CN113604233B - Tooth cage type multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof - Google Patents
Tooth cage type multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof Download PDFInfo
- Publication number
- CN113604233B CN113604233B CN202110777803.8A CN202110777803A CN113604233B CN 113604233 B CN113604233 B CN 113604233B CN 202110777803 A CN202110777803 A CN 202110777803A CN 113604233 B CN113604233 B CN 113604233B
- Authority
- CN
- China
- Prior art keywords
- reaction chamber
- pyrolysis
- stage
- organic solid
- cage
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 123
- 239000002910 solid waste Substances 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims abstract description 171
- 239000002994 raw material Substances 0.000 claims abstract description 37
- 238000011282 treatment Methods 0.000 claims abstract description 21
- 238000003756 stirring Methods 0.000 claims description 35
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 34
- 239000003546 flue gas Substances 0.000 claims description 34
- 238000002485 combustion reaction Methods 0.000 claims description 28
- 239000007789 gas Substances 0.000 claims description 20
- 239000002699 waste material Chemical group 0.000 claims description 16
- 239000007787 solid Substances 0.000 claims description 15
- 238000009826 distribution Methods 0.000 claims description 12
- 238000000746 purification Methods 0.000 claims description 10
- 239000012263 liquid product Substances 0.000 claims description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 7
- 230000009471 action Effects 0.000 claims description 5
- 238000005096 rolling process Methods 0.000 claims description 4
- 230000002708 enhancing effect Effects 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 230000003247 decreasing effect Effects 0.000 claims description 2
- 239000000126 substance Substances 0.000 abstract description 8
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 abstract description 6
- 230000009916 joint effect Effects 0.000 abstract 1
- 230000008569 process Effects 0.000 description 13
- 239000000047 product Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 238000012546 transfer Methods 0.000 description 5
- 230000008859 change Effects 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 238000005979 thermal decomposition reaction Methods 0.000 description 4
- 241000609240 Ambelania acida Species 0.000 description 3
- 239000010905 bagasse Substances 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000010813 municipal solid waste Substances 0.000 description 3
- 239000004033 plastic Substances 0.000 description 3
- 229920003023 plastic Polymers 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 239000013585 weight reducing agent Substances 0.000 description 3
- 239000000571 coke Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000011038 discontinuous diafiltration by volume reduction Methods 0.000 description 1
- 239000010791 domestic waste Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 238000009775 high-speed stirring Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 238000009270 solid waste treatment Methods 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/28—Other processes
- C10B47/30—Other processes in rotary ovens or retorts
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/02—Multi-step carbonising or coking processes
Abstract
The invention provides a tooth cage type multi-chamber organic solid waste pyrolysis reactor and a pyrolysis method thereof. The organic solid waste raw materials are continuously fed into a first-stage reaction chamber according to a certain feeding rate, and are uniformly heated and decomposed under the turning of a cage stirrer. The pyrolysis residues in each stage of reaction chambers are continuously pushed by the cage type stirrer, crushed by the joint action of the meshing teeth of the cage type stirrers of the adjacent reaction chambers at the connecting channel, automatically enter the next stage of reaction chambers for continuous pyrolysis, are discharged after being completely pyrolyzed in the last stage of reaction chambers, and the generated pyrolysis gas and residues can be further processed and utilized. The reactor is used for continuous pyrolysis of organic solid wastes under the anaerobic condition, so that harmful substances such as dioxin and the like can be effectively avoided, and harmless treatment of the organic solid wastes is realized.
Description
Technical Field
The invention belongs to the technical field of harmless treatment of organic solid wastes, and particularly relates to a tooth cage type multi-chamber organic solid waste pyrolysis reactor. The invention also provides a pyrolysis method using the tooth cage type multi-chamber organic solid waste pyrolysis reactor.
Background
Organic solid waste (organic solid waste) refers to solid organic matters which are generated in production, living or other activities and lose original utilization value or are discarded without losing the utilization value, and mainly comprises household garbage, sludge, waste plastics, waste rubber, agriculture and forestry waste and the like. With the rapid development of social economy in China, more and more organic solid wastes are generated in various fields of industry, agriculture, life and the like, so that a series of serious environmental pollution problems can be caused, and a large amount of resource waste can be caused. Therefore, the treatment of organic solid wastes has become a key problem related to the ecological civilization construction of China.
At present, the domestic treatment of organic solid waste still mainly depends on landfill or incineration treatment, and the problems of serious secondary pollution, resource waste and the like exist, and the method does not accord with the solid waste treatment development direction formulated by the country. Compared with the traditional mode, the pyrolysis method for treating the organic solid waste has the advantages of short treatment period, high conversion rate, obvious volume reduction effect, high-efficiency solidification of heavy metal and the like, and is a technology with great application and popularization prospects in the current organic solid waste recycling treatment technology. At present, pyrolysis technology for raw materials such as coal, biomass and the like is mature, but for general organic solid wastes such as household garbage, sludge and the like, the water content is large, the thermal conductivity is poor and fluctuates along with the change of weather, sources and the like, a pyrolysis device is required to have higher heat transfer performance and heat exchange efficiency, and most of the conventional pyrolysis devices are difficult to adapt; meanwhile, the components of the organic solid waste are extremely complex and have large fluctuation, and the pyrolysis device is required to be capable of rapidly adjusting the working condition; in addition, organic solid waste is heated and softened in the pyrolysis process and can be coked in large blocks, a certain crushing device or a device for preventing adhesion is needed, and the influence on heat exchange efficiency after the large blocks are adhered is avoided.
In the existing mainstream pyrolysis reactors, although the fixed bed reactor has the advantages of large treatment capacity and strong adaptability to organic solid wastes with different components and sizes, the fixed bed reactor has uneven heat transfer, is difficult to flexibly regulate and control pyrolysis conditions, and cannot overcome the problem of raw material adhesion; although the stirring reactor can achieve uniform pyrolysis by stirring the mixed materials, the stirring reactor also has the problems of low energy utilization rate and the like caused by intermittent operation, and the effect of avoiding raw material adhesion is poor only by high-speed stirring; while common continuous reactors, such as fluidized bed reactors, spiral reactors and the like, have good heat transfer effect and flexible reaction condition regulation, have strict requirements on components and sizes of organic solid wastes and have poor raw material adaptability. Therefore, development of a novel organic solid waste pyrolysis treatment device and a corresponding treatment process capable of overcoming the defects is an important research and development point in the field of organic solid waste pyrolysis at present.
Disclosure of Invention
The invention aims to solve the defects of low system efficiency, uneven heat transfer, poor raw material adaptability and the like of the traditional pyrolysis reaction device, and particularly solves the technical problems that caking and slagging in the organic solid waste pyrolysis process cannot be really realized, and the tooth cage type multi-chamber organic solid waste pyrolysis reactor and pyrolysis method are provided, so that the efficient and clean organic solid waste pyrolysis treatment can be realized.
In order to solve the technical problems, the embodiment of the invention provides a tooth-cage type multi-chamber organic solid waste pyrolysis reactor, which comprises a feed inlet, a flue gas outlet, a flue gas channel, a cage type stirrer, a reaction chamber, a discharge outlet, a flue gas inlet, a connecting channel and an air outlet pipe, wherein the cage type stirrer comprises a rotating shaft, a stirring frame, meshing teeth and stirring blades.
The reaction chambers of the whole pyrolysis reactor are of N levels, namely a first-level reaction chamber and a second-level reaction chamber … … Nth-level reaction chamber, each level reaction chamber is of a hollow horizontal cylindrical barrel structure, the reaction chambers are sequentially connected according to the level, can be obliquely or vertically arranged at a certain angle, and the sizes of the levels are sequentially decreased; adjacent two-stage reaction chambers are mutually overlapped, and the overlapped part is opened to form the connecting channel; each cage type stirrer is provided with a pair of rotating shafts, and extends into the reaction chamber along the two ends of the axis of the cylinder body of the reaction chamber respectively and is connected with the stirring frame; the stirring frame is provided with a disc structure with an outer contour clung to the inner wall of the reaction chamber at two ends of the axis of the cylinder of the reaction chamber, and the middle part of the stirring frame can be provided with holes; the meshing teeth are of plate-type convex tooth structures, a plurality of meshing teeth are outwards arranged on the outer side of the stirring frame along the radial direction and uniformly surround the whole circumference, the outer outline of each meshing tooth is clung to the inner wall of the corresponding reaction chamber, and the minimum distance between the meshing teeth of adjacent reaction chambers is continuously reduced along with the increase of the number of stages; at least one stirring blade can be connected to the middle of the stirring frame, the stirring blade is of a plate-type or pipe-type structure, at least one blade branch can be arranged on each blade, and the size of the stirring blade is reduced along with the increase of the stage number of the reaction chamber; outside the reaction chamber, each set of rotating shafts of the cage stirrers penetrate through the outer shell of the reactor and are connected with a driving device, the driving device drives all the cage stirrers to rotate, and the combination positions of the rotating shafts, the outer shell of the reactor and the reaction chamber are sealed by a sealing device; the flue is arranged in a space between the outer shell of the reactor and the reaction chamber, an adjustable air distribution plate is arranged in the flue, and ribs for enhancing heat exchange are arranged on the outer sides of the reaction chamber and the connecting channel; the upper end of the feed inlet is connected with the feed device, and the lower end of the feed inlet is connected with the opening position above the first-stage reaction chamber; the inlet of the air outlet pipe is connected to the upper part of each stage of reaction chamber or the connecting channel; the gas outlet pipes of each stage of the reaction chamber are connected to a combustion device or a condensing device for separating gas-liquid products after being converged; the discharge port is connected with the solid collecting device; the flue gas inlet is connected with the combustion device, and the flue gas outlet is connected with the purification device.
Preferably, the meshing teeth may be involute teeth, circular arc teeth or cycloidal teeth.
The embodiment of the invention also provides an organic solid waste pyrolysis method using the tooth cage type multi-chamber organic solid waste pyrolysis reactor, which comprises the following steps:
s1, high-temperature flue gas generated by a combustion device enters a flue through a flue gas inlet to heat each stage of reaction chamber; the low-temperature flue gas after heat exchange enters a purification device through a flue gas outlet, and is emptied after purification treatment; and adjusting air distribution plates in the flue so that the reaction chambers at all levels reach proper temperatures.
S2, organic solid waste raw materials in the feeding device pass through the cage stirrer through the feeding port and fall into the middle part of the first-stage reaction chamber at a certain feeding rate.
S3, the driving device drives the cage stirrer to rotate at a proper rotating speed, and organic solid waste raw materials in the reaction chamber are uniformly turned over; organic solid waste raw materials are heated and decomposed in a reaction chamber, and pyrolysis gas is generated and enters an air outlet pipe; the residues with higher pyrolysis degree at the near wall side of the reaction chamber are pushed into a connecting channel by a cage type stirrer, the residues are jointly meshed with the meshing teeth of the cage type stirrers of the adjacent reaction chambers at the position of the connecting channel and crushed by rolling action, then fall into the next-stage reaction chamber, and raw materials with lower pyrolysis degree at the middle part of the reaction chamber move to the near wall side for further pyrolysis; the pyrolysis residues sequentially repeat the process through each stage of reaction chamber, and the pyrolysis degree is continuously improved until the pyrolysis residues enter the reaction chamber of the last stage.
S4, after pyrolysis residues are completely pyrolyzed in the final stage reaction chamber, residual carbon residue and waste residues are discharged to a solid collecting device through a discharge hole.
S5, pyrolysis gas generated in each stage of reaction chamber is converged and properly dehydrated, and then is sent into a combustion device for combustion or is condensed to prepare a liquid product.
The tooth cage type multi-chamber organic solid waste pyrolysis reactor disclosed by the embodiment of the invention is characterized in that the multi-chamber continuous pyrolysis reactor is provided with a cage type stirrer capable of controlling the discharge amount through a rotating blade. After the solid waste raw materials enter the first-stage reaction chamber, the solid waste raw materials are turned by a cage stirrer to be heated and decomposed; the higher remainder of nearly wall side pyrolysis degree of reaction chamber promotes to get into the connecting channel via rotatory stirring vane, receives the common meshing of the meshing tooth of adjacent reaction chamber cage agitator in connecting channel position, rolls the effect and breaks, falls into the middle part of next level reaction chamber afterwards, and the lower raw materials of pyrolysis degree of original reaction chamber middle part then moves nearly wall side and further pyrolyzes. The pyrolysis residues sequentially enter the next-stage reaction chamber according to the steps, the pyrolysis degree is continuously improved until the pyrolysis of the last-stage reaction chamber is complete, and the continuous pyrolysis process is integrally realized; and finally, discharging the carbon residue and the waste residue to a solid collecting device, and sending the pyrolysis gas into an exhaust pipe for proper dehydration and further processing and utilization. The beneficial effects include:
1. the applicability of the raw material types is wide: can be suitable for organic solid wastes with various components and sizes without deep sorting and crushing of raw materials.
2. Multiple chambers are continuous, the space and heat utilization rate is high, and automatic discharging is carried out: the reaction chambers are connected, the sizes of the reaction chambers are sequentially reduced according to the increase of the number of stages, and the reaction chambers are suitable for the process that the raw materials in the reactor are heated and decomposed to be continuously reduced, and the heat and space utilization rate is high. Raw materials with higher pyrolysis degree at the near wall side of the reaction chamber automatically enter the next-stage reaction chamber in sequence under the pushing action of the stirrer, the pyrolysis degree is continuously improved until pyrolysis is complete in the last-stage reaction chamber, and raw materials with lower pyrolysis degree at the middle part of the reaction chamber are moved to the near wall side for further pyrolysis, so that the continuous pyrolysis process is integrally realized. The adjacent reaction chambers can be automatically discharged by using a cage stirrer, and a valve or other auxiliary devices are not needed, so that the structure is simple.
3. Even heated, easy to enlarge the treatment capacity: the reaction chamber is cylindrical barrel structure, improves throughput through increasing axial width easily to the cage agitator that the usable axial was rotated constantly stirs solid useless raw materials, strengthens the heat transfer, prevents to be heated unevenly and the pyrolysis that brings owing to the size enlarges.
4. Separate broken raw materials, prevent the large block from slagging: the meshing teeth are utilized to separate raw materials with higher pyrolysis degree on the near wall side, and simultaneously the meshing teeth of the adjacent reaction chambers at the connecting channel jointly mesh, roll and crush the raw materials, so that massive slagging is prevented, and the heat exchange efficiency of the raw materials is further improved.
5. The pyrolysis reaction condition is convenient to regulate and control, and the adaptability to the change of the organic solid waste components is strong: the working state of each reaction chamber in the pyrolysis reactor can be flexibly changed by adjusting the rotating speed of the cage type stirrer of each stage of reaction chamber, the temperature of flue gas generated by the burner and the position and angle of the air distribution plate outside each stage of reaction chamber in the flue so as to adapt to the change of the components of the organic solid waste raw materials under the influence of weather change, different sources and other factors.
6. Efficient recycling of products: the pyrolysis gas generated by the pyrolysis of the organic solid can be used for combustion to provide heat for the pyrolysis of the reactor, realize the self-heating pyrolysis process, or obtain a liquid product after condensation, and be used as liquid fuel or further prepare chemicals. The residue left after pyrolysis can be used for recycling in the mode of producing building materials after further combustion and other treatments.
7. Cleaning and discharging: the pyrolysis process of the organic solid waste raw material is an anaerobic process, and H can be generated 2 Reducing components such as CO, and the like, has low temperature and long residence time, can effectively inhibit the generation of harmful substances such as dioxin and the like from the source, and realizes the harmless treatment of organic solid waste.
Drawings
FIG. 1 is a schematic view of a tooth cage type multi-chamber organic solid waste hydrolysis reactor provided by an embodiment of the invention;
FIG. 2 is a schematic diagram of a cage mixer according to an embodiment of the present invention;
fig. 3 is a flowchart of the steps of the organic solid waste pyrolysis method according to the embodiment of the present invention.
[ description of the Main element symbols ]
1-a feed inlet; 2-a flue gas outlet; 3-reaction chamber; 4-cage stirrer; 5-flue; 6, a discharge hole; 7-a flue gas inlet; 8-an air outlet pipe; 9-connecting channels;
41-a rotation axis; 42-stirring rack; 43-engagement teeth; 44-stirring blades.
Detailed Description
In order to make the technical problems, technical solutions and advantages to be solved more apparent, the following detailed description will be given with reference to the accompanying drawings and specific embodiments.
Aiming at the existing problems, the invention provides the tooth cage type multi-chamber organic solid waste pyrolysis reactor and the pyrolysis method, which have the characteristics of wide raw material applicability, convenient pyrolysis regulation and control, high space and heat utilization rate, automatic discharge, easy discharge quantity adjustment, capability of separating broken raw materials, high resource utilization of products, clean discharge and the like, and can realize the continuous pyrolysis process of multiple reaction chambers.
In order to achieve the above technical solution, as shown in fig. 1 and fig. 2, the tooth-cage type multi-chamber organic solid waste pyrolysis reactor provided by the embodiment of the invention comprises a feed inlet 1, a flue gas outlet 2, a reaction chamber 3, a cage type stirrer 4, a flue 5, a discharge outlet 6, a flue gas inlet 7, an air outlet pipe 8 and a connecting channel 9, wherein the cage type stirrer 4 comprises a rotating shaft 41, a stirring frame 42, meshing teeth 43 and stirring blades 44.
The reaction chamber 3 of the whole pyrolysis reactor is provided with four stages, and is divided into a first stage reaction chamber, a second stage reaction chamber, a third stage reaction chamber and a fourth stage reaction chamber, wherein each stage reaction chamber is of a hollow horizontal cylindrical barrel structure; the reaction chambers are sequentially connected from the first stage to the fourth stage, and are vertically arranged as a whole; the width of the cylinder body of each stage of reaction chamber is 2500 mm, and the diameters are 900 mm, 700 mm, 500 mm and 300 mm respectively; adjacent reaction chambers are overlapped with each other, and the overlapped part is opened to form a connecting channel 9; a set of cage stirrers 4 are arranged in each stage of reaction chamber, each set of cage stirrers 4 is provided with a pair of rotating shafts 41, and the cage stirrers extend into the reaction chamber along the two ends of the axis of the cylinder of the reaction chamber respectively and are connected with a stirring frame 42; the stirring frame 42 has a disc structure with the thickness of 40 and mm at two ends of the axis of the reaction chamber, and the clearance between the outer contour and the inner wall of the reaction chamber is 5 mm; the meshing teeth 43 adopt an involute tooth structure, and the modulus is 16 mm; the outer contour of the meshing teeth 43 is tightly attached to the inner wall of the reaction chamber, and the minimum spacing between the meshing teeth 43 of adjacent reaction chambers is sequentially 10 mm, 6 mm and 3 mm along with the increase of the number of stages; a plate-type stirring blade 44 with the width of 40 and mm is connected to the middle part of the stirring frame 42, and blade branches with the width of 20 mm and the length of 20 mm are staggered at intervals of 200 mm along the stirring blade 44; outside the reaction chamber 3, the rotating shaft 41 of each set of the cage stirrers 4 passes through the outer shell of the reactor and is connected with a motor, the motor drives all the cage stirrers 4 to rotate, and the position where the rotating shaft 41 is combined with the outer shell of the reactor and the reaction chamber is sealed by a sealing device; the flue 3 is arranged in the space between the outer shell of the reactor and the reaction chamber 3, an adjustable air distribution plate is arranged in the flue 3, and ribs for enhancing heat exchange are arranged on the outer sides of the reaction chamber 3 and the connecting channel 9.
The upper end of the feed inlet 1 is connected with a feed device, and the lower end is connected with an opening position above the first-stage reaction chamber; the inlet of the air outlet pipe 8 is connected with the upper part of each stage of reaction chamber 3 or the connecting channel 9; after the gas outlet pipes 8 of the reaction chambers 3 at each stage are converged, the reaction chambers are connected to a combustion device or a condensing device for separating gas-liquid products; the discharge port 6 is connected with a solid collecting device; the flue gas inlet 7 is connected with the combustion device, and the flue gas outlet 2 is connected with the purification device.
In order to better realize the technical scheme, the invention also provides a pyrolysis method based on the tooth cage type multi-chamber organic solid waste pyrolysis reactor, which is shown in fig. 3, and comprises the following steps:
s1, high-temperature flue gas generated by a combustion device enters a flue through a flue gas inlet to heat each stage of reaction chamber; the low-temperature flue gas after heat exchange enters a purification device through a flue gas outlet, and is emptied after purification treatment; and adjusting air distribution plates in the flue so that the reaction chambers at all levels reach proper temperatures.
S2, organic solid waste raw materials in the feeding device pass through the clamp type stirrer through the feeding hole and fall into the middle part of the first-stage reaction chamber at a certain feeding rate.
S3, the driving device drives the cage stirrer to rotate at a proper rotating speed, and organic solid waste raw materials in the reaction chamber are uniformly turned over; organic solid waste raw materials are heated and decomposed in a reaction chamber, and pyrolysis gas is generated and enters an air outlet pipe; the residues with higher pyrolysis degree at the near wall side of the reaction chamber are pushed into a connecting channel by a cage type stirrer, the residues are jointly meshed with the meshing teeth of the cage type stirrers of the adjacent reaction chambers at the position of the connecting channel and crushed by rolling action, then fall into the next-stage reaction chamber, and raw materials with lower pyrolysis degree at the middle part of the reaction chamber move to the near wall side for further pyrolysis; the pyrolysis residues sequentially repeat the process through each stage of reaction chamber, and the pyrolysis degree is continuously improved until the pyrolysis residues enter the reaction chamber of the last stage.
S4, after pyrolysis residues are completely pyrolyzed in the fourth-stage reaction chamber, residual carbon residue and waste residues are discharged to a solid collecting device through a discharge hole.
S5, pyrolysis gas generated in each stage of reaction chamber is converged and properly dehydrated, and then is sent into a combustion device for combustion or is condensed to prepare a liquid product.
The specific operation steps are as follows:
before the organic solid waste pyrolysis reaction, firstly closing an inlet of a first-stage reaction chamber, and preheating the reaction chamber by utilizing high-temperature flue gas generated by a combustion device to flow through a flue; adjusting air distribution plates, opening an inlet of a first-stage reaction chamber after each reaction chamber reaches a required temperature, starting a feeding device and a driving motor, continuously feeding organic solid waste raw materials into the first-stage reaction chamber at a certain speed, uniformly heating and heating under the turning of a cage stirrer, and starting pyrolysis to generate pyrolysis gas; the residues with higher pyrolysis degree at the near wall side of the reaction chamber are pushed into a connecting channel by a cage type stirrer, the residues are jointly meshed with the meshing teeth of the cage type stirrers of the adjacent reaction chambers at the position of the connecting channel and crushed by rolling action, then fall into the next-stage reaction chamber, and raw materials with lower pyrolysis degree at the middle part of the reaction chamber move to the near wall side for further pyrolysis; the pyrolysis residues sequentially pass through the second-stage reaction chamber and the third-stage reaction chamber, and the pyrolysis degree is continuously improved until the pyrolysis is completed in the fourth-stage reaction chamber; the residual carbon residue and waste residue are discharged to a solid collecting device through a discharge hole for subsequent treatment and utilization; the generated pyrolysis gas can be sent to a combustion device for burning for heating a reactor after proper dehydration to realize self-heating pyrolysis, or sent to a condensing device for separating liquid products for being used as liquid fuel or further preparing chemicals; the low-temperature flue gas after heat exchange in the flue is processed by the purification device and then is exhausted.
The process flow of organic solid waste pyrolysis by using a tooth cage type multi-chamber organic solid waste pyrolysis reactor is described in detail below through specific examples, and devices with basically the same structure are adopted in each example.
Example 1
Firstly, the temperature of the first two-stage reaction chambers is maintained at 420 ℃ and the temperature of the second two-stage reaction chambers is maintained at 480 ℃ by adjusting the temperature of hot flue gas generated by a combustion device and an air distribution plate in a flue 5; then, the driving motor is regulated to maintain the rotating speed of the cage stirrer 4 in each stage of reaction chamber at 12 r/min; continuously feeding waste plastics into a reactor at a feed rate of 0.8 t/h by using a screw feeder as a feeding device, and continuously performing thermal decomposition in each stage of reaction chambers until pyrolysis in a fourth stage of reaction chambers is complete; after the generated pyrolysis gas is condensed and separated from a liquid phase product, the non-condensable gas is communicated to another catalytic reaction furnace at 600 ℃ for producing hydrogen; the liquid phase product is sent into a combustion device for combustion and is used for the self heat supply of the reactor; finally, the residue left is discharged through a discharge hole 6 and is collected in a solid collecting device. The whole device realizes continuous pyrolysis of waste plastics under the anaerobic condition, effectively suppresses generation and emission of harmful substances such as dioxin, has a weight reduction rate of 92.7w%, and realizes efficient harmless treatment.
Example 2
Firstly, the temperature of each stage of reaction chamber is maintained at 480 ℃ by adjusting the temperature of hot flue gas generated by a combustion device and an air distribution plate in a flue 5; the drive motor was then adjusted to maintain the rotational speed of the cage mixer 4 in each stage of reaction chamber at 7.5 r/min. Continuously feeding municipal domestic waste into a reactor at a feeding rate of 1 t/h by using a belt conveyor as a feeding device, and continuously performing thermal decomposition in each stage of reaction chambers until pyrolysis in a fourth stage of reaction chambers is complete; the generated pyrolysis gas is sent into a combustion device to be combusted after being dehydrated to a certain extent, and is used for the self heat supply of the reactor; finally, the residual waste residue and carbon residue are discharged through a discharge hole 6 and then are collected in a solid collecting device. The whole device realizes continuous pyrolysis of household garbage under anaerobic condition, effectively suppresses generation and emission of harmful substances such as dioxin, has a weight reduction rate of 83.6w%, and realizes efficient harmless treatment.
Example 3
Firstly, the temperature of the first three-stage reaction chamber is maintained at 550 ℃ and the temperature of the fourth-stage reaction chamber is maintained at 300 ℃ by adjusting the temperature of hot flue gas generated by a combustion device and an air distribution plate in a flue 5; then, the driving motor is regulated to maintain the rotating speed of the cage stirrer 4 in each stage of reaction chamber at 15 r/min; continuously feeding bagasse into a reactor at a feed rate of 0.4 t/h by using a screw feeder as a feeding device, and continuously performing thermal decomposition in each stage of reaction chambers until pyrolysis in a fourth stage of reaction chambers is complete; the generated pyrolysis gas is condensed to separate gas phase and liquid phase products, and finally the residual coke is discharged from a discharge hole 6 and is collected in a solid collecting device. Wherein, the non-condensable gas is dehydrated to a certain extent and then is sent into a combustion device together with the coke block to be burnt, so as to be used for the self heat supply of the reactor; the whole device realizes continuous pyrolysis of bagasse under the anaerobic condition, effectively suppresses generation and emission of harmful substances such as dioxin, and the yield of the obtained liquid-phase product can reach 30.2w%, thereby realizing efficient recycling of bagasse.
Example 4
Firstly, the temperature of each stage of reaction chamber is maintained at 400 ℃ by adjusting the temperature of hot flue gas generated by a combustion device and an air distribution plate in a flue 5; then, the driving motor is regulated to maintain the rotating speed of the cage stirrer 4 in each stage of reaction chamber at 6 r/min; continuously feeding the waste rubber into the reactor at a feeding rate of 0.6 t/h by using a belt conveyor as a feeding device, and continuously performing thermal decomposition in each stage of reaction chambers until the pyrolysis in the fourth stage of reaction chambers is complete; the generated pyrolysis gas is sent into a combustion device to be combusted after being dehydrated to a certain extent, and is used for the self heat supply of the reactor; finally, the residual waste residue and carbon residue are discharged through a discharge hole 6 and then are collected in a solid collecting device. The whole device realizes continuous pyrolysis of waste rubber under the anaerobic condition, effectively suppresses generation and emission of harmful substances such as dioxin, has the weight reduction rate reaching 79.7w%, and realizes efficient harmless treatment.
In the description of the present invention, the azimuth or positional relationship indicated by the terms "upper", "lower", "inner", "outer", etc., are based on the azimuth or positional relationship shown in the drawings, and are merely for convenience of description and simplification of the description, and are not indicative or implying that the apparatus or element in question must have a specific azimuth, be constructed and operated in a specific azimuth, and should not be construed as limiting the present invention; unless specifically stated or limited otherwise, the terms "connected," "communicating," and the like should be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present invention will be understood in specific cases by those of ordinary skill in the art.
Common sense of the above embodiments of the present invention, such as specific structures and features that are well known in the art, are not described in detail; the embodiments are described in a progressive manner, technical features related to the embodiments can be combined on the premise that the technical features do not form conflict with each other, and the same similar parts of the embodiments are mutually seen. It should be noted that it will be apparent to those skilled in the art that modifications and variations can be made without departing from the principles of the present invention, and such modifications and variations should also be considered to fall within the scope of the invention.
Claims (3)
1. A tooth cage type multi-chamber organic solid waste pyrolysis reactor comprises a feed inlet (1), a flue gas outlet (2), a reaction chamber (3), a cage type stirrer (4), a flue (5), a discharge port (6), a flue gas inlet (7), an air outlet pipe (8) and a connecting channel (9); the cage stirrer (4) comprises a rotating shaft (41), a stirring frame (42), meshing teeth (43) and stirring blades (44), and is characterized in that,
the reaction chamber (3) is divided into a first-stage reaction chamber, a second-stage reaction chamber and an Nth-stage reaction chamber, each stage reaction chamber is of a hollow horizontal cylindrical barrel structure, the reaction chambers are sequentially connected according to the number of stages and are arranged obliquely or vertically at a certain angle, and the size of each stage is sequentially decreased; adjacent two-stage reaction chambers are mutually overlapped, and the overlapped part is opened to form the connecting channel (9); each cage type stirrer (4) is arranged in each stage of reaction chamber, each cage type stirrer (4) is provided with a pair of rotating shafts (41), and the rotating shafts extend into the reaction chamber along the two ends of the axis of the cylinder of the reaction chamber respectively and are connected with the stirring frame (42); the stirring frame (42) is provided with a disc structure with an outer contour clung to the inner wall of the reaction chamber at two ends of the axis of the cylinder of the reaction chamber, and the middle part of the stirring frame is provided with a hole; the meshing teeth (43) are of plate-type convex tooth structures, a plurality of meshing teeth (43) are radially outwards arranged around the whole circumference on the outer side of the stirring frame (42) uniformly, the outer profile of each meshing tooth (43) is tightly attached to the inner wall of the corresponding reaction chamber, and the minimum distance between the meshing teeth (43) of adjacent reaction chambers is continuously reduced along with the increase of the number of stages; at least one stirring blade (44) is connected to the middle of the stirring frame (42), the stirring blade (44) is of a plate-type or pipe-type structure, at least one blade branch is arranged on each blade, and the size of the stirring blade (44) is reduced along with the increase of the stage number of the reaction chamber; outside the reaction chamber (3), a rotating shaft (41) of each set of the cage stirrer (4) penetrates through an outer shell of the reactor to be connected with a driving device, the driving device drives all the cage stirrers to rotate, and the combination positions of the rotating shafts (41) and the outer shell of the reactor as well as the reaction chamber are sealed by a sealing device; the flue (5) is arranged in a space between the outer shell of the reactor and the reaction chamber (3), an air distribution plate is arranged in the flue (5), and ribs for enhancing heat exchange are arranged on the outer sides of the reaction chamber (3) and the connecting channel (9);
the upper end of the feed inlet (1) is connected with the feed device, and the lower end of the feed inlet is connected with the opening position above the first-stage reaction chamber; the inlet of the air outlet pipe (8) is connected to the upper part of each stage of reaction chamber or the connecting channel (9); the gas outlet pipes (8) of each stage of reaction chamber are connected to a combustion device or a condensing device for separating gas-liquid products after being converged; the discharge port (6) is connected with a solid collecting device; the flue gas inlet (7) is connected with the combustion device, and the flue gas outlet (2) is connected with the purification device.
2. A pyrolysis reactor according to claim 1, wherein the meshing teeth (34) are involute, circular arc or cycloidal teeth.
3. A method of organic solid waste pyrolysis based on a tooth cage type multi-chamber organic solid waste pyrolysis reactor according to claim 1 or 2, comprising the steps of:
s1, high-temperature flue gas generated by a combustion device enters a flue through a flue gas inlet to heat each stage of reaction chamber; the low-temperature flue gas after heat exchange enters a purification device through a flue gas outlet, and is emptied after purification treatment; adjusting air distribution plates in the flue so that the reaction chambers at all levels reach the required temperature;
s2, organic solid waste raw materials in the feeding device pass through the cage stirrer through the feeding port and fall into the middle part of the first-stage reaction chamber;
s3, driving the cage stirrer by the driving device, and uniformly stirring the organic solid waste raw materials in the reaction chamber; organic solid waste raw materials are heated and decomposed in a reaction chamber, and pyrolysis gas is generated and enters an air outlet pipe; the residues with higher pyrolysis degree at the near wall side of the reaction chamber are pushed into a connecting channel by a cage type stirrer, the residues are jointly meshed with the meshing teeth of the cage type stirrers of the adjacent reaction chambers at the position of the connecting channel and crushed by rolling action, then fall into the next-stage reaction chamber, and raw materials with lower pyrolysis degree at the middle part of the reaction chamber move to the near wall side for further pyrolysis; the pyrolysis residues sequentially repeat the steps and pass through each stage of reaction chamber, and the pyrolysis degree is continuously improved until the pyrolysis residues enter the reaction chamber of the last stage;
s4, after pyrolysis residues are completely pyrolyzed in the final stage reaction chamber, residual carbon residue and waste residues are discharged to a solid collecting device through a discharge hole;
s5, pyrolysis gas generated in each stage of reaction chamber is converged and properly dehydrated, and then is sent into a combustion device for combustion or is condensed to prepare a liquid product.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110777803.8A CN113604233B (en) | 2021-07-09 | 2021-07-09 | Tooth cage type multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110777803.8A CN113604233B (en) | 2021-07-09 | 2021-07-09 | Tooth cage type multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113604233A CN113604233A (en) | 2021-11-05 |
| CN113604233B true CN113604233B (en) | 2024-02-02 |
Family
ID=78304274
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110777803.8A Active CN113604233B (en) | 2021-07-09 | 2021-07-09 | Tooth cage type multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113604233B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113604232B (en) * | 2021-07-09 | 2024-02-02 | 华北电力大学 | Rotary cage type multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof |
| CN113604234B (en) * | 2021-07-09 | 2024-02-02 | 华北电力大学 | Multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof |
| CN115948172B (en) * | 2022-12-29 | 2024-04-09 | 中国科学院广州能源研究所 | Device and method for preparing clean synthetic gas by organic solid waste pyrolysis-chemical chain reforming |
Citations (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB8410129D0 (en) * | 1984-04-18 | 1984-05-31 | Exxon Research Engineering Co | Calcined coke |
| JPH11128878A (en) * | 1997-11-05 | 1999-05-18 | Mitsui Eng & Shipbuild Co Ltd | Thermal decomposition reactor for waste treating device |
| CN101903505A (en) * | 2007-04-27 | 2010-12-01 | 学校法人近畿大学 | Biocoke producing apparatus and process |
| CN101985562A (en) * | 2010-08-19 | 2011-03-16 | 西峡龙成特种材料有限公司 | Horizontal coal separating equipment with multiple combustors |
| JP2012097202A (en) * | 2010-11-02 | 2012-05-24 | Iwamoto:Kk | Carbonization furnace |
| FR2982274A1 (en) * | 2011-11-09 | 2013-05-10 | Commissariat Energie Atomique | BIOMASS TORREFACTION AND GRINDING REACTOR, BIOMASS TREATMENT SYSTEM AND PLANT INCORPORATING SUCH REACTOR, ASSOCIATED METHOD |
| GB201503772D0 (en) * | 2015-03-05 | 2015-04-22 | Standard Gas Ltd | Temperature profile in an advanced thermal treatment apparatus and method |
| CN104910929A (en) * | 2014-03-14 | 2015-09-16 | 上海金匙环保科技股份有限公司 | Domestic garbage pyrolysis treatment device and system |
| WO2016049326A1 (en) * | 2014-09-24 | 2016-03-31 | Intellergy, Inc. | Compact and maintainable waste reformation apparatus |
| CN105505416A (en) * | 2015-12-18 | 2016-04-20 | 江苏鼎新环保科技有限公司 | Zoned-temperature-control rotary continuous pyrolyzing and carbonizing device for biomass |
| CN108431182A (en) * | 2015-11-04 | 2018-08-21 | 哈夫纳能源公司 | The equipment thermally decomposed stage by stage |
| CN108587671A (en) * | 2018-05-21 | 2018-09-28 | 华北电力大学 | A kind of apparatus and method of biomass quick catalysis pyrolysis |
| CN111534311A (en) * | 2020-04-01 | 2020-08-14 | 华北电力大学 | Double-chamber organic solid waste pyrolysis device and method |
| CN212179681U (en) * | 2020-03-25 | 2020-12-18 | 武汉方特工业设备技术有限公司 | Riser heat exchanger with integrated multipoint and multiwall layer temperature monitoring and monitoring functions |
| CN212741236U (en) * | 2020-05-26 | 2021-03-19 | 汕头市谷源新能源有限公司 | Pyrolysis device for low-temperature easily-melted organic material |
| CN113604234A (en) * | 2021-07-09 | 2021-11-05 | 华北电力大学 | Multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof |
| CN113604232A (en) * | 2021-07-09 | 2021-11-05 | 华北电力大学 | Rotary cage type multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7951271B2 (en) * | 2006-06-12 | 2011-05-31 | David Brent Thompson | System for recovering oil from used automobile tires |
-
2021
- 2021-07-09 CN CN202110777803.8A patent/CN113604233B/en active Active
Patent Citations (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB8410129D0 (en) * | 1984-04-18 | 1984-05-31 | Exxon Research Engineering Co | Calcined coke |
| JPH11128878A (en) * | 1997-11-05 | 1999-05-18 | Mitsui Eng & Shipbuild Co Ltd | Thermal decomposition reactor for waste treating device |
| CN101903505A (en) * | 2007-04-27 | 2010-12-01 | 学校法人近畿大学 | Biocoke producing apparatus and process |
| CN101985562A (en) * | 2010-08-19 | 2011-03-16 | 西峡龙成特种材料有限公司 | Horizontal coal separating equipment with multiple combustors |
| JP2012097202A (en) * | 2010-11-02 | 2012-05-24 | Iwamoto:Kk | Carbonization furnace |
| FR2982274A1 (en) * | 2011-11-09 | 2013-05-10 | Commissariat Energie Atomique | BIOMASS TORREFACTION AND GRINDING REACTOR, BIOMASS TREATMENT SYSTEM AND PLANT INCORPORATING SUCH REACTOR, ASSOCIATED METHOD |
| CN104910929A (en) * | 2014-03-14 | 2015-09-16 | 上海金匙环保科技股份有限公司 | Domestic garbage pyrolysis treatment device and system |
| WO2016049326A1 (en) * | 2014-09-24 | 2016-03-31 | Intellergy, Inc. | Compact and maintainable waste reformation apparatus |
| GB201503772D0 (en) * | 2015-03-05 | 2015-04-22 | Standard Gas Ltd | Temperature profile in an advanced thermal treatment apparatus and method |
| CN108431182A (en) * | 2015-11-04 | 2018-08-21 | 哈夫纳能源公司 | The equipment thermally decomposed stage by stage |
| CN105505416A (en) * | 2015-12-18 | 2016-04-20 | 江苏鼎新环保科技有限公司 | Zoned-temperature-control rotary continuous pyrolyzing and carbonizing device for biomass |
| CN108587671A (en) * | 2018-05-21 | 2018-09-28 | 华北电力大学 | A kind of apparatus and method of biomass quick catalysis pyrolysis |
| CN212179681U (en) * | 2020-03-25 | 2020-12-18 | 武汉方特工业设备技术有限公司 | Riser heat exchanger with integrated multipoint and multiwall layer temperature monitoring and monitoring functions |
| CN111534311A (en) * | 2020-04-01 | 2020-08-14 | 华北电力大学 | Double-chamber organic solid waste pyrolysis device and method |
| CN212741236U (en) * | 2020-05-26 | 2021-03-19 | 汕头市谷源新能源有限公司 | Pyrolysis device for low-temperature easily-melted organic material |
| CN113604234A (en) * | 2021-07-09 | 2021-11-05 | 华北电力大学 | Multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof |
| CN113604232A (en) * | 2021-07-09 | 2021-11-05 | 华北电力大学 | Rotary cage type multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof |
Non-Patent Citations (1)
| Title |
|---|
| 羰基合成反应搅拌器故障诊断与处理;李欣;高常春;刘洪刚;;齐鲁石油化工(02);36-43 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN113604233A (en) | 2021-11-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN113604233B (en) | Tooth cage type multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof | |
| CN104028547B (en) | Municipal solid waste extreme decrement and highly resourceful treatment process and municipal solid waste extreme decrement and highly resourceful treatment device | |
| CN113604232B (en) | Rotary cage type multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof | |
| CN201593035U (en) | Gas production device using spiral dry distillation and decomposition of biomass | |
| CN113604234B (en) | Multi-chamber organic solid waste pyrolysis reactor and pyrolysis method thereof | |
| CN104804775A (en) | Method and system for producing combustible gas from domestic waste through pyrolysis gasification | |
| CN111534311B (en) | Double-chamber organic solid waste pyrolysis device and method | |
| CN111040791A (en) | Organic garbage pyrolysis device and organic garbage pyrolysis treatment method | |
| CN111561700A (en) | Rotary rake type organic solid waste pyrolysis device and pyrolysis method | |
| CN105737163A (en) | Household garbage internal circulation sealed low-temperature pyrolysis system and method based on decoupling combustion | |
| CN110066083B (en) | Sludge pyrolysis recycling system and pyrolysis method | |
| CN114308988B (en) | Skid-mounted medical waste isothermal pyrolysis treatment system | |
| CN211367362U (en) | Sludge cracking treatment device | |
| CN111440707A (en) | Dry type anaerobic fermentation treatment system for mixed garbage | |
| CN204607940U (en) | The system of combustible gas is produced in domestic garbage pyrolysis gasification | |
| WO2022067882A1 (en) | System and process of industrial continuous cracking of mixed waste plastics according to class | |
| CN201288111Y (en) | Apparatus for treating sewage sludge and/or waste slag | |
| CN211119364U (en) | Domestic waste fast pyrolysis device | |
| CN210151029U (en) | Device for pyrolyzing biogas residues and preparing phenol compounds by using molten salt | |
| CN111718095A (en) | Municipal sludge pyrolysis carbonization treatment system and treatment process | |
| CN115651717A (en) | Alternate pyrolysis gasification device and method | |
| CN211367361U (en) | Multidimensional and tubular sludge cracking device | |
| CN210163375U (en) | Container type small-sized pyrolysis device for organic solid wastes such as household garbage | |
| CN210595928U (en) | Device that catalyst can be palingenetic microwave-assisted catalysis pyrolysis domestic waste fast | |
| CN209508146U (en) | A kind of pyrolysis system of solid waste containing organic matter |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |