone enters the pyrolysis gas oxygen-controlled combustion chamber upward, the temperature of the pyrolysis gas oxygen-controlled combustion chamber is controlled at 800-900°C, and air is introduced, the air excess coefficient is 2, and the pyrolysis gas is subjected to oxygen-controlled combustion, wherein the air supply amount is 10-30% of the total air supply amount;

[0023] The exhaust gas of the pyrolysis gas oxygen-controlled combustion chamber enters the pyrolysis gas peroxygen incineration zone, the temperature of the pyrolysis gas peroxygen incineration zone is controlled at 900-1050° C., and air is introduced to perform peroxygen incineration on the incompletely burned pyrolysis gas, wherein the air supply is 170-190% of the total air supply;

[0024] The flue gas discharged from the pyrolysis gas peroxygen incineration zone is used to produce steam, and the obtained steam is supplied to the steam activation zone.

[0025] In one embodiment, the organic solid waste has an organic matter content greater than 35% and a moisture content less than 15%.

[0026] Compared with the prior art, the present invention has the following beneficial effects:

[0027] The present invention highly couples pyrolysis carbonization, pyrolysis gas oxidation combustion, and flue gas in-situ steam conversion, thereby solving the problem of tar blockage caused by the traditional separation and recovery or combustion of pyrolysis gas / pyrolysis oil from the pyrolysis chamber, and further avoids the separation of waste heat flue gas utilization and steam boiler, thereby improving heat utilization efficiency, saving floor space, simplifying process flow and equipment, and realizing scientific disposal of organic solid waste and resource utilization of carbon-steam cogeneration.

[0028] The present invention divides the oxidative combustion of pyrolysis gas into two links: oxygen-controlled combustion and over-oxygen incineration. An appropriate amount of air is introduced into the pyrolysis gas oxygen-controlled combustion chamber to maintain a high-temperature environment in the furnace and meet the pyrolysis carbonization and activation conditions. Excessive oxygen is supplied in the pyrolysis gas over-oxygen incineration zone to achieve complete combustion of combustible components, completely release the heat of the combustible components, increase the total heat of the steam boiler and reduce the subsequent flue gas purification pressure. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] Figure 1 It is a schematic diagram of the structure of the present invention.

[0030] Figure 2 It is a schematic diagram of the internal structure of the pyrolysis carbonization chamber of the present invention. DETAILED DESCRIPTION

[0031] The embodiments of the present invention are described in detail below with reference to the accompanying drawings and examples.

[0032] The present invention discloses an organic solid waste in-situ pyrolysis oxidized carbon-steam integrated device, which mainly includes a pyrolysis oxidized carbon-steam integrated furnace. According to the function, the present invention divides the pyrolysis oxidized carbon-steam integrated furnace into a pyrolysis carbonization chamber, a pyrolysis gas oxygen-controlled combustion chamber 9 and a pyrolysis gas peroxygen incineration chamber, and divides the pyrolysis gas peroxygen incineration chamber into a pyrolysis gas peroxygen incineration zone 11 and a steam generation zone 13 along the vertical direction. The pyrolysis gas oxygen-controlled combustion chamber 9 is located above the pyrolysis carbonization chamber, and the pyrolysis gas oxygen-controlled combustion chamber 9 is also directly connected to the pyrolysis gas peroxygen incineration zone 11, and the overall device adopts a closed feeding design.

[0033] For details, please refer to Figure 1 and Figure 2 As shown, the pyrolysis carbonization chamber has a material inlet 1 and a biochar outlet 4, and a built-in horizontal stirring and conveying system. The material inlet 1 is connected to the uniform feeding closed system, and the material is fed through the uniform feeding closed system. The horizontal stirring and conveying system conveys the material from the material inlet 1 to the direction of the biochar outlet 4, that is, the present invention adopts a horizontal material conveying direction. Along the material conveying direction, the pyrolysis carbonization chamber is divided into three areas: pyrolysis zone 3, air activation zone 5 and steam activation zone 7. Therefore, the material entering the pyrolysis carbonization chamber is pyrolyzed, air activated and steam activated in turn, and the solid biochar is obtained as a product, which is sent out from the biochar outlet 4.

[0034] The pyrolysis gas generated by the pyrolysis of the material in the pyrolysis carbonization chamber directly goes up to the pyrolysis gas oxygen-controlled combustion chamber 9 in the furnace, and oxygen-controlled combustion is carried out after the air is introduced. The heat generated by the combustion can be radiated to the pyrolysis carbonization chamber to provide energy for solid phase drying and pyrolysis activation.

[0035] Since the pyrolysis gas oxygen-controlled combustion chamber 9 performs oxygen-controlled combustion, there is some pyrolysis gas that is not completely burned. This part of the pyrolysis gas is introduced into the pyrolysis gas peroxygen incineration zone 11, and is peroxygenally incinerated in the pyrolysis gas peroxygen incineration zone 11 to be converted into heat in the form of flue gas. This heat can generate steam products in situ in the steam generation zone 13 and is supplied to the steam activation zone 7.

[0036] Through the above structure, the present invention realizes the coupling of pyrolysis carbonization, pyrolysis gas oxidation combustion and flue gas in-situ conversion to steam. Biomass waste is used as raw material. In the oxygen-deficient environment of the pyrolysis zone 3 at the bottom of the furnace, the combustible pyrolysis gas produced by the material volatilization due to heat is burned in situ in the upper pyrolysis gas oxygen-controlled combustion chamber 9 in the furnace to release heat. The heat is radiated to the surface and interior of the lower material for in-situ utilization, thereby promoting the pyrolysis reaction to continue. The excess heat is subsequently utilized in the steam generation zone 13 to generate high-temperature steam, and the steam is recycled to the steam activation zone 7 in the pyrolysis carbonization chamber to react with biochar for activation and quality improvement. In this process, biomass solid waste is converted into biological activated carbon.

[0037] In a further embodiment of the present invention, the pyrolysis oxidation carbon-steam integrated furnace is an internal heat horizontal stirring type, the pyrolysis carbonization is an internal heat type, the material transportation is a horizontal stirring type, and the horizontal stirring and conveying system includes a pyrolysis activation conveying shaft 2, and the pyrolysis activation conveying shaft 2 is a spiral shaft. The pyrolysis activation conveying shaft 2 is used to realize that the material passes through the pyrolysis zone 3, the air activation zone 5 and the steam activation zone 7 in sequence. During the transportation process, the pyrolysis and the air activation and water vapor activation of the charcoal after pyrolysis are completed in sequence. According to the spatial volume ratio, the pyrolysis zone: air activation zone: steam activation zone is approximately 5:2:3. At the same time, in order to ensure that the temperature of the pyrolysis gas-controlled oxygen combustion chamber 9 can be effectively radiated to the pyrolysis carbonization chamber, the height ratio of the pyrolysis gas-controlled oxygen combustion chamber 9 to the pyrolysis carbonization chamber needs to be designed according to the material processing capacity, and verified and improved through experiments. This design process is not difficult for those skilled in the art.

[0038] In a further embodiment of the present invention, the pyrolysis oxidation carbon-steam integrated furnace is provided with an air supply inlet 6 and a steam inlet 8. The air supply inlet 6 is provided corresponding to the air activation zone 5, and the steam inlet 8 is provided corresponding to the steam activation zone 7. Thus, air can be directly and specifically supplied to the air activation zone 5 through the air supply inlet 6, and steam can be directly and specifically supplied to the steam activation zone 7 through the steam inlet 8.

[0039] In a further embodiment of the present invention, the pyrolysis gas oxygen-controlled combustion chamber 9 is the upper space of the pyrolysis oxidized carbon-steam integrated furnace, and the solid material undergoes pyrolysis and activation in the pyrolysis carbonization chamber, and the generated pyrolysis gas and activation gas enter the upper part, and air is supplied to the pyrolysis gas oxygen-controlled combustion chamber 9 to realize partial combustion of the pyrolysis gas, that is, oxygen-controlled combustion, and the generated heat is directly radiated downward to the pyrolysis zone 3 and activation zone 7 at the lower part. Through oxygen-controlled combustion, the temperature of the pyrolysis gas oxygen-controlled combustion chamber 9 can be controlled, thereby providing heat for the pyrolysis and activation of the lower part in situ. Among them, the pyrolysis oxidized carbon-steam integrated furnace is provided with a pyrolysis gas combustion air supply inlet 10 corresponding to the pyrolysis gas oxygen-controlled combustion chamber 9, thereby, air can be directly and specifically fed into the pyrolysis gas oxygen-controlled combustion chamber 9 through the pyrolysis gas combustion air supply inlet 10.

[0040] In a further embodiment of the present invention, a light oil burner is provided at the starting end of the pyrolysis carbonization chamber as an energy source for the initial startup of the system and as an energy supplement during operation. An induced draft fan can be arranged in the pyrolysis carbonization-steam integrated furnace to guide the generated pyrolysis gas upward into the pyrolysis gas oxygen-controlled combustion chamber 9. The pyrolysis carbonization-steam integrated furnace maintains a slightly negative pressure state to prevent odor leakage. The internal shape of the pyrolysis carbonization-steam integrated furnace has no special structure and is consistent with the external dimensions. Figure 1 The volume is designed according to the processing scale. The pyrolysis gas controlled oxygen combustion chamber 9 of the present invention performs combustion, and the pyrolysis carbonization chamber performs pyrolysis at the same time, which is realized by the following principle:

[0041] After the material is heated in the furnace, pyrolysis begins in the pyrolysis zone 3, and pyrolysis gas is volatilized from the inside of the material. The pyrolysis gas is a combustible gas with a low density and can diffuse upward. In addition, under the action of the induced draft fan, the pyrolysis gas can be further ensured to enter the pyrolysis gas oxygen-controlled combustion chamber 9 upward. Air is blown into the pyrolysis gas oxygen-controlled combustion chamber 9 through the pyrolysis gas combustion air supply inlet 10. When the light oil burner is ignited, the pyrolysis gas will burn and release heat. Later, when the furnace temperature is increased and the material is continuously input, the light oil burner is turned off, and the pyrolysis gas continues to burn in the upper pyrolysis gas oxygen-controlled combustion chamber 9, and the heat is radiated to the lower pyrolysis carbonization chamber, and the material continues to pyrolyze.

[0042] In a further embodiment of the present invention, the steam generating area 13 of the present invention is arranged with a plurality of steam pipes. Specifically, the steam pipes are arranged in a surrounding manner, with flue gas running in the middle to heat the walls of the surrounding steam pipes to generate steam, and the generated steam is supplied to the steam activation area 7.

[0043] In a further embodiment of the present invention, the pyrolysis gas peroxygen combustion zone 11 can be connected to the steam generation zone 13 and be an integrated structure. The pyrolysis gas burns in the lower pyrolysis gas peroxygen combustion zone 11, and the generated flue gas directly enters the upper steam generation zone 13, heating the surrounding steam pipe walls to generate steam from the water in the pipe. A pyrolysis gas combustion air supply inlet 12 is provided corresponding to the pyrolysis gas peroxygen combustion zone 11, so that air can be directly and specifically supplied to the pyrolysis gas peroxygen combustion zone 11 through the pyrolysis gas combustion air supply inlet 12, and the flue gas outlet is directly connected to the steam generation zone 13, directly providing energy for steam generation in situ.

[0044] In a further embodiment of the present invention, air is provided to the air activation zone 5, the pyrolysis gas oxygen-controlled combustion chamber 9 and the pyrolysis gas oxygen-peroxide incineration zone 11 through an air supply system, and the air supply system is a valve and frequency conversion two-phase control of the air intake volume.

[0045] According to the above integrated device, the method for in-situ pyrolysis and oxidation of organic solid waste to carbon-gas of the present invention mainly comprises the following steps:

[0046] Feed the pyrolysis carbonization chamber. In the present invention, the original material is organic solid waste, typically organic solid waste with a dry organic matter content of more than 35% such as biomass, dried sludge, etc. Its moisture content is preferably less than 15%, and the material is homogeneous and can be pre-crushed to a size of about 5cm*5cm and a thickness of less than 2-5mm. The material can be supplied to the pyrolysis carbonization chamber through a uniform feeding closed system, which requires entering a uniformly sealed and supplied system to prevent air from entering the pyrolysis carbonization chamber. Pyrolysis requires anoxic or anaerobic conditions. The temperature of the pyrolysis zone 3 is then controlled at 400-600°C to perform pyrolysis carbonization on the material. During the first run, it is necessary to ignite the generated pyrolysis gas at the starting end of the feed, and the pyrolysis gas can continue to burn after the operation is stable.

[0047] Start the horizontal stirring and conveying system, control the speed, and convey the pyrolysis carbonized material to the air activation zone 5 while ensuring the pyrolysis effect in the pyrolysis zone 3. Control the temperature of the air activation zone 5 at 800-900°C, and introduce air to activate the material. The amount of air introduced is adjusted in real time according to the combustion phenomenon and temperature during the actual operation. The activation of charcoal is a process of mixed action of multiple gases, mainly water vapor. In the actual activation process, water vapor, air, and flue gas after combustion will react with charcoal to varying degrees. The role of air activation here is mainly to remove the tar that may remain on the surface of the charcoal by reacting with oxygen in the air in the form of combustion, which is convenient for subsequent water vapor further activation.

[0048] The air-activated material is further transferred to the steam activation zone 7, where the temperature is controlled at 800-900°C and steam is introduced. The steam volume is preferably more than twice the charcoal produced after pyrolysis, and the material is steam activated. For example, if the pyrolysis charcoal volume is 100kg / h, the water vapor introduction volume is required to be greater than 200kg / h. Water vapor is used as an activator to react with charcoal, and a rich porous structure is etched on the surface and inside of the charcoal to increase its specific surface area and transform the charcoal into activated charcoal. The specific reaction process is: C+H20→CO+H2.

[0049] The cavity of the pyrolysis oxidation carbon-steam integrated furnace of the present invention is relatively large, and the amount of air introduced is relatively small, which can ensure the oxygen-deficient or oxygen-free atmosphere of the pyrolysis zone 3. First, the amount of air introduced will quickly react with the combustible pyrolysis gas to form combustion, and the oxygen is consumed and converted into CO2 and H2O; secondly, the induced draft fan is used to maintain negative pressure in the entire system, that is, the gas maintains a state of rapid flow to the rear section; finally, the introduced air will not quickly diffuse to the carbonization zone at the bottom of the pyrolysis oxidation carbon-steam integrated furnace, ensuring that the entire furnace chamber is an oxygen-deficient environment.

[0050] The pyrolysis gas generated in the pyrolysis carbonization chamber enters the pyrolysis gas oxygen-controlled combustion chamber 9 upward, the temperature of the pyrolysis gas oxygen-controlled combustion chamber 9 is controlled at 800-900°C, and air is introduced with an excess air coefficient of 2, and the pyrolysis gas is subjected to oxygen-controlled combustion, wherein the air supply is 10-30% of the total air supply, and the generated heat is transferred to the pyrolysis zone 3 and used as pyrolysis energy.

[0051] The exhaust gas of the pyrolysis gas oxygen-controlled combustion chamber 9 enters the pyrolysis gas peroxygen incineration zone 11, and the temperature of the pyrolysis gas peroxygen incineration zone 11 is controlled at 900-1050°C, and excess air or oxygen is introduced to perform peroxygen incineration on the unburned pyrolysis gas, so that all the pyrolysis gas is completely burned, wherein the air supply is 170-190% of the total gas supply.

[0052] The flue gas discharged from the pyrolysis gas peroxygen incineration zone 11 enters the steam generation zone 13 to produce steam, and the obtained steam is supplied to the steam activation zone 7 .

[0053] In a specific application embodiment of the present invention, a 24t / d garden waste treatment project in a certain city is taken as an example:

[0054] The raw materials come from green garden waste (mainly branches and trunks of various tree species), with an initial moisture content of about 15%. After being crushed, they are made into thin blocks with a diameter of 3 to 5 mm as processing raw materials;

[0055] The material is sent to the thermal pyrolysis oxidized carbon-steam integrated furnace for treatment, with a furnace processing capacity of 1t / h, a temperature of 500℃ in the pyrolysis zone 3, a residence time of 20-25min, a temperature of 850℃ in the steam activation zone 7, a residence time of 15-20min, a temperature of 900℃ in the pyrolysis gas controlled oxygen combustion chamber 9, a temperature of 1000℃ in the pyrolysis gas peroxygen incineration zone 11, and a high-temperature flue gas enters the steam generation zone 13 for heat utilization, with a steam output of about 2.6t / h and a flue gas temperature of 160℃ at the boiler outlet. The steam is recycled to the pyrolysis oxidized carbon-steam integrated furnace, with a steam input of ≥0.4t / h, and a final activated carbon output of about 0.15t / h.

[0056] After analysis, the main products are 0.15t / h activated carbon and 2.2t / h high-temperature steam. The performance indicators of activated carbon are iodine value 500mg / g and specific surface area 600m 2 / g, after long-term operation, the whole system was found to have no tar or solid phase blockage problems.

Claims

1. An organic solid waste in-situ pyrolysis oxidation carbon-steam integrated device, characterized in that: The invention comprises a pyrolysis carbonization furnace and a steam furnace. According to the function, the pyrolysis carbonization furnace is divided into a pyrolysis carbonization chamber, a pyrolysis gas oxygen-controlled combustion chamber (9) and a pyrolysis gas peroxygen combustion chamber. The pyrolysis gas peroxygen combustion chamber is divided into a pyrolysis gas peroxygen combustion zone (11) and a steam generation zone (13) along the vertical direction. The pyrolysis gas oxygen-controlled combustion chamber is located above the pyrolysis carbonization chamber, the pyrolysis gas oxygen-controlled combustion chamber (9) is connected to the inside of the pyrolysis gas peroxygen combustion chamber, and the steam generation zone (13) is located above the pyrolysis gas peroxygen combustion zone (11). The pyrolysis carbonization chamber is equipped with a horizontal stirring and conveying system. Along the material conveying direction, the pyrolysis carbonization chamber is divided into a pyrolysis zone (3), an air activation zone (5) and a steam activation zone (7); the pyrolysis gas oxygen-controlled combustion chamber (9) receives the pyrolysis gas generated by the pyrolysis carbonization chamber for oxygen-controlled combustion, and the heat generated by the combustion is radiated to the pyrolysis carbonization chamber, providing energy for pyrolysis activation in situ; The unburned pyrolysis gas in the pyrolysis gas oxygen-controlled combustion chamber (9) enters the pyrolysis gas peroxygen combustion chamber and is peroxygen-combusted in the pyrolysis gas peroxygen combustion zone (11) to obtain flue gas. The heat carried by the flue gas is used to produce steam in the steam generation zone (13) and supplied to the steam activation zone (7).

2. The in-situ pyrolysis and oxidation carbon-steam integrated device for organic solid waste according to claim 1 is characterized in that: A light oil burner is provided at the starting end of the pyrolysis carbonization chamber as an energy source for the initial startup of the device and as an energy supplement during operation. The pyrolysis carbonization-steam integrated furnace is provided with an induced draft fan, which is used to guide the pyrolysis gas generated in the pyrolysis carbonization chamber to the pyrolysis gas oxygen-controlled combustion chamber (9). The pyrolysis carbonization-steam integrated furnace maintains a slightly negative pressure state to prevent odor leakage.

3. The in-situ pyrolysis and oxidation carbon-steam integrated device for organic solid waste according to claim 1 or 2, characterized in that: The pyrolysis oxidized carbon-steam integrated furnace is of an internally heated horizontal stirring type, and the horizontal stirring and conveying system comprises a pyrolysis activation conveying shaft (2).

4. The in-situ pyrolysis and oxidation carbon-steam integrated device for organic solid waste according to claim 1 is characterized in that: The pyrolysis oxidation carbon-steam integrated furnace is provided with a material inlet (1), a biochar outlet (4), an air supply inlet (6), a steam inlet (8) and a pyrolysis gas combustion air supply inlet (10); the air supply inlet (6) is provided corresponding to the air activation zone (5), the steam inlet (8) is provided corresponding to the steam activation zone (7), and the pyrolysis gas combustion air supply inlet (10) is provided corresponding to the pyrolysis gas oxygen-controlled combustion chamber (9).

5. The in-situ pyrolysis and oxidation carbon-steam integrated device for organic solid waste according to claim 1 is characterized in that: The steam generation area (13) is arranged with a plurality of steam pipes, each of which is arranged in a circle with a flue gas path in the middle. The flue gas heats the walls of the surrounding steam pipes to generate steam, and the generated steam is supplied to the steam activation area (7).

6. The in-situ pyrolysis and oxidation carbon-steam integrated device for organic solid waste according to claim 5, characterized in that: A pyrolysis gas combustion air supply inlet (12) is provided corresponding to the pyrolysis gas peroxygen combustion zone (11), and its smoke outlet is communicated with the steam generation zone (13), so as to directly provide energy for steam generation in situ.

7. The in-situ pyrolysis and oxidation carbon-steam integrated device for organic solid waste according to claim 6, characterized in that: The pyrolysis gas peroxygen combustion zone (11) is arranged directly below the steam generation zone (13), and the smoke outlet of the pyrolysis gas peroxygen combustion zone (11) is at the top and is directly connected to the steam generation zone (13) through an induced draft fan.

8. The in-situ pyrolysis and oxidation carbon-steam integrated device for organic solid waste according to claim 1 is characterized in that: Air is provided to the air activation zone (5), the pyrolysis gas oxygen-controlled combustion chamber (9) and the pyrolysis gas oxygen-peroxidation incineration zone (11) through an air supply system, and the oxygen supply air system is a valve and frequency conversion two-phase control of air intake.

9. A method for in-situ pyrolysis and oxidation of organic solid waste to carbon-steam, based on the organic solid waste in-situ pyrolysis and oxidation of carbon-steam integrated device according to any one of claims 1 to 8, comprising the following steps: Feeding materials into the pyrolysis carbonization chamber, the materials are organic solid waste, controlling the temperature of the pyrolysis zone (3) at 400-600°C, pyrolyzing and carbonizing the materials; and igniting the generated pyrolysis gas at the starting end of the feeding; The horizontal stirring and conveying system is started to convey the pyrolyzed and carbonized material to the air activation zone (5), the temperature of the air activation zone (5) is controlled at 800-900° C., and air is introduced to air-activate the material; The air-activated material is further transferred to the steam activation zone (7), the temperature of the steam activation zone (7) is controlled at 800-900°C, and steam is introduced to steam-activate the material; The pyrolysis gas generated in the pyrolysis zone (3) enters the pyrolysis gas oxygen-controlled combustion chamber (9) upward, the temperature of the pyrolysis gas oxygen-controlled combustion chamber (9) is controlled at 800-900° C., and air is introduced, the air excess coefficient is 2, and the pyrolysis gas is subjected to oxygen-controlled combustion, wherein the air supply amount is 10-30% of the total air supply amount; The exhaust gas of the pyrolysis gas oxygen-controlled combustion chamber (9) enters the pyrolysis gas oxygen-controlled combustion zone (11), the temperature of the pyrolysis gas oxygen-controlled combustion zone (11) is controlled at 900-1050° C., and air is introduced to perform oxygen-controlled combustion on the incompletely burned pyrolysis gas, wherein the air supply amount is 170-190% of the total air supply amount; The flue gas discharged from the pyrolysis gas peroxygen incineration zone (11) is used to produce steam, and the obtained steam is supplied to the steam activation zone (7).

10. The method for in-situ pyrolysis and oxidation of organic solid waste to carbon-gas according to claim 9, characterized in that: The organic solid waste has an organic matter content greater than 35% and a moisture content less than 15%.

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