An organic solid waste pyrolysis system and method

Abstract

The present invention discloses an organic solid waste pyrolysis system and method. The system includes a feeding subsystem, a pyrolysis subsystem, and a pyrolysis gas purification subsystem connected in sequence; the feeding subsystem includes a feeding pipe; the pyrolysis subsystem includes a partition rotary kiln, a burner inside the kiln, and a non-condensable gas incinerator; the partition rotary kiln includes a feeding port, a pyrolysis gas outlet, a jacket flue gas inlet, and a jacket flue gas outlet; the pyrolysis gas outlet is connected to the inlet of the pyrolysis gas purification subsystem for purifying the pyrolysis gas to obtain non-condensable gas; the pyrolysis gas purification subsystem is connected to the burner inside the kiln through a first non-condensable gas delivery pipeline to provide non-condensable gas for the combustion of the burner inside the kiln; the pyrolysis gas purification subsystem is connected to the inlet of the non-condensable gas incinerator through a second non-condensable gas delivery pipeline for generating flue gas; the first outlet of the non-condensable gas incinerator is connected to the jacket flue gas inlet. The system of the present invention has high heat exchange efficiency and operates safely and stably.

Description

Technical Field

[0001] The present invention relates to an organic solid waste pyrolysis system and method. Background Art

[0002] Among the treatment methods of organic solid waste (such as domestic waste, agricultural and forestry biomass, etc., containing a certain amount of organic components, with a low calorific value but mostly capable of self-sustained combustion), pyrolysis technology under anoxic or even anaerobic conditions can remove and thermally crack the organic components in the raw materials, achieving the goals of reduction and harmlessness. At the same time, there is no minimum treatment scale requirement for the incineration line by a power station steam turbine, and it has the characteristic of more flexible scale, and can be applied to different demand scenarios within 5t / d to 200t / d. However, the current pyrolysis technology still has some disadvantages.

[0003] For example, patent document CN111635773A discloses an organic solid waste pyrolysis gasification system and method, which has the following several problems:

[0004] (1) The combustion chamber is arranged at the tail of the rotary gasification kiln, and part of the pyrolysis gas produced by the rotary kiln is sent back to the combustion chamber for incineration, and the high-temperature flue gas generated by the incineration of this part of the pyrolysis gas is used as a heat source. After passing through a high-temperature dust removal net, it enters the rotary gasification kiln and is in direct contact with the material to achieve convective heat transfer. The intensity of convective heat transfer and wall heat transfer between the high-temperature flue gas and the material is not as good as radiative heat transfer. Therefore, for a rotary kiln using convective heat transfer or wall heat conduction, the diameter and length of the kiln body are usually large, while the actual filling degree of the material is very low, usually 5% - 8%.

[0005] (2) This system needs to provide excessive high-temperature flue gas for heat exchange with the material, and the pyrolysis gas generated by the material will be mixed with the inert components in the flue gas, resulting in a decrease in the calorific value of the mixed gas. As the number of cycles increases, the calorific value of the pyrolysis gas generated by the rotary gasification kiln gradually tends to be balanced. Therefore, this system cannot handle materials with low calorific value (such as industrial waste salts containing organic substances, unclassified domestic waste, sludge and oily sludge with a high water content) or materials with large calorific value fluctuations (such as various hazardous waste mixtures in industrial parks), and even raw material coal blending or combustion chamber supplementary combustion is required to ensure stable operation.

[0006] Again, for example, patent document CN204829926U discloses a domestic waste hierarchical gasification system for rotary kiln gasification and plasma melting, which uses the high-temperature gas generated by the melting furnace as an external heat source for pyrolysis gasification, and at the same time recovers the heat of the syngas to improve the thermal efficiency of the system. The rotary kiln type pyrolysis gasifier conducts convective heat transfer between the high-temperature syngas and the material for pyrolysis reaction, and also has the problems of low heat transfer efficiency, large equipment size, and low material filling rate in patent document CN111635773A.

[0007] In summary, the organic solid waste pyrolysis technology in the prior art urgently needs to improve the heat transfer efficiency of the pyrolysis reactor. Summary of the Invention

[0008] The present invention provides an organic solid waste pyrolysis system and method to solve the problem of low heat exchange efficiency of the indirect rotary kiln in the existing organic solid waste pyrolysis technology. The indirect rotary kiln of the present invention combines in-kiln radiation heat exchange and shell-and-tube heat exchange, with high heat exchange efficiency, and the pyrolysis reaction system operates safely and stably.

[0009] The present invention solves the above technical problems through the following technical solutions.

[0010] The present invention provides an organic solid waste pyrolysis system, which includes a feeding subsystem, a pyrolysis subsystem, and a pyrolysis gas purification subsystem connected in sequence;

[0011] The feeding subsystem includes a feeding pipe;

[0012] The pyrolysis subsystem includes an indirect rotary kiln, an in-kiln burner, and a non-condensable gas incinerator;

[0013] The indirect rotary kiln includes a feeding port, a pyrolysis gas outlet, a jacket flue gas inlet, and a jacket flue gas outlet;

[0014] The feeding pipe passes through the feeding port, and the outlet of the feeding pipe is located inside the indirect rotary kiln;

[0015] The in-kiln burner is arranged at the kiln head of the indirect rotary kiln;

[0016] The pyrolysis gas outlet is connected to the inlet of the pyrolysis gas purification subsystem for purifying the pyrolysis gas to obtain non-condensable gas;

[0017] The pyrolysis gas purification subsystem is connected to the in-kiln burner through a first non-condensable gas delivery pipeline to provide non-condensable gas for the combustion of the in-kiln burner; the pyrolysis gas purification subsystem is connected to the inlet of the non-condensable gas incinerator through a second non-condensable gas delivery pipeline for generating flue gas;

[0018] The first outlet of the non-condensable gas incinerator is connected to the jacket flue gas inlet;

[0019] The jacket flue gas inlet and the jacket flue gas outlet are respectively arranged at both ends of the outer jacket of the indirect rotary kiln.

[0020] In the present invention, the in-kiln burner incinerates the pyrolysis non-condensable gas in the indirect rotary kiln, and the flame generated by the incineration provides part of the heat required for the pyrolysis of the raw material in the form of radiation heat exchange. The first outlet of the non-condensable gas incinerator is connected to the jacket flue gas inlet, and the high-temperature flue gas obtained by the incineration is used for heat exchange for the indirect rotary kiln. Thus, the in-kiln radiation heat exchange and the outer jacket shell-and-tube heat exchange together meet all the heat required for the pyrolysis of the raw material.

[0021] In the present invention, preferably, the feeding subsystem further includes a raw material storage tank and a raw material conveying device. The raw material storage tank is used to store the dried raw materials.

[0022] Among them, preferably, the raw material conveying device includes a grab crane and a silo. The grab crane conveys the raw materials in the raw material storage tank to the silo, and the outlet at the bottom of the silo is connected to the inlet pipeline of the feeding pipe to convey the raw materials to the feeding pipe.

[0023] In the present invention, preferably, a hydraulic ram pump and a piston push rod are further provided in the pipeline of the feeding pipe. The piston push rod in the feeding pipe is driven by the hydraulic ram pump, and the raw materials are compressed under the extrusion pressure in the feeding pipe, and the air in the gaps between the raw materials is discharged, reducing the entry of unmeasurable external air into the downstream pyrolysis subsystem along with the raw materials; at the same time, the compressed raw materials form a material plug to prevent the high-temperature gas in the pyrolysis subsystem operating under slightly positive pressure from surging back to the feeding pipe.

[0024] In the present invention, those skilled in the art know that the two ends of the partition rotary kiln can be respectively referred to as the kiln head and the kiln tail, and the feeding port of the partition rotary kiln is generally arranged at the kiln head.

[0025] In the present invention, preferably, a kiln head seal cover is provided at one end of the partition rotary kiln close to the kiln head, and the kiln head seal cover is rotatably connected to the partition rotary kiln to form a dynamic and static seal.

[0026] Among them, preferably, the in-kiln burner is fixed in the kiln head seal cover.

[0027] Among them, preferably, the feeding pipe is fixed in the kiln head seal cover.

[0028] Preferably, the feeding pipe is located above the in-kiln burner, the feeding pipe is arranged tangent to the outside of the in-kiln burner, and the feeding pipe and the in-kiln burner are respectively arranged tangent to the inside of the kiln head seal cover; the centers of the feeding pipe, the in-kiln burner, and the partition rotary kiln are on a straight line. Thus, the connecting line of the centers of the feeding pipe and the in-kiln burner is perpendicular to the material accumulation surface (as Figure 2 , that is, ∠a + ∠b = 90°), and the in-kiln burner is located between the feeding pipe and the material. According to the dynamic accumulation angle of the material in the kiln body, the angles of the feeding pipe and the in-kiln burner are determined to optimize the radiation heat transfer effect.

[0029] In the present invention, preferably, the kiln head is of a reduced diameter structure to reduce the dynamic and static seal area.

[0030] In the present invention, preferably, the kiln tail of the partition rotary kiln is of a straight cylinder structure, and the kiln tail seal cover of the partition rotary kiln is rotatably connected to the partition rotary kiln to form a dynamic and static seal.

[0031] In the present invention, preferably, the partition rotary kiln further includes a material outlet; the material outlet is located below the kiln tail of the partition rotary kiln, and the material outlet is used to recover the material pyrolyzed by the partition rotary kiln.

[0032] In the present invention, preferably, the kiln tail sealing cover of the partition rotary kiln is further provided with a first pyrolysis gas thermometer and a pyrolysis gas pressure gauge.

[0033] In the present invention, preferably, the pyrolysis subsystem further includes a first flue gas branch, a second flue gas branch and a total flue gas line;

[0034] The jacket flue gas outlet is connected to the inlet of the first flue gas branch; the second outlet of the non-condensable gas incinerator is connected to the inlet of the second flue gas branch, and the first flue gas branch and the second flue gas branch converge into the total flue gas line.

[0035] Among them, preferably, the outlet of the total flue gas line is sequentially connected to the raw material drying unit and the flue gas purification unit.

[0036] Among them, preferably, a first flow regulating valve is provided on the first flue gas branch, a second flow regulating valve is provided on the second flue gas branch, and the first flow regulating valve and the second flow regulating valve are used to adjust and distribute the ratio of the flue gas flow rate leading to the outer jacket of the partition rotary kiln to the flue gas flow rate of the second flue gas branch.

[0037] Among them, preferably, a first flue gas thermometer is provided in the pipeline connecting the first outlet of the non-condensable gas incinerator to the jacket flue gas inlet, and a second flue gas thermometer is further provided on the first flue gas branch.

[0038] In the present invention, preferably, the pyrolysis subsystem further includes a non-condensable gas main pipeline, an evacuation pipe and a natural gas pipeline; the inlet of the non-condensable gas main pipeline is connected to the pyrolysis gas purification subsystem, the outlet of the non-condensable gas main pipeline is respectively connected to the first non-condensable gas conveying pipeline and the second non-condensable gas conveying pipeline, and a non-condensable gas induced draft fan, a first shut-off valve, an evacuation port and a natural gas inlet are provided on the non-condensable gas main pipeline; the inlet of the evacuation pipe is connected to the evacuation port of the non-condensable gas main pipeline, and a second shut-off valve is provided on the evacuation pipe; the outlet of the natural gas pipeline is connected to the natural gas inlet, and the natural gas inlet is located in the downstream pipeline of the first shut-off valve.

[0039] Among them, preferably, a third flow regulating valve and a first non-condensable gas flowmeter are provided in the first non-condensable gas conveying pipeline.

[0040] Among them, preferably, a fourth flow regulating valve and a second non-condensable gas flowmeter are provided in the second non-condensable gas conveying pipeline.

[0041] Preferably, a third shut-off valve is provided on the natural gas pipeline for cutting in or out the natural gas supply operation.

[0042] Preferably, a non-condensable gas combustion analyzer is further provided at the outlet of the non-condensable gas induced draft fan. In a preferred embodiment, the non-condensable gas combustion analyzer can detect information such as the calorific value and oxygen content of the non-condensable gas.

[0043] Preferably, the pyrolysis subsystem further includes a non-condensable gas inlet pressure regulating valve and a non-condensable gas thermometer, which are arranged in the pipeline connecting the non-condensable gas induced draft fan and the pyrolysis gas purification subsystem. In a preferred embodiment, the pressure of the pyrolysis gas pressure gauge can be controlled by regulating the non-condensable gas inlet pressure regulating valve in a piezoresistive throttling manner to maintain a slightly positive pressure operation of the shell-and-tube rotary kiln. The non-condensable gas thermometer can be used to monitor the temperature drop of the non-condensable gas and the tar removal situation.

[0044] In the present invention, preferably, the pyrolysis subsystem further includes a blower for supplying air and / or oxygen to the pyrolysis subsystem; the first outlet pipeline of the blower is connected to the burner inside the kiln, and the second outlet pipeline of the blower is connected to the inlet of the non-condensable gas incinerator.

[0045] Preferably, a first oxidant flowmeter and a fifth flow regulating valve are provided on the first outlet pipeline of the blower; a second oxidant flowmeter and a sixth flow regulating valve are provided on the second outlet pipeline of the blower. In a preferred embodiment, by controlling the fifth flow regulating valve and the third flow regulating valve, the air coefficient inside the shell-and-tube rotary kiln can be made about 0.7 to achieve slightly oxygen-deficient combustion of the burner inside the kiln and prevent unreacted oxygen from mixing into the high-temperature pyrolysis gas; in addition, by controlling the sixth flow regulating valve and the fourth flow regulating valve, the flue gas temperature at the outlet of the non-condensable gas incinerator can be ensured to be about 650 °C to prevent the pipeline and the shell of the shell-and-tube rotary kiln from overheating.

[0046] In the present invention, preferably, the pyrolysis gas purification subsystem includes a spray tower, the inlet of the spray tower is connected to the pyrolysis gas outlet, and the non-condensable gas outlet pipeline of the spray tower is respectively connected to the first non-condensable gas conveying pipeline and the second non-condensable gas conveying pipeline. In a preferred embodiment, after the non-condensable gas outlet pipeline of the spray tower is connected to the non-condensable gas main pipeline, it is respectively connected to the first non-condensable gas conveying pipeline and the second non-condensable gas conveying pipeline.

[0047] Preferably, a second pyrolysis gas thermometer is provided in the pipeline connecting the inlet of the spray tower and the pyrolysis gas outlet.

[0048] Preferably, the liquid outlet of the spray tower is connected to an oil-water separation tank, which is located below the spray tower for oil-water separation.

[0049] Preferably, the water phase outlet of the oil-water separation tank is connected to a spray water cooling unit; the oil phase outlet of the oil-water separation tank is connected to a tar treatment unit, or the oil phase outlet of the oil-water separation tank is connected to the inlet of the non-condensable gas incinerator. The spray water cooling unit can adopt closed-circuit air cooling.

[0050] Preferably, the water phase outlet of the oil-water separation tank is connected to the spray water cooling unit and the spray tower in sequence, whereby the spray water of the spray tower can be recycled.

[0051] More preferably, the spray water cooling unit is also connected to the atomizing water pipeline of the discharging subsystem.

[0052] More preferably, a spray pump and a spray water flow regulating valve are also provided in the pipeline connecting the spray water cooling unit and the spray tower.

[0053] In the present invention, preferably, the organic solid waste pyrolysis system further includes a discharging subsystem; the discharging subsystem is connected to the material outlet of the partition rotary kiln.

[0054] Among them, preferably, the discharging subsystem includes a closed slag scraping conveyor and a product storage tank connected in sequence.

[0055] Preferably, a number of atomizing water spray nozzles are provided on the closed slag scraping conveyor along the traveling direction of the pyrolysis coke residue. Preferably, the discharging subsystem further includes an atomizing water pipeline, and a number of the atomizing water spray nozzles are provided on the atomizing water pipeline; more preferably, a coke discharging thermometer is provided at the outlet of the closed slag scraping conveyor, and an atomizing water regulating valve is provided on the atomizing water pipeline to adjust the spray amount so that the temperature measured by the coke discharging thermometer is maintained at 150-200 °C to achieve semi-dry quenching of the pyrolysis coke residue. The discharging subsystem adopts a closed semi-dry quenching process, which increases the airtightness of the system, improves the reusability of the slag discharge, and does not generate waste water. In a preferred embodiment, the inlet of the atomizing water pipeline is connected to the first atomizing water outlet of the pyrolysis gas purification subsystem.

[0056] Preferably, a fourth shut-off valve is provided in the outlet pipeline of the closed slag scraping conveyor, and a fifth shut-off valve is provided in the outlet pipeline of the product storage tank.

[0057] Preferably, the outlet of the product storage tank is connected to a pyrolysis residue treatment unit to send the pyrolysis residue to the pyrolysis residue treatment unit for harmless treatment after separating the recyclable metals, such as sanitary landfill, direct incineration or use as gasification raw materials, etc.

[0058] The present invention also provides a method for pyrolyzing organic solid waste, which is carried out by using the organic solid waste pyrolysis system as described above, and includes the following steps:

[0059] Convey the organic solid waste to the partitioned rotary kiln through the feed pipe, and burn it through the burner in the kiln to obtain pyrolysis gas;

[0060] Convey the pyrolysis gas to the pyrolysis gas purification subsystem, and purify the pyrolysis gas to obtain non-condensable gas;

[0061] Divide the non-condensable gas into at least two parts, convey a part of the non-condensable gas to the burner in the kiln to provide non-condensable gas for the combustion of the burner in the kiln; and convey a part of the non-condensable gas to the non-condensable gas incinerator to obtain flue gas through incineration;

[0062] Convey the flue gas to the outer jacket of the partitioned rotary kiln to provide heat for the partitioned rotary kiln.

[0063] In a preferred embodiment of the present invention, the startup of the organic solid waste pyrolysis system includes: a partitioned rotary kiln startup step, a non-condensable gas incinerator startup step, an oxygen replacement step in the partitioned rotary kiln, a load increase adjustment step, a step of replacing natural gas with non-condensable gas, and a system dynamic balance step;

[0064] The partitioned rotary kiln startup step includes:

[0065] S1.1. Under the cold state of the system, the partitioned rotary kiln starts to rotate at a low speed. During the rotation process, check the positioning scales at the head and tail of the partitioned rotary kiln to determine whether the radial runout and axial positioning of the kiln body of the partitioned rotary kiln meet the sealing requirements of the head seal cover and the tail seal cover;

[0066] S1.2. Gradually increase the rotation speed of the partitioned rotary kiln until the rated speed, and check the rotation and runout conditions of the kiln body of the partitioned rotary kiln;

[0067] The rotation speed of the low-speed rotation is generally 5-25% of the rated speed, which is known to those skilled in the art;

[0068] The non-condensable gas incinerator startup step includes:

[0069] S2.1. Start the spray tower, the spray water cooling unit and the spray pump;

[0070] S2.2. Open the second shut-off valve, close the first shut-off valve, start the non-condensable gas induced draft fan, and adjust the opening of the non-condensable gas inlet pressure regulating valve so that the pyrolysis gas pressure gauge shows a slight negative pressure;

[0071] S2.3. Open the third shut-off valve, start the forced draft fan, and coordinately control the valve openings of the third flow regulating valve, the fifth flow regulating valve, the fourth flow regulating valve, and the sixth flow regulating valve to enable slightly oxygen-deficient combustion of the burners in the kiln (i.e., the excess air coefficient < 1) and normal combustion of the non-condensable gas incinerator (i.e., the excess air coefficient > 1); preheat the shell of the partition rotary kiln through the non-condensable gas incinerator and the burners in the kiln, and displace the air in the partition rotary kiln with flue gas;

[0072] S2.4. Adjust the opening of the non-condensable gas inlet pressure regulating valve to keep the pyrolysis gas pressure gauge showing a slightly negative pressure to maintain a stable slightly negative pressure inside the shell of the partition rotary kiln;

[0073] The oxygen displacement step inside the partition rotary kiln includes:

[0074] S3.1. Adjust the opening of the non-condensable gas inlet pressure regulating valve to keep the pyrolysis gas pressure gauge showing a slightly positive pressure;

[0075] S3.2. Keep the burners in the kiln stable in the slightly oxygen-deficient combustion state, and observe that the oxygen concentration measured by the non-condensable gas gas analyzer gradually decreases from 21% (i.e., the oxygen concentration in the air) to the safe range (≤ 0.5% Vol.); until the oxygen displacement in the partition rotary kiln and its pyrolysis gas pipeline is complete;

[0076] The load increase adjustment step includes:

[0077] S4.1. Use the second pyrolysis gas thermometer as an index to determine the preheating degree of the pyrolysis gas pipeline to prevent condensation and blockage of the pyrolysis gas in the pipeline due to low temperature;

[0078] S4.2. Start the hydraulic piston pump and start feeding at a low load (30% - 50%). During the feeding process, observe the pressure change of the oil pressure cylinder of the hydraulic piston pump (reflecting the extrusion situation of the material in the feeding pipe and the shape of the formed material plug); at the same time, adjust the air volume of the non-condensable gas induced draft fan and the opening of the non-condensable gas inlet pressure regulating valve to keep the pyrolysis gas pressure gauge showing a slightly positive pressure;

[0079] S4.3. Gradually increase the load until the load reaches 100%;

[0080] The step of replacing natural gas with non-condensable gas includes:

[0081] S5.1. Observe the shape of the pyrolysis residue discharged from the discharge subsystem to judge whether the material is pyrolyzed sufficiently; judge whether the quality of the non-condensable gas meets the standard (i.e., judge whether it meets the demand for stable combustion) based on the calorific value measured by the non-condensable gas gas analyzer;

[0082] S5.2. Open the first shut-off valve and close the second shut-off valve to send the non-condensable gas into the main non-condensable gas pipeline; gradually reduce the opening degree of the third shut-off valve until it is completely closed to completely cut off the natural gas; at the same time, adjust the air volume of the blower and the opening degrees of the fifth flow regulating valve and the sixth flow regulating valve to keep the burner in the kiln in slightly oxygen-deficient combustion and the non-condensable gas incinerator in normal combustion;

[0083] The system dynamic balance steps include:

[0084] S6.1. Analyze the properties of the pyrolysis residue and observe whether there is undercooking or other conditions;

[0085] S6.2. Observe the measurement results of the first pyrolysis gas thermometer (whether the pyrolysis gas temperature meets the standard), the pyrolysis gas pressure gauge (whether the indirect rotary kiln operates stably under slightly positive pressure), the non-condensable gas thermometer (whether the spray tower works normally), the non-condensable gas fuel gas analyzer (whether the calorific value and oxygen concentration level of the non-condensable gas meet the standard), the first flue gas thermometer and the second flue gas thermometer (whether the heat provided by the flue gas in the outer jacket of the indirect rotary kiln is sufficient). If the set targets are achieved, it indicates that the system has achieved stable operation.

[0086] In a preferred embodiment of the present invention, the treatment steps for the low calorific value or excessive oxygen content of the non-condensable gas in the organic solid waste pyrolysis system include: the natural gas substitution for non-condensable gas step, the load reduction step, the oxygen replacement step in the indirect rotary kiln, the load increase step, the non-condensable gas substitution for natural gas step, and the system dynamic balance step;

[0087] The natural gas substitution for non-condensable gas step includes:

[0088] S1.1. Slowly open the opening degree of the third shut-off valve to send a small amount of natural gas into the main non-condensable gas pipeline to increase the calorific value of the non-condensable gas and keep the burner in the kiln and the non-condensable gas incinerator burning stably;

[0089] S1.2. During the process of opening the opening degree of the third shut-off valve, slowly increase the opening degree of the second shut-off valve and decrease the opening degree of the first shut-off valve until the third shut-off valve and the second shut-off valve are completely opened and the first shut-off valve is closed; during the process, maintain the burner in the kiln in slightly oxygen-deficient combustion, the non-condensable gas incinerator in normal combustion, and the pyrolysis gas pressure gauge showing slightly positive pressure;

[0090] The load reduction step includes:

[0091] S2.1. Reduce the feeding frequency of the hydraulic ram pump to reduce the feeding amount to a small load (30% - 50%). During the process, observe the pressure changes of the oil pressure cylinder of the hydraulic ram pump and the pyrolysis gas pressure gauge, and maintain the plug seal of the feeding pipe and the indirect rotary kiln operating under slightly positive pressure;

[0092] S2.2. Reduce the air volume of the air blower, and reduce the opening degree of the third shut-off valve to reduce the natural gas flow rate; thereby reducing the thermal power of the burners in the kiln and the non-condensable gas incinerator;

[0093] The oxygen replacement step in the partition rotary kiln includes:

[0094] S3.1. Adjust the opening degree of the non-condensable gas inlet pressure regulating valve to keep the pyrolysis gas pressure gauge showing a slightly positive pressure;

[0095] S3.2. Keep the burners in the kiln stable in a slightly oxygen-deficient combustion state, and observe that the oxygen concentration measured by the non-condensable gas gas analyzer gradually decreases to the safe range (≤0.5% Vol.); until the oxygen replacement in the partition rotary kiln and its pyrolysis gas pipeline is complete;

[0096] The load increase adjustment step includes:

[0097] S4.1. Use the second pyrolysis gas thermometer as an index to judge the preheating degree of the pyrolysis gas pipeline to prevent condensation and blockage of the pyrolysis gas in the pipeline due to low temperature;

[0098] S4.2. Start the hydraulic piston pump and start feeding at a low load (30% - 50%). During the feeding process, observe the pressure change of the oil pressure cylinder of the hydraulic piston pump (reflecting the extrusion situation of the material in the feeding pipe and the shape of the formed material plug); at the same time, adjust the air volume of the non-condensable gas induced draft fan and the opening degree of the non-condensable gas inlet pressure regulating valve to keep the pyrolysis gas pressure gauge showing a slightly positive pressure;

[0099] S4.3. Gradually increase the load until the load reaches 100%;

[0100] The step of replacing natural gas with non-condensable gas includes:

[0101] S5.1. Observe the shape of the pyrolysis residue discharged from the discharge subsystem to judge whether the material is pyrolyzed sufficiently; judge whether the quality of the non-condensable gas meets the standard by the calorific value measured by the non-condensable gas gas analyzer (that is, judge whether it meets the demand for stable combustion);

[0102] S5.2. Open the first shut-off valve and close the second shut-off valve to send the non-condensable gas into the non-condensable gas main pipeline; gradually reduce the opening degree of the third shut-off valve until the third shut-off valve is completely closed to completely cut off the natural gas; at the same time, adjust the air volume of the air blower and the opening degrees of the fifth flow regulating valve and the sixth flow regulating valve to keep the burners in the kiln in slightly oxygen-deficient combustion and the non-condensable gas incinerator burning normally;

[0103] The system dynamic balance step includes:

[0104] S6.1. Analyze the properties of the pyrolysis residue and observe whether there are undercooked situations;

[0105] S6.2. Observe the measurement results of the first pyrolysis gas thermometer (whether the pyrolysis gas temperature reaches the standard), the pyrolysis gas pressure gauge (whether the partitioned rotary kiln operates stably under slightly positive pressure), the non-condensable gas thermometer (whether the spray tower operates normally), the non-condensable gas fuel gas analyzer (whether the calorific value and oxygen concentration level of the non-condensable gas reach the standard), the first flue gas thermometer and the second flue gas thermometer (whether the heat provided by the flue gas in the outer jacket of the partitioned rotary kiln is sufficient). If the set target is achieved, it indicates that the system has achieved stable operation.

[0106] In a preferred embodiment of the present invention, the shutdown of the organic solid waste pyrolysis system includes: a natural gas replacing non-condensable gas step, a load reduction step, a natural gas cut-off step, and a partitioned rotary kiln shutdown step;

[0107] The natural gas replacing non-condensable gas step includes:

[0108] S1.1. Slowly open the opening degree of the third shut-off valve, deliver a small amount of natural gas to the non-condensable gas main pipeline, and increase the calorific value of the non-condensable gas to maintain stable combustion of the burner in the kiln and the non-condensable gas incinerator;

[0109] S1.2. During the process of opening the opening degree of the third shut-off valve, slowly increase the opening degree of the second shut-off valve and decrease the opening degree of the first shut-off valve until the third shut-off valve and the second shut-off valve are fully opened and the first shut-off valve is closed; during the process, maintain the burner in the kiln to burn under slightly oxygen-deficient conditions, the non-condensable gas incinerator to burn normally, and the pyrolysis gas pressure gauge to show slightly positive pressure;

[0110] The load reduction step includes:

[0111] S2.1. Stop the feeding action of the hydraulic plunger pump;

[0112] S2.2. The partitioned rotary kiln continues to operate at the rated speed until all the materials in the partitioned rotary kiln are discharged;

[0113] The natural gas cut-off step includes:

[0114] S3. Close the third flow regulating valve and the third shut-off valve, turn off the blower, and turn off the burner in the kiln;

[0115] The partitioned rotary kiln shutdown step includes:

[0116] S4.1. Observe that the calorific value of the gas detected by the non-condensable gas fuel gas analyzer drops to 0, that is, after all the combustible components in the partitioned rotary kiln and its pipelines are completely replaced, turn on the blower, turn on the fifth flow regulating valve, and let the outside cold air be transported from the burner in the kiln to the inside of the partitioned rotary kiln. Observe that the oxygen concentration detected by the non-condensable gas fuel gas analyzer returns to 21%, indicating that the flue gas in the kiln body has been completely replaced, and then the blower can be turned off;

[0117] S4.2. Reduce the rotational speed of the partition rotary kiln until the partition rotary kiln drops to the safe shutdown temperature, and then the partition rotary kiln can be shut down.

[0118] Based on common knowledge in the art, the above preferred conditions can be combined arbitrarily to obtain various preferred embodiments of the present invention.

[0119] The reagents and raw materials used in the present invention are all commercially available.

[0120] The positive and progressive effects of the present invention are as follows:

[0121] The partition rotary kiln of the present invention combines in-kiln radiation heat transfer and shell partition heat transfer, with high heat transfer efficiency and safe and stable operation of the pyrolysis reaction system. The organic solid waste pyrolysis system of the present invention can achieve safe and stable operation of the system and is widely applicable to the disposal of municipal domestic waste, oily sludge, hazardous waste salts, etc. BRIEF DESCRIPTION OF THE DRAWINGS

[0122] Figure 1 Schematic diagram of the organic solid waste pyrolysis system for Example 1.

[0123] Figure 2 Cross-sectional view of the in-kiln burner and the feed pipe for Example 1.

[0124] Figure 3 Schematic diagram of the in-kiln burner and the feed pipe for Example 1.

[0125] Figure 4 Flow chart of the start-up steps of the organic solid waste pyrolysis system for Example 1.

[0126] Figure 5 Flow chart of the treatment steps for low non-condensable gas calorific value or excessive oxygen content in the organic solid waste pyrolysis system for Example 1.

[0127] Figure 6 Schematic diagram of the furnace shutdown steps of the organic solid waste pyrolysis system for the example.

[0128] DESCRIPTION OF THE REFERENCE NUMERALS

[0129] Feed subsystem 1

[0130] Feed pipe 101

[0131] Piston push rod 102

[0132] Grab crane 103

[0133] Bunker 104

[0134] Hydraulic plunger pump 105

[0135] Pyrolysis subsystem 2

[0136] Partition Rotary Kiln 201

[0137] Feed Inlet 202

[0138] In-kiln Burner 203

[0139] Non-condensable Gas Incinerator 204

[0140] Pyrolysis Gas Outlet 205

[0141] Jacket Flue Gas Inlet 206

[0142] Jacket Flue Gas Outlet 207

[0143] Kiln Head 208

[0144] Kiln Tail 209

[0145] Kiln Head Sealing Cover 210

[0146] Material Outlet 211

[0147] First Pyrolysis Gas Thermometer 212

[0148] Pyrolysis Gas Pressure Gauge 213

[0149] First Flue Gas Branch 214

[0150] Second Flue Gas Branch 215

[0151] Main Flue Gas Line 216

[0152] Raw Material Drying Unit 217

[0153] Flue Gas Purification Unit 218

[0154] First Flow Control Valve 219

[0155] Second Flow Control Valve 220

[0156] Non-condensable Gas Main Pipeline 221

[0157] Vent Pipe 222

[0158] First Non-condensable Gas Transfer Pipeline 223

[0159] Second Non-condensable Gas Transfer Pipeline 224

[0160] Non-condensable Gas Induced Draft Fan 225

[0161] First Shut-off Valve 226

[0162] Second Shut-off Valve 227

[0163] Third Flow Control Valve 228

[0164] First Non-condensable Gas Flowmeter 229

[0165] Fourth Flow Regulating Valve 230

[0166] Second Non-Condensable Gas Flowmeter 231

[0167] Natural Gas Pipeline 232

[0168] Third Shutoff Valve 233

[0169] Non-Condensable Gas Combustion Analyzer 234

[0170] Non-Condensable Gas Inlet Pressure Regulating Valve 235

[0171] Non-Condensable Gas Thermometer 236

[0172] Air Blower 237

[0173] First Oxidant Flowmeter 238

[0174] Fifth Flow Regulating Valve 239

[0175] Second Oxidant Flowmeter 240

[0176] Sixth Flow Regulating Valve 241

[0177] First Flue Gas Thermometer 242

[0178] Second Flue Gas Thermometer 243

[0179] Pyrolysis Gas Purification Subsystem 3

[0180] Spray Tower 301

[0181] Non-Condensable Gas Outlet Pipeline 302

[0182] Second Pyrolysis Gas Thermometer 303

[0183] Oil-Water Separation Tank 304

[0184] Spray Water Cooling Unit 305

[0185] Tar Treatment Unit 306

[0186] Spray Pump 307

[0187] Spray Water Flow Regulating Valve 308

[0188] Discharge Subsystem 4

[0189] Atomizing Water Pipeline 401

[0190] Enclosed Slag Scraper Conveyor 402

[0191] Product Storage Tank 403

[0192] Atomizing Water Spray Nozzle 404

[0193] Coke discharging thermometer 405

[0194] Atomizing water regulating valve 406

[0195] Fourth shut-off valve 407

[0196] Fifth shut-off valve 408

[0197] Pyrolysis residue treatment unit 409 Detailed implementation manners

[0198] The present invention will be further described below by way of embodiments, but the present invention is not limited to the scope of the embodiments. For the experimental methods without specific conditions noted in the following embodiments, they are carried out according to conventional methods and conditions, or selected according to the product specifications.

[0199] Embodiment 1

[0200] As Figure 1 shown, the organic solid waste pyrolysis system of Embodiment 1 includes a feeding subsystem 1, a pyrolysis subsystem 2 and a pyrolysis gas purification subsystem 3 connected in sequence; the feeding subsystem 1 includes a feeding pipe 101; the pyrolysis subsystem 2 includes a shell-and-tube rotary kiln 201, an in-kiln burner 203 and a non-condensable gas incinerator 204; the shell-and-tube rotary kiln 201 includes a feeding port 202, a pyrolysis gas outlet 205, a jacket flue gas inlet 206 and a jacket flue gas outlet 207; the feeding pipe 101 passes through the feeding port 202, and the outlet of the feeding pipe 101 is located inside the shell-and-tube rotary kiln 201; the in-kiln burner 203 is arranged at the kiln head 208 of the shell-and-tube rotary kiln 201; the pyrolysis gas outlet 205 is connected to the inlet of the pyrolysis gas purification subsystem 3 for purifying the pyrolysis gas to obtain non-condensable gas; the pyrolysis gas purification subsystem 3 is connected to the in-kiln burner 203 through a first non-condensable gas delivery pipeline 223 to provide non-condensable gas for the combustion of the in-kiln burner 203; the pyrolysis gas purification subsystem 3 is connected to the inlet of the non-condensable gas incinerator 204 through a second non-condensable gas delivery pipeline 224 for generating flue gas; the first outlet of the non-condensable gas incinerator 204 is connected to the jacket flue gas inlet 206; the jacket flue gas inlet 206 and the jacket flue gas outlet 207 are respectively arranged at both ends of the outer jacket of the shell-and-tube rotary kiln 201.

[0201] The in-kiln burner 203 incinerates the pyrolysis non-condensable gas in the shell-and-tube rotary kiln 201, and the flame generated by the incineration provides part of the heat required for the pyrolysis of the raw material in the form of radiative heat transfer. The first outlet of the non-condensable gas incinerator 204 is connected to the jacket flue gas inlet 206, and the high-temperature flue gas obtained by the incineration is used for heat exchange with the shell-and-tube rotary kiln 201. Thus, the in-kiln radiative heat transfer and the outer jacket wall heat transfer together meet all the heat required for the pyrolysis of the raw material.

[0202] The feeding subsystem 1 further includes a raw material storage tank and raw material conveying equipment. The raw material storage tank is used to store the dried raw materials. The raw material conveying equipment includes a grab crane 103 and a silo 104. The grab crane 103 conveys the raw materials in the raw material storage tank to the silo 104. The outlet at the bottom of the silo 104 is connected to the inlet pipeline of the feed pipe 101 to convey the raw materials to the feed pipe 101. A hydraulic ram pump 105 and a piston push rod 102 are also provided in the pipeline of the feed pipe 101. The piston push rod 102 in the feed pipe 101 is driven by the hydraulic ram pump 105, and the raw materials are compressed under the extrusion pressure in the feed pipe 101. The air in the gaps between the raw materials is discharged, reducing the entry of unmeasurable external air into the downstream pyrolysis subsystem 2 along with the raw materials. At the same time, the compressed raw materials form a material plug to prevent the high-temperature gas in the pyrolysis subsystem 2 operating under slightly positive pressure from surging back into the feed pipe 101.

[0203] The two ends of the partition rotary kiln 201 are respectively a kiln head 208 and a kiln tail 209. A kiln head seal cover 210 is provided at one end of the partition rotary kiln 201 close to the kiln head 208, and the kiln head seal cover 210 is rotatably connected to the partition rotary kiln 201 to form a dynamic and static seal. The in-kiln burner 203 is fixed inside the kiln head seal cover 210. The feed pipe 101 is fixed inside the kiln head seal cover 210.

[0204] As Figure 2 and Figure 3 shown, the feed pipe 101 is located above the in-kiln burner 203. The feed pipe 101 is externally tangent to the in-kiln burner 203, and the feed pipe 101 and the in-kiln burner 203 are respectively internally tangent to the kiln head seal cover 210. The centers of the feed pipe 101, the in-kiln burner 203, and the partition rotary kiln 201 are on the same straight line. Thus, the connecting line of the centers of the feed pipe 101 and the in-kiln burner 203 is perpendicular to the material accumulation surface (as Figure 2 , that is, ∠a + ∠b = 90°), and the in-kiln burner 203 is located between the feed pipe 101 and the material. According to the dynamic accumulation angle of the material in the kiln body, the angles of the feed pipe 101 and the in-kiln burner 203 are determined to optimize the radiation heat transfer effect.

[0205] The kiln head 208 has a reduced-opening structure to reduce the dynamic and static seal area.

[0206] The kiln tail 209 of the partition rotary kiln 201 has a straight cylinder structure, and the kiln tail seal cover of the partition rotary kiln 201 is rotatably connected to the partition rotary kiln 201 to form a dynamic and static seal.

[0207] The partition rotary kiln 201 further includes a material outlet 211; the material outlet 211 is located below the kiln tail 209 of the partition rotary kiln 201, and the material outlet 211 is used to recover the pyrolyzed materials of the partition rotary kiln 201. A first pyrolysis gas thermometer 212 and a pyrolysis gas pressure gauge 213 are also provided on the kiln tail seal cover of the partition rotary kiln 201.

[0208] The pyrolysis subsystem 2 further includes a first flue gas branch 214, a second flue gas branch 215, and a main flue gas line 216; the jacket flue gas outlet 207 is connected to the inlet of the first flue gas branch 214; the second outlet of the non-condensable gas incinerator 204 is connected to the inlet of the second flue gas branch 215, and the first flue gas branch 214 and the second flue gas branch 215 converge into the main flue gas line 216. The outlet of the main flue gas line 216 is sequentially connected to the raw material drying unit 217 and the flue gas purification unit 218. A first flow regulating valve 219 is provided on the first flue gas branch 214, and a second flow regulating valve 220 is provided on the second flue gas branch 215. The first flow regulating valve 219 and the second flow regulating valve 220 are used to adjust the ratio of the flue gas flow rate leading to the outer jacket of the partition rotary kiln 201 to the flue gas flow rate of the second flue gas branch 215.

[0209] A first flue gas thermometer 242 is provided in the pipeline connecting the first outlet of the non-condensable gas incinerator 204 to the jacket flue gas inlet 206, and a second flue gas thermometer 243 is also provided on the first flue gas branch 214.

[0210] The pyrolysis subsystem 2 further includes a non-condensable gas main pipeline 221, a vent pipe 222, and a natural gas pipeline 232; the inlet of the non-condensable gas main pipeline 221 is connected to the pyrolysis gas purification subsystem 3, the outlet of the non-condensable gas main pipeline 221 is respectively connected to a first non-condensable gas conveying pipeline 223 and a second non-condensable gas conveying pipeline 224, and a non-condensable gas induced draft fan 225, a first shut-off valve 226, a vent port, and a natural gas inlet are provided on the non-condensable gas main pipeline 221; the inlet of the vent pipe 222 is connected to the vent port of the non-condensable gas main pipeline 221, and a second shut-off valve 227 is provided on the vent pipe 222; the outlet of the natural gas pipeline 232 is connected to the natural gas inlet, and the natural gas inlet is located in the downstream pipeline of the first shut-off valve 226. A third flow regulating valve 228 and a first non-condensable gas flowmeter 229 are provided in the first non-condensable gas conveying pipeline 223. A fourth flow regulating valve 230 and a second non-condensable gas flowmeter 231 are provided in the second non-condensable gas conveying pipeline 224. A third shut-off valve 233 is provided on the natural gas pipeline 232 for cutting in or out the natural gas supply operation. A non-condensable gas-gas analyzer 234 is also provided at the outlet of the non-condensable gas induced draft fan 225. The non-condensable gas-gas analyzer 234 can detect information such as the calorific value and oxygen content of the non-condensable gas.

[0211] The pyrolysis subsystem 2 further includes a non-condensable gas inlet pressure regulating valve 235 and a non-condensable gas thermometer 236, which are provided in the pipeline connecting the non-condensable gas induced draft fan 225 and the pyrolysis gas purification subsystem 3. By adjusting the non-condensable gas inlet pressure regulating valve 235 in a piezoresistive throttling manner, the pressure of the pyrolysis gas pressure gauge 213 can be controlled to maintain the slightly positive pressure operation of the partition rotary kiln 201, and the non-condensable gas thermometer 236 can be used to monitor the temperature drop of the non-condensable gas and the tar removal situation.

[0212] The pyrolysis subsystem 2 further includes a blower 237 for supplying air and / or oxygen to the pyrolysis subsystem 2; the first outlet pipeline of the blower 237 is connected to the in-kiln burner 203, and the second outlet pipeline of the blower 237 is connected to the inlet of the non-condensable gas incinerator 204.

[0213] A first oxidant flowmeter 238 and a fifth flow regulating valve 239 are provided on the first outlet pipeline of the blower 237; a second oxidant flowmeter 240 and a sixth flow regulating valve 241 are provided on the second outlet pipeline of the blower 237. By controlling the fifth flow regulating valve 239 and the third flow regulating valve 228, the air coefficient in the partitioned rotary kiln 201 can be made about 0.7, realizing slightly oxygen-deficient combustion of the in-kiln burner 203 and preventing unreacted oxygen from mixing into the high-temperature pyrolysis gas; in addition, by controlling the sixth flow regulating valve 241 and the fourth flow regulating valve 230, the flue gas temperature at the outlet of the non-condensable gas incinerator 204 can be ensured to be about 650 °C, preventing overheating of the pipeline and the cylinder body of the partitioned rotary kiln 201.

[0214] The pyrolysis gas purification subsystem 3 includes a spray tower 301. The inlet of the spray tower 301 is connected to the pyrolysis gas outlet 205. After the non-condensable gas outlet pipeline 302 of the spray tower 301 is connected to the non-condensable gas main pipeline 221, it is respectively connected to the first non-condensable gas conveying pipeline 223 and the second non-condensable gas conveying pipeline 224. A second pyrolysis gas thermometer 303 is provided in the pipeline where the inlet of the spray tower 301 is connected to the pyrolysis gas outlet 205. The liquid outlet of the spray tower 301 is connected to an oil-water separation tank 304. The oil-water separation tank 304 is located below the spray tower 301 for oil-water separation. The water phase outlet of the oil-water separation tank 304 is connected to the spray water cooling unit 305; the oil phase outlet of the oil-water separation tank 304 is connected to the tar treatment unit 306. The spray water cooling unit 305 can adopt closed-air cooling. The water phase outlet of the oil-water separation tank 304 is sequentially connected to the spray water cooling unit 305 and the spray tower 301. Thus, the spray water of the spray tower 301 can be recycled. The spray water cooling unit 305 is also connected to the atomizing water pipeline 401 of the discharging subsystem 4. A spray pump 307 and a spray water flow regulating valve 308 are also provided in the pipeline connecting the spray water cooling unit 305 and the spray tower 301.

[0215] The organic solid waste pyrolysis system further includes a discharging subsystem 4; the discharging subsystem 4 is connected to the material outlet 211 of the partitioned rotary kiln 201. The discharging subsystem 4 includes a closed slag scraping conveyor 402 and a product storage tank 403 connected in sequence. The closed slag scraping conveyor 402 is provided with a plurality of atomizing water spray nozzles 404 along the traveling direction of the pyrolysis char. The atomizing water pipeline 401 is provided with a plurality of atomizing water spray nozzles 404; the outlet of the closed slag scraping conveyor 402 is provided with a coke discharging thermometer 405, and the atomizing water pipeline 401 is provided with an atomizing water regulating valve 406 to adjust the spraying amount so that the temperature measured by the coke discharging thermometer 405 is maintained at 150-200°C, realizing semi-dry quenching of the pyrolysis char. The discharging subsystem 4 adopts a closed semi-dry quenching process, which increases the airtightness of the system, improves the reusability of the slag discharge, and does not produce waste water. A fourth shut-off valve 407 is provided in the outlet pipeline of the closed slag scraping conveyor 402, and a fifth shut-off valve 408 is provided in the outlet pipeline of the product storage tank 403.

[0216] The outlet of the product storage tank 403 is connected to the pyrolysis residue treatment unit 409, and the pyrolysis residue is sent to the pyrolysis residue treatment unit 409 for harmless treatment after separating recyclable metals, such as sanitary landfill, direct incineration or being used as gasification raw materials, etc.

[0217] The organic solid waste pyrolysis method of the organic solid waste pyrolysis system in Embodiment 1 includes the following steps:

[0218] The organic solid waste is transported to the partitioned rotary kiln 201 through the feed pipe 101 and burned by the burner 203 in the kiln to obtain pyrolysis gas; the pyrolysis gas is transported to the pyrolysis gas purification subsystem 3 to purify the pyrolysis gas to obtain non-condensable gas; the non-condensable gas is divided into at least two parts, one part of the non-condensable gas is transported to the burner 203 in the kiln to provide non-condensable gas for the combustion of the burner 203 in the kiln; and one part of the non-condensable gas is transported to the non-condensable gas incinerator 204 to obtain flue gas through incineration; the flue gas is transported to the outer jacket of the partitioned rotary kiln 201 to provide heat for the partitioned rotary kiln 201.

[0219] As Figure 4 shown, the startup of the organic solid waste pyrolysis system includes: the startup step of the partitioned rotary kiln 201, the startup step of the non-condensable gas incinerator 204, the oxygen replacement step in the partitioned rotary kiln 201, the load increase adjustment step, the step of replacing natural gas with non-condensable gas, and the system dynamic balance step;

[0220] The startup step of the partitioned rotary kiln 201 includes:

[0221] S1.1. Under cold state of the system, the partition rotary kiln 201 starts to rotate slowly (0.5 r / min). During the rotation process, check the positioning scales at the kiln head 208 and the kiln tail 209 of the partition rotary kiln 201 to determine that the radial runout of the kiln body of the partition rotary kiln 201 ≤ 1.5 mm and whether the axial positioning meets the sealing requirements of the kiln head seal cover 210 and the kiln tail seal cover;

[0222] S1.2. Gradually increase the rotation speed of the partition rotary kiln 201 until the rated speed (2 r / min), and check the rotation and runout ≤ 1.5 mm of the kiln body of the partition rotary kiln 201;

[0223] The start-up steps of the non-condensable gas incinerator 204 include:

[0224] S2.1. Start the spray tower 301, the spray water cooling unit 305 and the spray pump 307, and adjust the spray water volume to 30 t / h and the water temperature below 35 °C;

[0225] S2.2. Open the second shut-off valve 227, close the first shut-off valve 226, start the non-condensable gas induced draft fan 225, set the frequency to 20 Hz, and adjust the opening of the non-condensable gas inlet pressure regulating valve 235 to 30% so that the pyrolysis gas pressure gauge 213 shows a slightly negative pressure (-100 Pa to -50 Pa);

[0226] S2.3. Open the third shut-off valve 233, open the forced draft fan 237, set the frequency to 40 Hz, and coordinately control the valve openings of the third flow regulating valve 228, the fifth flow regulating valve 239 and the fourth flow regulating valve 230, the sixth flow regulating valve 241 to make the burner 203 in the kiln burn with slightly insufficient oxygen (natural gas flow rate 7 Nm 3 / h, excess air coefficient = 0.7), and make the non-condensable gas incinerator 204 burn normally (natural gas flow rate 10 Nm 3 / h, excess air coefficient = 1.1; preheat the kiln body of the partition rotary kiln 201 through the non-condensable gas incinerator 204 and the burner 203 in the kiln, and displace the air in the partition rotary kiln 201 with flue gas;

[0227] S2.4. Adjust the opening of the non-condensable gas inlet pressure regulating valve 235 to 80%, and keep the pyrolysis gas pressure gauge 213 showing a slightly negative pressure to maintain the slightly negative pressure (-100 Pa to -50 Pa) stability in the kiln body of the partition rotary kiln 201;

[0228] The oxygen displacement steps in the partition rotary kiln 201 include:

[0229] S3.1. Adjust the opening of the non-condensable gas inlet pressure regulating valve 235 to 70%, and keep the pyrolysis gas pressure gauge 213 showing a slightly positive pressure (+50 Pa to +100 Pa);

[0230] S3.2. Keep the burner 203 in the kiln stable in a slightly oxygen-deficient combustion state, and observe that the oxygen concentration measured by the non-condensable gas analyzer 234 gradually decreases from 21% (i.e., the oxygen concentration in the air) to the safe range (decreases to 0.03% Vol.); until the oxygen replacement in the indirect rotary kiln 201 and its pyrolysis gas pipeline is complete;

[0231] The load increase adjustment steps include:

[0232] S4.1. Use the second pyrolysis gas thermometer 303 (reaching 200 °C) as an index to determine the preheating degree of the pyrolysis gas pipeline, and prevent condensation and blockage of the pyrolysis gas in the pipeline due to low temperature;

[0233] S4.2. Start the hydraulic piston pump 105 and start feeding at a small load (40%). During the feeding process, observe the pressure change of the oil cylinder of the hydraulic piston pump 105 (reflecting the extrusion situation of the material in the feeding pipe 101 and the shape of the formed material plug); at the same time, adjust the air volume of the non-condensable gas induced draft fan 225 to 30 Hz and the opening degree of the non-condensable gas inlet pressure regulating valve 235 to 75%, and keep the pyrolysis gas pressure gauge 213 showing a slightly positive pressure (+50 Pa to +100 Pa);

[0234] S4.3. Gradually increase the load until the load reaches 100%;

[0235] The steps of replacing natural gas with non-condensable gas include:

[0236] S5.1. Observe the form of the pyrolysis residue discharged from the discharge subsystem 4 to judge whether the material is pyrolyzed sufficiently; judge whether the quality of the non-condensable gas meets the standard (i.e., judge whether it meets the demand for stable combustion) according to the calorific value measured by the non-condensable gas analyzer 234 (the calorific value is about 4.5 MJ / Nm 3 )

[0237] S5.2. Open the first shut-off valve 226 and close the second shut-off valve 227 to send the non-condensable gas into the non-condensable gas main pipeline 221; gradually reduce the opening degree of the third shut-off valve 233 until the third shut-off valve 233 is completely closed to completely cut off the natural gas; at the same time, adjust the air volume of the air blower 237 and the opening degrees of the fifth flow regulating valve 239 and the sixth flow regulating valve 241 to keep the burner 203 in the kiln in slightly oxygen-deficient combustion and the non-condensable gas incinerator 204 burning normally;

[0238] The steps of system dynamic balance include:

[0239] S6.1. Analyze the properties of the pyrolysis residue and observe whether there are undercooked situations;

[0240] S6.2. Observe the measurement results of the first pyrolysis gas thermometer 212 (whether the pyrolysis gas temperature reaches 450 °C), the pyrolysis gas pressure gauge 213 (whether the indirect rotary kiln 201 operates stably at about +80 Pa), the non-condensable gas thermometer 236 (whether the spray tower 301 operates normally, 40 °C), the non-condensable gas fuel gas analyzer 234 (whether the calorific value and oxygen concentration level of the non-condensable gas meet the standards, calorific value 4.5 MJ / Nm 3 and the oxygen concentration is 0.08% Vol.), the first flue gas thermometer 242 and the second flue gas thermometer 243 (whether the heat provided by the flue gas in the outer jacket of the indirect rotary kiln 201 is sufficient, the first flue gas thermometer 242 and the second flue gas thermometer 243 are about 650 °C and 160 °C respectively). If the set target is achieved, it indicates that the system has achieved stable operation.

[0241] As Figure 5 shown, the treatment steps for low calorific value or excessive oxygen content of the non-condensable gas in the organic solid waste pyrolysis system include: natural gas replacing non-condensable gas step, load reduction step, oxygen replacement step in the indirect rotary kiln 201, load increase step, non-condensable gas replacing natural gas step, and system dynamic balance step;

[0242] The natural gas replacing non-condensable gas step includes:

[0243] S1.1. Slowly open the opening of the third shut-off valve 233, and send a small amount of natural gas to the non-condensable gas main pipeline 221 to increase the calorific value of the non-condensable gas, so as to maintain the stable combustion of the burner 203 in the kiln and the non-condensable gas incinerator 204;

[0244] S1.2. During the process of opening the opening of the third shut-off valve 233, slowly increase the opening of the second shut-off valve 227 and decrease the opening of the first shut-off valve 226 until the third shut-off valve 233 and the second shut-off valve 227 are fully opened and the first shut-off valve 226 is closed; during the process, maintain the burner 203 in the kiln to burn under slightly oxygen-deficient conditions, the non-condensable gas incinerator 204 to burn normally, and the pyrolysis gas pressure gauge 213 to show a slightly positive pressure (+50 Pa to +100 Pa);

[0245] The load reduction step includes:

[0246] S2.1. Reduce the feeding frequency of the hydraulic piston pump 105 to reduce the feeding amount to a small load (30%). During the process, observe the pressure changes of the oil cylinder of the hydraulic piston pump 105 and the pressure of the pyrolysis gas pressure gauge 213, and maintain the plug seal of the feeding pipe 101 and the indirect rotary kiln 201 to operate under slightly positive pressure conditions;

[0247] S2.2. Reduce the air volume of the blower 237, and reduce the opening of the third shut-off valve 233 to reduce the natural gas flow rate; to reduce the thermal power of the burner 203 in the kiln and the non-condensable gas incinerator 204;

[0248] The oxygen replacement steps in the partition rotary kiln 201 include (which can be the same as the oxygen replacement steps in the partition rotary kiln 201 during the startup of the organic solid waste pyrolysis system):

[0249] S3.1. Adjust the opening degree of the non-condensable gas inlet pressure regulating valve 235 to keep the pyrolysis gas pressure gauge 213 showing a slightly positive pressure;

[0250] S3.2. Keep the burner 203 in the kiln stable in a slightly oxygen-deficient combustion state, and observe that the oxygen concentration measured by the non-condensable gas gas analyzer 234 gradually decreases to the safe range (≤0.5%Vol.); until the oxygen replacement in the partition rotary kiln 201 and its pyrolysis gas pipeline is complete;

[0251] The load increase adjustment steps include (which can be the same as the load increase adjustment steps in the startup of the organic solid waste pyrolysis system):

[0252] S4.1. Take the second pyrolysis gas thermometer 303 as the judgment index for the preheating degree of the pyrolysis gas pipeline to prevent the pyrolysis gas from condensing and blocking in the pipeline due to low temperature;

[0253] S4.2. Start the hydraulic piston pump 105 and start feeding at a small load (30% - 50%). During the feeding process, observe the pressure change of the oil pressure cylinder of the hydraulic piston pump 105 (reflecting the extrusion situation of the material in the feeding pipe 101 and the formed plug shape); at the same time, adjust the air volume of the non-condensable gas induced draft fan 225 and the opening degree of the non-condensable gas inlet pressure regulating valve 235 to keep the pyrolysis gas pressure gauge 213 showing a slightly positive pressure;

[0254] S4.3. Gradually increase the load until the load reaches 100%;

[0255] The steps of replacing natural gas with non-condensable gas include (which can be the same as the steps of replacing natural gas with non-condensable gas in the startup of the organic solid waste pyrolysis system):

[0256] S5.1. Observe the form of the pyrolysis residue discharged from the discharge subsystem 4 to judge whether the material is pyrolyzed sufficiently; judge whether the quality of the non-condensable gas meets the standard by the calorific value measured by the non-condensable gas gas analyzer 234 (that is, judge whether it meets the demand for stable combustion);

[0257] S5.2. Open the first shut-off valve 226 and close the second shut-off valve 227 to send the non-condensable gas into the non-condensable gas main pipeline 221; gradually reduce the opening degree of the third shut-off valve 233 until the third shut-off valve 233 is completely closed to completely cut off the natural gas; at the same time, adjust the air volume of the air blower 237 and the opening degrees of the fifth flow regulating valve 239 and the sixth flow regulating valve 241 to keep the burner 203 in the kiln in slightly oxygen-deficient combustion and the non-condensable gas incinerator 204 burning normally;

[0258] The system dynamic balance steps include (which may be the same as the system dynamic balance steps in the startup of the organic solid waste pyrolysis system):

[0259] S6.1. Analyze the properties of the pyrolysis residue and observe whether there is any undercooking;

[0260] S6.2. Observe the measurement results of the first pyrolysis gas thermometer 212 (whether the pyrolysis gas temperature meets the standard), the pyrolysis gas pressure gauge 213 (whether the partition wall rotary kiln 201 operates at a stable micro-positive pressure), the non-condensable gas thermometer 236 (whether the spray tower 301 works normally), the non-condensable gas analyzer 234 (whether the calorific value and oxygen concentration level of the non-condensable gas meet the standard), the first flue gas thermometer 242 and the second flue gas thermometer 243 (whether the flue gas in the outer jacket of the partition wall rotary kiln 201 provides sufficient heat). If the set target is achieved, it means that the system has achieved stable operation.

[0261] like Figure 6 As shown, the shutdown of the organic solid waste pyrolysis system includes: a natural gas replacement non-condensable gas step, a load reduction step, a natural gas removal step, and a partition wall rotary kiln 201 shutdown step;

[0262] The steps of replacing non-condensable gas with natural gas include:

[0263] S1.1. Slowly open the third shut-off valve 233, deliver a small amount of natural gas to the non-condensable gas main pipeline 221, increase the calorific value of the non-condensable gas, in order to maintain the kiln burner 203 and the non-condensable gas incinerator 204 combustion stability;

[0264] S1.2. In the process of opening the third shut-off valve 233, slowly increase the opening of the second shut-off valve 227 and reduce the opening of the first shut-off valve 226 until the third shut-off valve 233 and the second shut-off valve 227 are fully opened and the first shut-off valve 226 is closed; in the process, the burner 203 in the kiln is kept burning under slightly hypoxic conditions, the non-condensable gas incinerator 204 is burning normally, and the pyrolysis gas pressure gauge 213 displays a slightly positive pressure;

[0265] The load reduction steps include:

[0266] S2.1. Stop the hydraulic piston pump 105 to push the material;

[0267] S2.2. The partition wall rotary kiln 201 continues to operate at the rated speed until all the materials in the partition wall rotary kiln 201 are discharged;

[0268] The natural gas removal steps include:

[0269] S3. Close the third flow regulating valve 228 and the third shut-off valve 233, turn off the blower 237, and turn off the kiln burner 203;

[0270] The shutdown steps of the partition wall rotary kiln 201 include:

[0271] S4.1. Observe that the calorific value of the gas detected by the non-condensable gas fuel analyzer 234 drops to 0, that is, after all the combustible components in the partitioned rotary kiln 201 and its pipeline are completely replaced, turn on the air blower 237 and the fifth flow regulating valve 239, so that the outside cold air is transported from the burner 203 in the kiln to the inside of the partitioned rotary kiln 201. Observe that the oxygen concentration detected by the non-condensable gas fuel analyzer 234 returns to 21%, indicating that the flue gas in the kiln body has been completely replaced, and then the air blower 237 can be turned off;

[0272] S4.2. Reduce the rotational speed of the partitioned rotary kiln 201 until the partitioned rotary kiln 201 drops to the safe shutdown temperature, and then the partitioned rotary kiln 201 can be turned off.

Claims

1. An organic solid waste pyrolysis system, characterized in that, It includes a feeding subsystem, a pyrolysis subsystem, and a pyrolysis gas purification subsystem that are connected in sequence; The feeding subsystem includes a feed pipe; The pyrolysis subsystem includes a shell-and-tube rotary kiln, an in-kiln burner, and a non-condensable gas incinerator; The shell-and-tube rotary kiln includes a feed inlet, a pyrolysis gas outlet, a jacket flue gas inlet, and a jacket flue gas outlet; The feed pipe passes through the feed inlet, and the outlet of the feed pipe is located inside the shell-and-tube rotary kiln; The in-kiln burner is arranged at the kiln head of the shell-and-tube rotary kiln; The pyrolysis gas outlet is connected to the inlet of the pyrolysis gas purification subsystem to purify the pyrolysis gas to obtain non-condensable gas; The pyrolysis gas purification subsystem is connected to the in-kiln burner through a first non-condensable gas pipeline to provide non-condensable gas for the combustion of the in-kiln burner; the pyrolysis gas purification subsystem is connected to the inlet of the non-condensable gas incinerator through a second non-condensable gas pipeline to generate flue gas; The first outlet of the non-condensable gas incinerator is connected to the jacket flue gas inlet; The jacket flue gas inlet and the jacket flue gas outlet are respectively arranged at both ends of the outer jacket of the shell-and-tube rotary kiln; A kiln head seal cover is arranged at one end of the shell-and-tube rotary kiln close to the kiln head, and the kiln head seal cover is rotatably connected to the shell-and-tube rotary kiln; the in-kiln burner is fixed inside the kiln head seal cover, and the feed pipe is fixed inside the kiln head seal cover; the feed pipe is located above the in-kiln burner, the feed pipe is externally tangent to the in-kiln burner, the feed pipe and the in-kiln burner are respectively internally tangent to the kiln head seal cover, and the centers of the feed pipe, the in-kiln burner, and the shell-and-tube rotary kiln are on a straight line.

2. The organic solid waste pyrolysis system according to claim 1, characterized in that, The feeding subsystem further includes a raw material storage tank and a raw material conveying device; And / or, a hydraulic piston pump and a piston push rod are further arranged in the pipeline of the feed pipe; And / or, the kiln head of the in-kiln burner is of a reduced diameter structure; And / or, the kiln tail of the shell-and-tube rotary kiln is of a straight cylinder structure, and the kiln tail seal cover of the shell-and-tube rotary kiln is rotatably connected to the shell-and-tube rotary kiln; And / or, the shell-and-tube rotary kiln further includes a material outlet; the material outlet is located below the kiln tail of the shell-and-tube rotary kiln; And / or, a first pyrolysis gas thermometer and a pyrolysis gas pressure gauge are further arranged on the kiln tail seal cover of the shell-and-tube rotary kiln.

3. The organic solid waste pyrolysis system according to claim 2, characterized in that, The raw material conveying device includes a grab crane and a silo.

4. The organic solid waste pyrolysis system according to claim 1, wherein The pyrolysis subsystem further includes a first flue gas branch, a second flue gas branch, and a flue gas main line; The jacket flue gas outlet is connected to the inlet of the first flue gas branch; the second outlet of the non-condensable gas incinerator is connected to the inlet of the second flue gas branch, and the first flue gas branch and the second flue gas branch converge into the flue gas main line.

5. The organic solid waste pyrolysis system according to claim 4, characterized in that, The outlet of the flue gas main line is sequentially connected to a raw material drying unit and a flue gas purification unit; And / or, a first flow regulating valve is arranged on the first flue gas branch, and a second flow regulating valve is arranged on the second flue gas branch; And / or, a first flue gas thermometer is arranged in the pipeline where the first outlet of the non-condensable gas incinerator is connected to the jacket flue gas inlet, and a second flue gas thermometer is further arranged on the first flue gas branch.

6. The organic solid waste pyrolysis system according to claim 1, characterized in that, The pyrolysis subsystem further includes a non-condensable gas main pipeline, a vent pipe, and a natural gas pipeline; the inlet of the non-condensable gas main pipeline is connected to the pyrolysis gas purification subsystem, the outlet of the non-condensable gas main pipeline is respectively connected to the first non-condensable gas transfer pipeline and the second non-condensable gas transfer pipeline, and a non-condensable gas induced draft fan, a first shut-off valve, a vent port, and a natural gas inlet are provided on the non-condensable gas main pipeline; the inlet of the vent pipe is connected to the vent port of the non-condensable gas main pipeline, and a second shut-off valve is provided on the vent pipe; the outlet of the natural gas pipeline is connected to the natural gas inlet, and the natural gas inlet is located in the downstream pipeline of the first shut-off valve.

7. The organic solid waste pyrolysis system according to claim 6, wherein, A third flow regulating valve and a first non-condensable gas flowmeter are provided in the first non-condensable gas transfer pipeline; and / or, a fourth flow regulating valve and a second non-condensable gas flowmeter are provided in the second non-condensable gas transfer pipeline; and / or, a third shut-off valve is provided on the natural gas pipeline; and / or, a non-condensable gas combustion analyzer is further provided at the outlet of the non-condensable gas induced draft fan; and / or, the pyrolysis subsystem further includes a non-condensable gas inlet pressure regulating valve and a non-condensable gas thermometer, and the non-condensable gas inlet pressure regulating valve and the non-condensable gas thermometer are provided in the pipeline connecting the non-condensable gas induced draft fan and the pyrolysis gas purification subsystem.

8. The organic solid waste pyrolysis system according to claim 1, wherein The pyrolysis subsystem further includes a blower for supplying air and / or oxygen to the pyrolysis subsystem; the first outlet pipeline of the blower is connected to the in-kiln burner, and the second outlet pipeline of the blower is connected to the inlet of the non-condensable gas incinerator.

9. The organic solid waste pyrolysis system according to claim 8, wherein, A first oxidant flowmeter and a fifth flow regulating valve are provided on the first outlet pipeline of the blower; a second oxidant flowmeter and a sixth flow regulating valve are provided on the second outlet pipeline of the blower.

10. The organic solid waste pyrolysis system according to claim 1, characterized in that, The pyrolysis gas purification subsystem includes a spray tower, the inlet of the spray tower is connected to the pyrolysis gas outlet, and the non-condensable gas outlet pipeline of the spray tower is respectively connected to the first non-condensable gas transfer pipeline and the second non-condensable gas transfer pipeline.

11. The organic solid waste pyrolysis system according to claim 10, characterized in that, After the non-condensable gas outlet pipeline of the spray tower is connected to the non-condensable gas main pipeline, it is respectively connected to the first non-condensable gas transfer pipeline and the second non-condensable gas transfer pipeline; and / or, a second pyrolysis gas thermometer is provided in the pipeline connecting the inlet of the spray tower and the pyrolysis gas outlet; and / or, the liquid outlet of the spray tower is connected to an oil-water separation tank, and the oil-water separation tank is located below the spray tower.

12. The organic solid waste pyrolysis system according to claim 11, wherein, The water phase outlet of the oil-water separation tank is connected to a spray water cooling unit; the oil phase outlet of the oil-water separation tank is connected to a tar treatment unit, or the oil phase outlet of the oil-water separation tank is connected to the inlet of the non-condensable gas incinerator; and / or, the water phase outlet of the oil-water separation tank is sequentially connected to the spray water cooling unit and the spray tower.

13. The organic solid waste pyrolysis system according to claim 12, characterized in that, A spray pump and a spray water flow regulating valve are further provided in the pipeline connecting the spray water cooling unit and the spray tower.

14. The organic solid waste pyrolysis system according to claim 13, characterized in that, The organic solid waste pyrolysis system further includes a discharging subsystem; the discharging subsystem is connected to the material outlet of the partition rotary kiln.

15. The organic solid waste pyrolysis system according to claim 14, characterized in that, The discharging subsystem includes a closed slag scraping conveyor and a product storage tank connected in sequence.

16. The organic solid waste pyrolysis system according to claim 15, characterized in that, The enclosed slag scraping conveyor is provided with a plurality of atomizing water spray nozzles along the traveling direction of the pyrolysis residual carbon; And / or, the discharge subsystem further includes an atomizing water pipeline, and the spray water cooling unit is also connected to the atomizing water pipeline of the discharge subsystem, and a plurality of the atomizing water spray nozzles are provided on the atomizing water pipeline.

17. The organic solid waste pyrolysis system according to claim 16, wherein, A coke discharging thermometer is provided at the outlet of the enclosed slag scraping conveyor, And / or, an atomizing water regulating valve is provided on the atomizing water pipeline; And / or, a fourth shut-off valve is provided in the outlet pipeline of the enclosed slag scraping conveyor, and a fifth shut-off valve is provided in the outlet pipeline of the product storage tank; And / or, the outlet of the product storage tank is connected to the pyrolysis residue treatment unit.

18. A method for pyrolyzing organic solid waste, characterized in that, It is carried out by using the organic solid waste pyrolysis system described in any one of claims 1 to 17, and includes the following steps: Convey the organic solid waste to the partition rotary kiln through the feed pipe, and burn it through the in-kiln burner to obtain pyrolysis gas; Convey the pyrolysis gas to the pyrolysis gas purification subsystem, and purify the pyrolysis gas to obtain non-condensable gas; Divide the non-condensable gas into at least two parts, convey a part of the non-condensable gas to the in-kiln burner to provide non-condensable gas for the combustion of the in-kiln burner; and convey a part of the non-condensable gas to the non-condensable gas incinerator to obtain flue gas through incineration; Convey the flue gas to the outer jacket of the partition rotary kiln to provide heat for the partition rotary kiln.

19. The pyrolysis method of organic solid waste according to claim 18, characterized in that, The startup of the organic solid waste pyrolysis system includes: the startup step of the partition rotary kiln, the startup step of the non-condensable gas incinerator, the oxygen replacement step in the partition rotary kiln, the load up-regulation step, the step of replacing natural gas with non-condensable gas, and the system dynamic balance step; The startup step of the partition rotary kiln includes: S1.

1. Under the cold state of the system, the partition rotary kiln starts to rotate at a low speed. During the rotation process, check the positioning scales at the head and tail of the partition rotary kiln to determine whether the radial runout and axial positioning of the kiln body of the partition rotary kiln meet the sealing requirements of the head seal cover and the tail seal cover; S1.

2. Gradually increase the rotation speed of the partition rotary kiln until the rated speed, and check the rotation and runout conditions of the kiln body of the partition rotary kiln; The startup step of the non-condensable gas incinerator includes: S2.

1. Start the spray tower, the spray water cooling unit and the spray pump; S2.

2. Open the second shut-off valve, close the first shut-off valve, start the non-condensable gas induced draft fan, and adjust the opening of the non-condensable gas inlet pressure regulating valve so that the pyrolysis gas pressure gauge shows a slight negative pressure; S2.

3. Open the third shut-off valve, start the forced draft fan, and coordinately control the valve openings of the third flow regulating valve, the fifth flow regulating valve, the fourth flow regulating valve, and the sixth flow regulating valve to make the in-kiln burner burn with slight oxygen deficiency and the non-condensable gas incinerator burn normally; S2.

4. Adjust the opening of the non-condensable gas inlet pressure regulating valve to keep the pyrolysis gas pressure gauge showing a slight negative pressure; The oxygen replacement step in the partition rotary kiln includes: S3.

1. Adjust the opening of the non-condensable gas inlet pressure regulating valve to keep the pyrolysis gas pressure gauge showing a slight positive pressure; S3.

2. Keep the burner in the kiln stable in a slightly oxygen-deficient combustion state, and observe that the oxygen concentration measured by the non-condensable gas gas analyzer gradually decreases from 21% to the safe range; until the oxygen replacement in the shell-and-tube rotary kiln and its pyrolysis gas pipeline is complete; The load increasing step includes: S4.

1. Use the second pyrolysis gas thermometer as an index to judge the preheating degree of the pyrolysis gas pipeline to prevent condensation and blockage of the pyrolysis gas in the pipeline due to low temperature; S4.

2. Start the hydraulic piston pump and start feeding at a small load. Observe the pressure change of the oil pressure cylinder of the hydraulic piston pump during the feeding process; at the same time, adjust the air volume of the non-condensable gas induced draft fan and the opening degree of the non-condensable gas inlet pressure regulating valve to keep the pyrolysis gas pressure gauge showing a slightly positive pressure; S4.

3. Gradually increase the load until the load reaches 100%; The step of replacing natural gas with non-condensable gas includes: S5.

1. Observe the morphology of the pyrolysis residue discharged from the discharge subsystem to judge whether the material is pyrolyzed sufficiently; judge whether the quality of the non-condensable gas meets the standard according to the calorific value measured by the non-condensable gas gas analyzer; S5.

2. Open the first shut-off valve and close the second shut-off valve to transport the non-condensable gas into the non-condensable gas main pipeline; gradually reduce the opening degree of the third shut-off valve until the third shut-off valve is completely closed to completely cut off the natural gas; at the same time, adjust the air volume of the forced draft fan and the opening degrees of the fifth flow regulating valve and the sixth flow regulating valve to keep the burner in the kiln in slightly oxygen-deficient combustion and the non-condensable gas incinerator burning normally; The system dynamic balance step includes: S6.

1. Analyze the properties of the pyrolysis residue and observe whether there is undercooking or other situations; S6.

2. Observe the measurement results of the first pyrolysis gas thermometer, pyrolysis gas pressure gauge, non-condensable gas thermometer, non-condensable gas gas analyzer, first flue gas thermometer and second flue gas thermometer. Reaching the set target indicates that the system has achieved stable operation; Alternatively, the treatment steps for the low calorific value or excessive oxygen content of the non-condensable gas in the organic solid waste pyrolysis system include: the natural gas replacing non-condensable gas step, the load decreasing step, the oxygen replacement step in the shell-and-tube rotary kiln, the load increasing step, the step of replacing natural gas with non-condensable gas and the system dynamic balance step; The natural gas replacing non-condensable gas step includes: S1.

1. Slowly open the opening degree of the third shut-off valve to transport a small amount of natural gas to the non-condensable gas main pipeline to increase the calorific value of the non-condensable gas and keep the combustion of the burner in the kiln and the non-condensable gas incinerator stable; S1.

2. During the process of opening the opening degree of the third shut-off valve, slowly increase the opening degree of the second shut-off valve and decrease the opening degree of the first shut-off valve until the third shut-off valve and the second shut-off valve are completely opened and the first shut-off valve is closed; during the process, maintain the burner in the kiln burning under slightly oxygen-deficient conditions, the non-condensable gas incinerator burning normally, and the pyrolysis gas pressure gauge showing a slightly positive pressure; The load decreasing step includes: S2.

1. Reduce the feeding frequency of the hydraulic piston pump to reduce the feeding amount to a small load. Observe the pressure changes of the oil pressure cylinder of the hydraulic piston pump and the pressure of the pyrolysis gas pressure gauge during the process, and maintain the plug seal of the feed pipe and the shell-and-tube rotary kiln operating under slightly positive pressure conditions; S2.

2. Reduce the air volume of the air blower, and reduce the opening degree of the third shut-off valve to reduce the natural gas flow rate; thereby reducing the thermal power of the burner in the kiln and the non-condensable gas incinerator; The oxygen replacement step in the partition rotary kiln includes: S3.

1. Adjust the opening degree of the non-condensable gas inlet pressure regulating valve to keep the pyrolysis gas pressure gauge showing a slightly positive pressure; S3.

2. Keep the burner in the kiln stable in a slightly oxygen-deficient combustion state, and observe that the oxygen concentration measured by the non-condensable gas gas analyzer gradually decreases to the safe range; until the oxygen replacement in the partition rotary kiln and its pyrolysis gas pipeline is complete; The load increase adjustment step includes: S4.

1. Use the second pyrolysis gas thermometer as an index to judge the preheating degree of the pyrolysis gas pipeline to prevent condensation and blockage of the pyrolysis gas in the pipeline due to low temperature; S4.

2. Start the hydraulic piston pump and start feeding at a small load. Observe the change of the oil cylinder pressure of the hydraulic piston pump during the feeding process; at the same time, adjust the air volume of the non-condensable gas induced draft fan and the opening degree of the non-condensable gas inlet pressure regulating valve to keep the pyrolysis gas pressure gauge showing a slightly positive pressure; S4.

3. Gradually increase the load until the load reaches 100%; The step of replacing natural gas with non-condensable gas includes: S5.

1. Observe the form of the pyrolysis residue discharged from the discharge subsystem to judge whether the material is pyrolyzed sufficiently; judge whether the quality of the non-condensable gas meets the standard according to the calorific value measured by the non-condensable gas gas analyzer; S5.

2. Open the first shut-off valve and close the second shut-off valve to send the non-condensable gas into the non-condensable gas main pipeline; gradually reduce the opening degree of the third shut-off valve until the third shut-off valve is completely closed to completely cut off the natural gas; at the same time, adjust the air volume of the air blower and the opening degrees of the fifth flow regulating valve and the sixth flow regulating valve to keep the burner in the kiln in slightly oxygen-deficient combustion and the non-condensable gas incinerator burning normally; The system dynamic balance step includes: S6.

1. Analyze the properties of the pyrolysis residue and observe whether there is undercooking or other conditions; S6.

2. Observe the measurement results of the first pyrolysis gas thermometer, pyrolysis gas pressure gauge, non-condensable gas thermometer, non-condensable gas gas analyzer, first flue gas thermometer and second flue gas thermometer. When the set target is reached, it indicates that the system has achieved stable operation; Alternatively, the shutdown of the organic solid waste pyrolysis system includes: the step of replacing non-condensable gas with natural gas, the load reduction adjustment step, the natural gas cut-off step and the partition rotary kiln shutdown step; The step of replacing non-condensable gas with natural gas includes: S1.

1. Slowly open the opening degree of the third shut-off valve, send a small amount of natural gas to the non-condensable gas main pipeline to increase the calorific value of the non-condensable gas, so as to keep the burner in the kiln and the non-condensable gas incinerator burning stably; S1.

2. During the process of opening the opening degree of the third shut-off valve, slowly increase the opening degree of the second shut-off valve and reduce the opening degree of the first shut-off valve until the third shut-off valve and the second shut-off valve are completely opened and the first shut-off valve is closed; during the process, maintain the burner in the kiln burning under slightly oxygen-deficient conditions, the non-condensable gas incinerator burning normally, and the pyrolysis gas pressure gauge showing a slightly positive pressure; The load reduction adjustment step includes: S2.

1. Stop the feeding action of the hydraulic piston pump; S2.

2. The partition rotary kiln continues to run at the rated speed until all the materials in the partition rotary kiln are discharged; The natural gas cut-off step includes: S3. Close the third flow regulating valve and the third shut-off valve, turn off the air blower, and turn off the burner in the kiln; The step of stopping the partition rotary kiln includes: S4.

1. Observe that the gas calorific value detected by the non-condensable gas gas analyzer drops to 0, turn on the air blower, turn on the fifth flow regulating valve, and let the outside cold air be transported from the burner in the kiln to the inside of the partition rotary kiln. When observing that the oxygen concentration detected by the non-condensable gas gas analyzer returns to 21%, the air blower can be turned off; S4.

2. Reduce the rotational speed of the partition rotary kiln until the partition rotary kiln drops to the safe shutdown temperature, and then the partition rotary kiln can be turned off.

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