CN113831925B - Reverse progressive organic solid waste pyrolysis device and method - Google Patents
Reverse progressive organic solid waste pyrolysis device and method Download PDFInfo
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- CN113831925B CN113831925B CN202111174573.2A CN202111174573A CN113831925B CN 113831925 B CN113831925 B CN 113831925B CN 202111174573 A CN202111174573 A CN 202111174573A CN 113831925 B CN113831925 B CN 113831925B
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 118
- 239000002910 solid waste Substances 0.000 title claims abstract description 29
- 230000000750 progressive effect Effects 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 17
- 239000007789 gas Substances 0.000 claims abstract description 51
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 43
- 239000003546 flue gas Substances 0.000 claims abstract description 43
- 230000005540 biological transmission Effects 0.000 claims abstract description 29
- 239000000463 material Substances 0.000 claims abstract description 26
- 239000007787 solid Substances 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 22
- 230000005855 radiation Effects 0.000 claims abstract description 19
- 210000000078 claw Anatomy 0.000 claims abstract description 14
- 238000002485 combustion reaction Methods 0.000 claims description 45
- 239000000047 product Substances 0.000 claims description 17
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 14
- 229910052799 carbon Inorganic materials 0.000 claims description 14
- 239000002994 raw material Substances 0.000 claims description 12
- 238000009833 condensation Methods 0.000 claims description 10
- 230000005494 condensation Effects 0.000 claims description 10
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 238000001035 drying Methods 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 7
- 239000012265 solid product Substances 0.000 claims description 7
- 239000000428 dust Substances 0.000 claims description 6
- 239000012263 liquid product Substances 0.000 claims description 6
- 229910000831 Steel Inorganic materials 0.000 claims description 5
- 239000010959 steel Substances 0.000 claims description 5
- 239000000446 fuel Substances 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 229910052760 oxygen Inorganic materials 0.000 claims description 3
- 239000001301 oxygen Substances 0.000 claims description 3
- 230000003014 reinforcing effect Effects 0.000 claims description 2
- 238000004140 cleaning Methods 0.000 abstract description 3
- 238000004321 preservation Methods 0.000 abstract description 2
- 230000003749 cleanliness Effects 0.000 abstract 1
- 239000002699 waste material Substances 0.000 description 10
- 239000012159 carrier gas Substances 0.000 description 4
- 239000000571 coke Substances 0.000 description 4
- 239000004033 plastic Substances 0.000 description 4
- 229920003023 plastic Polymers 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000010813 municipal solid waste Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 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 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention belongs to the technical field of organic solid waste disposal and utilization, and particularly relates to a reverse progressive pyrolysis device and method. The device comprises a hopper, a feeding system, a reverse progressive pyrolysis system, a product collecting system, a gas-solid separation system, a condensing system and a tail gas treatment system. The pyrolysis system comprises a pyrolysis chamber, a radiation heat exchange tube, a reverse rotating wheel, a conveying chain plate and a heat preservation layer. After the organic solid waste enters the reverse progressive pyrolysis reactor after being dried, the material is turned over by forward transmission of the transmission chain plate and reverse rotation of the reverse rotating wheel, so that the material is ensured to be uniformly heated and decomposed; the hook claw is arranged on the reversing rotating wheel, so that materials adhered to the rotating wheel and the chain plate are effectively removed, and the cleanliness and the running stability of the device are ensured; the generated pyrolysis gas is sent into a burner for burning, and high-temperature flue gas generated by burning is purified by a tail gas treatment system and is discharged after being used for pyrolysis heat supply and air preheating. The device can realize the efficient cleaning and safe disposal of organic solid waste.
Description
Technical Field
The invention belongs to the field of organic solid waste pyrolysis treatment, and particularly relates to a reverse progressive organic solid waste pyrolysis device and method.
Background
The source of organic solid waste such as household garbage, waste plastic, waste mask and the like is wide and numerous, has both pollution and resource attributes, and can cause improper treatmentWaste of resources and serious environmental pollution. At present, the main treatment modes of the organic solid waste comprise sanitary landfill, high-temperature incineration and the like. However, the sanitary landfill not only has large occupied area and has the problems of soil and water body damage caused by pollutant leakage, but also has low degradation speed, and is an unsustainable treatment mode. The high-temperature incineration can realize the rapid disposal of organic solid wastes, has better reduction effect, but easily generates a large amount of NO in the incineration process x 、SO x And the pollutants such as dioxin, fly ash and the like have large treatment difficulty and high environmental protection cost.
Pyrolysis is a technique in which organic matter is thermally decomposed under anaerobic or anoxic conditions to form liquid, gas, and solid products. The liquid product can be used as fuel or purifying chemical, the gas product can be used as synthetic gas or combustion for heat supply, and the solid product can be used for preparing functional carbon materials such as active carbon and the like, thereby being beneficial to the reduction, harmless and recycling of organic solid waste. At present, various pyrolysis reaction devices such as fixed beds, fluidized beds, rotating cones and the like have been developed at home and abroad and are mainly used for pyrolysis treatment of agricultural and forestry wastes, but are difficult to be suitable for heat-sensitive substances such as waste masks, waste plastics and the like. These substances are not only difficult to crush, but also easily soften and coke during pyrolysis, which seriously hinders the pyrolysis reaction and the stable operation of the device.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provides a reverse progressive organic solid waste pyrolysis device and method.
According to an aspect of the present invention, there is provided a reverse progressive organic solid waste thermal decomposition device, the device comprising:
the device comprises a hopper, a feeding system, a reverse progressive pyrolysis system, a product collection system, a gas-solid separation system, a condensation system, a combustion heating system and a tail gas treatment system; the reverse progressive pyrolysis system comprises a pyrolysis chamber, a radiation heat exchange tube, a reverse rotating wheel, a conveying chain plate and a heat preservation layer.
Wherein the pyrolysis chamber is a horizontal cuboid, a feed inlet is arranged at the upper left part of the pyrolysis chamber, a pyrolysis gas pipe is arranged right above the pyrolysis chamber, and a discharge outlet is arranged at the lower right part of the pyrolysis chamber; the radiation heat exchange tubes are distributed above the pyrolysis chamber and in the middle of the conveying chain plate; the reverse rotating wheel consists of a working rotating shaft and a rotating wheel disc and is positioned above the traditional chain plate and used for turning materials; the conveying chain plate consists of a driving wheel and a chain plate and is used for conveying materials.
The diameter of the rotating wheel disc is 400-1200 mm, and 6-12 hooks are arranged on the rotating wheel disc; the hook claws are radially distributed by taking the working rotating shaft as the center; the hook claw consists of a J-shaped steel plate with the thickness of 5-10 mm, a reinforcing rib is arranged on the hook claw, and the central angle corresponding to the circular arc at the tail end is 10-20 degrees; the diameter of the working rotating shaft (321) is 50-150 mm.
The outlet of the hopper is connected with the material inlet of the feeding system to convey organic solid waste; the material outlet of the feeding system is connected with the feeding port; the discharge port is connected with the inlet of a carbon collection box of the product collection system to discharge solid reaction products, and the pyrolysis gas pipe is used for conveying pyrolysis steam and is connected with the inlet of the condensation system through the gas-solid separation system; the lower part of the gas-solid separation system is connected with a carbon collection box to discharge solid products; a liquid outlet below the condensing system is connected with an inlet of an oil collector of the product collecting system to collect liquid products; the gas outlet above the condensing system is connected with the gas inlet of the combustion chamber in the combustion heating system to convey combustible gas; the outlet of the combustion chamber is connected with the inlet of the radiation heat exchange tube, and high-temperature flue gas is conveyed to supply heat for pyrolysis; the outlet of the radiation heat exchange tube is connected with an air preheater of the combustion heat exchange system, and secondary hot flue gas is input to preheat air required by combustion of the combustion chamber; the flue gas outlet of the air preheater is connected with the flue gas inlet of the feeding system, and is used for conveying low-temperature flue gas and drying materials; and a flue gas outlet of the feeding system is communicated with the tail gas purifying system to discharge cold flue gas. The air preheater is provided with an air inlet and an air outlet, wherein the air inlet is used for inputting cold air, and the air outlet is communicated with the combustion chamber to convey hot air to participate in combustion.
Preferably, the width of the pyrolysis chamber is 800-3000 mm, the width-to-length ratio is 1/6-1/9, and the aspect ratio is 1/1-2/1.
Preferably, the distance between the outer contour of the reversing rotary wheel and the transmission chain plate is not more than 10mm; the reverse rotating wheels are distributed at equal intervals along the length direction of the pyrolysis chamber, and the outer contour intervals of the front and rear reverse rotating wheels are not more than 10mm.
Preferably, the driving chain plate positively drives the material along the pyrolysis direction; the rotation direction of the reversing rotating wheel is opposite to the rotation direction of the transmission chain plate.
Preferably, the gas-solid separation system is at least one of a cyclone separator, a ceramic filter and a bag-type dust collector.
According to another aspect of the present invention, there is provided a method for implementing reverse progressive organic solid waste pyrolysis using the above apparatus, comprising the steps of:
s1, sending auxiliary fuel and hot air into a combustion chamber, and sending high-temperature flue gas generated by combustion into a radiation heat exchange tube to heat a pyrolysis chamber;
s2, organic solid waste enters a feeding system through a hopper, is dried by low-temperature flue gas at a flue gas outlet of an air preheater, and then enters a transmission chain plate of a reverse progressive pyrolysis system;
s3, driving a transmission chain plate and a reverse rotating wheel, fully pyrolyzing raw materials under the forward transmission of the transmission chain plate and the turning of the reverse rotating wheel, enabling generated solid products to enter a carbon collection box through a discharge hole, enabling pyrolysis gas to enter a gas-solid separation system through a pyrolysis gas pipe, and enabling separated dust to enter the carbon collection box;
s4, the purified pyrolysis gas enters a condensing system, liquid products generated by condensation enter an oil collector, and uncondensable combustible gas is sent into a combustion chamber to participate in combustion;
s5, secondary hot flue gas exhausted from a flue gas outlet of the radiation heat exchange pipe is input into a flue gas inlet of the air preheater to heat cold air, the hot air is conveyed to a combustion chamber to be used for combustion oxygen supply, low-temperature flue gas after heat exchange is input into a feeding system to dry and supply heat for raw materials, and cold flue gas exhausted from the feeding system is sent into a tail gas treatment system to be purified and then is exhausted.
As the preference of the step S3, the rotating speed of the reversing rotating wheel is 5-30 r/min, the conveying speed of the driving chain plate is 2-20 m/min, and the pyrolysis reaction temperature is 400-800 ℃.
As the optimization of the step S5, the temperature of the air preheated by the air preheater is 200-300 ℃, and the drying temperature of the feeding system is 150-200 ℃.
The core of the reverse progressive organic solid waste pyrolysis poly-generation device is a reverse progressive pyrolysis reactor, and the heat transfer process is strengthened through the forward rotation of the transmission chain plate and the reverse rotation of the reverse rotating wheel, so that the high-efficiency pyrolysis of the organic solid waste is promoted. The beneficial effects of the invention mainly include:
(1) The structure is compact: the forward transmission of the transmission chain plate and the reverse rotation of the rotating wheel are combined, so that the residence time of materials in the pyrolysis chamber can be effectively improved, the length of the transmission chain plate is shortened, the structure is more compact, and the occupied area is reduced.
(2) High pyrolysis efficiency: the reverse rotating wheel can effectively strengthen material turning, strengthen heat and mass transfer, avoid coking and agglomeration of materials and ensure full pyrolysis of the materials.
(3) The device self-cleans: the self-cleaning device can effectively scrape off materials stuck on the hook claw and the chain plate by controlling the distance between the reverse rotating wheels and the transmission chain plate, thereby realizing self-cleaning of the device, ensuring stable operation of equipment and prolonging the service life of the equipment.
(4) Energy cascade utilization: the non-condensable combustible gas is adopted to supply heat for the system, so that the heat supply requirement of material pyrolysis can be met, combustion air and dry materials can be preheated, and the gradient and high-efficiency utilization of high-temperature flue gas energy are realized.
(5) No carrier gas is required: the material is pyrolyzed by adopting the transmission chain plate, carrier gas is not needed, so that not only is energy loss caused by the preheating and cooling processes of the carrier gas avoided, but also the problem that the calorific value of combustible gas is low caused by the carrier gas is avoided.
(6) The usability of raw materials is strong: the method is widely applied to multi-source organic solid wastes such as household garbage, waste plastics, waste rubber, waste mask and the like, and raw materials can be directly pyrolyzed without being crushed, so that the raw material pretreatment cost is greatly reduced.
Drawings
FIG. 1 is a schematic view of the overall structure of the reverse progressive pyrolysis apparatus of the present invention.
Fig. 2 is a schematic diagram of the reverse progressive pyrolysis system of the present invention.
Reference numerals in the drawings:
1-a hopper;
2-a feed system;
3-a reverse progressive pyrolysis system;
31-a pyrolysis chamber; 311-a feed inlet; 312-pyrolyzing the gas pipe; 313-a discharge port; 32-reversing wheel; 321-working shaft; 322-rotating a wheel disc; 33-radiation heat exchange tubes; 34-a transfer flight; 341-a driving wheel; 342-link plate; 35-an insulating layer;
4-a product collection system;
41-a carbon collection box; 42-an oil collector;
5-a gas-solid separation system;
6-a condensing system;
7-a combustion heating system;
71-a combustion chamber; 72-an air preheater;
8-an exhaust gas treatment system.
Detailed Description
The invention provides a reverse progressive organic solid waste pyrolysis device and a reverse progressive organic solid waste pyrolysis method, and the invention is further described below with reference to specific embodiments.
Example 1
Referring to fig. 1-2, the invention provides a reverse progressive pyrolysis device, which comprises a hopper 1, a feeding system 2, a reverse progressive pyrolysis system 3, a product collecting system 4, a gas-solid separation system 5, a condensing system 6, a combustion heating system 7 and a tail gas treatment system 8. The reverse progressive pyrolysis system 3 comprises a pyrolysis chamber 31, a reverse rotating wheel 32, a radiation heat exchange tube 33, a conveying chain plate 34 and an insulating layer 35, wherein:
the pyrolysis chamber 31 is a horizontal cuboid, a feed inlet 311 is formed in the upper left part of the pyrolysis chamber, a pyrolysis gas pipe 312 is formed in the upper right part of the pyrolysis chamber, and a discharge outlet 313 is formed in the lower right part of the pyrolysis chamber; the radiation heat exchange tubes are distributed above the pyrolysis chamber 31 and in the middle of the conveying chain plate 34; the reversing rotary wheel 32 consists of a working rotary shaft 321 and a rotary wheel disc 322, and is positioned above the traditional chain plate 34 and used for turning materials; the conveying chain plate 34 consists of a driving wheel 341 and a chain plate 342 and is used for conveying materials;
the outlet of the hopper 1 is connected with the material inlet of the feeding system 2 to convey organic solid waste; the material outlet of the feeding system 2 is connected with a feeding hole 311; the discharge hole 313 is connected with the inlet of the carbon collection box 41 of the product collection system 4 to discharge solid reaction products, and the pyrolysis gas pipe 312 is used for conveying pyrolysis steam and is connected with the inlet of the condensation system 6 through the gas-solid separation system 5; the lower part of the gas-solid separation system 5 is connected with a carbon collection box 41 to discharge solid products; the liquid outlet below the condensing system 6 is connected with the inlet of the oil collector 42 of the product collecting system 4 to collect liquid product; the gas outlet above the condensing system 6 is connected with the gas inlet of the combustion chamber 71 in the combustion heating system 7 to deliver combustible gas; the outlet of the combustion chamber 71 is connected with the inlet of the radiation heat exchange tube 33, and high-temperature flue gas is conveyed to supply heat for pyrolysis; the outlet of the radiation heat exchange tube 33 is connected with an air preheater 72 of the combustion heat exchange system 7, and secondary hot flue gas is input to preheat air required by combustion of the combustion chamber 71; the flue gas outlet of the air preheater 72 is connected with the flue gas inlet of the feeding system 2, and is used for conveying low-temperature flue gas and drying materials; the flue gas outlet of the feeding system 2 is communicated with the tail gas purifying system 8 to discharge cold flue gas. The air preheater 72 is provided with an air inlet for cold air input and an air outlet communicating with the combustion chamber 71 for delivering hot air for combustion.
The gas-solid separation system 5 is a cyclone separator.
The drive link 34 positively drives the material in the pyrolysis direction; the reverse rotation wheel 32 rotates in the opposite direction to the drive link plate 34.
Referring to fig. 1-2, the organic solid waste pyrolysis method (also the working process of the device) implemented by the device of the invention comprises the following steps:
1. auxiliary fuel and hot air are sent into the combustion chamber 71, and high-temperature flue gas generated by combustion is sent into the radiation heat exchange tube 33 to heat the pyrolysis chamber 31;
2. the organic solid waste enters the feeding system 2 through the hopper 1, is dried by low-temperature flue gas at a flue gas outlet of the air preheater 72, and then enters the transmission chain plate 34 of the reverse progressive pyrolysis system 3;
3. the transmission chain plate 34 and the reverse rotating wheel 32 are driven, under the forward transmission of the transmission chain plate 34 and the turning of the reverse rotating wheel 32, raw materials are fully pyrolyzed, generated solid products enter the carbon collecting box 41 through the discharge hole 313, pyrolysis gas enters the gas-solid separation system 5 through the pyrolysis gas pipe 312, and separated dust enters the carbon collecting box 41;
4. the purified pyrolysis gas enters a condensing system 6, liquid products generated by condensation enter an oil collector 42, and non-condensable combustible gas is sent into a combustion chamber 71 to participate in combustion;
5. the secondary hot flue gas discharged from the flue gas outlet of the radiation heat exchange tube 33 is input into the flue gas inlet of the air preheater 72 to heat cold air, the hot air is conveyed to the combustion chamber 71 for combustion oxygen supply, the low-temperature flue gas after heat exchange is input into the feeding system 2 to dry and supply heat for raw materials, and the cold flue gas discharged from the feeding system 2 is sent into the tail gas treatment system 2 to be purified and then is exhausted.
Waste plastic with water content of 10% is used as a raw material, the width of the pyrolysis chamber 31 is 800mm, the width-to-length ratio is 1/6, the aspect ratio is 1/1, the thickness of the hook claw steel plate is 5mm, and the central angle corresponding to the circular arc at the tail end of the hook claw is 20 degrees; the diameter of the working rotating shaft is 50mm; the distance between the outer contour of the reversing wheel 32 and the transmission chain plate 34 is 6mm, and the distance between the outer contour of the front reversing wheel 32 and the outer contour of the rear reversing wheel 32 is 8mm; the rotating speed of the reversing rotating wheel 32 is 5r/min, the conveying speed of the transmission chain plate 34 is 2m/min, and the pyrolysis reaction temperature is 600 ℃; the temperature of the air preheated by the air preheater 72 is 300 ℃, and the drying temperature of the feeding system 2 is 200 ℃; the pyrolysis products are subjected to gas-solid separation and pyrolysis gas condensation to obtain coke, liquid and combustible gas three-phase pyrolysis products with respective yields of 12.0%,33.6% and 54.4%.
Example 2
Pyrolysis of organic solid waste was achieved using substantially the same apparatus as in example 1, and only the gas-solid separation system was changed to a ceramic filter.
Taking household garbage with water content of 20% as a raw material, wherein the width of a pyrolysis chamber 31 is 3000mm, the width-to-length ratio is 1/6, the aspect ratio is 1/2, the thickness of a hook claw steel plate is 10mm, and the central angle corresponding to the circular arc at the tail end of the hook claw is 10 degrees; the diameter of the working rotating shaft is 150mm; the distance between the outer contour of the reversing wheel 32 and the transmission chain plate 34 is 10mm, and the distance between the outer contour of the front reversing wheel 32 and the outer contour of the rear reversing wheel 32 is 10mm; the rotating speed of the reversing rotating wheel 33 is 30r/min, the conveying speed of the transmission chain plate 34 is 20m/min, and the pyrolysis reaction temperature is 400 ℃; the temperature of the air preheated by the air preheater 72 is 200 ℃, and the drying temperature of the feeding system 2 is 150 ℃; the pyrolysis products are subjected to gas-solid separation and pyrolysis gas condensation to obtain coke, liquid and combustible gas three-phase pyrolysis products with respective yields of 48.1%,40.6% and 11.3%.
Example 3
The pyrolysis of the organic solid waste was achieved by using substantially the same apparatus as in example 1, and only the gas-solid separation system was changed to a bag-type dust collector.
The waste mask with 15% of water content is used as a raw material, the width of the pyrolysis chamber 31 is 1000mm, the width-to-length ratio is 1/4, the aspect ratio is 1/1.5, the thickness of the hook claw steel plate is 8mm, and the central angle corresponding to the circular arc at the tail end of the hook claw is 15 degrees; the diameter of the working rotating shaft is 100mm; the distance between the outer contour of the reversing wheel 32 and the transmission chain plate 34 is 8mm, and the distance between the outer contour of the front reversing wheel 32 and the outer contour of the rear reversing wheel 32 is 10mm; the rotating speed of the reversing rotating wheel 33 is 15r/min, the conveying speed of the transmission chain plate 34 is 10m/min, and the pyrolysis reaction temperature is 800 ℃; the air temperature after the preheating of the air preheater 72 is 270 ℃, and the drying temperature of the feeding system 2 is 170 ℃; the pyrolysis products are subjected to gas-solid separation and pyrolysis gas condensation to obtain coke, liquid and combustible gas three-phase pyrolysis products with respective yields of 22.1%,27.3% and 50.6%.
Claims (8)
1. The reverse progressive organic solid waste pyrolysis device comprises a hopper (1), a feeding system (2), a reverse progressive pyrolysis system (3), a product collecting system (4), a gas-solid separation system (5), a condensing system (6), a combustion heating system (7) and a tail gas treatment system (8); the reverse progressive pyrolysis system (3) comprises a pyrolysis chamber (31), a reverse rotating wheel (32), a radiation heat exchange tube (33), a conveying chain plate (34) and an insulating layer (35), and is characterized in that:
the pyrolysis chamber (31) is a horizontal cuboid, a feed inlet (311) is formed in the upper left part of the pyrolysis chamber, a pyrolysis gas pipe (312) is formed in the right upper part of the pyrolysis chamber, and a discharge outlet (313) is formed in the lower right part of the pyrolysis chamber; the radiation heat exchange tubes (33) are distributed above the pyrolysis chamber (31) and in the middle of the conveying chain plate (34); the reversing rotating wheel (32) consists of a working rotating shaft (321) and a rotating wheel disc (322) and is positioned above the traditional chain plate (34); the conveying chain plate (34) consists of a driving wheel (341) and a chain plate (342);
the diameter of the rotating wheel disc (322) is 400-1200 mm, and 6-12 hooks are arranged on the rotating wheel disc; the hook claws are radially distributed by taking the working rotating shaft (321) as the center; the hook claw consists of a J-shaped steel plate with the thickness of 5-10 mm, a reinforcing rib is arranged on the hook claw, and the central angle corresponding to the circular arc at the tail end is 10-20 degrees; the diameter of the working rotating shaft (321) is 50-150 mm;
the outlet of the hopper (1) is connected with the material inlet of the feeding system (2); the material outlet of the feeding system (2) is connected with the feeding port (311); the discharge hole (313) is connected with an inlet of a carbon collection box (41) of the product collection system (4), and the pyrolysis gas pipe (312) is used for conveying pyrolysis steam and is connected with an inlet of the condensation system (6) through the gas-solid separation system (5); the lower part of the gas-solid separation system (5) is connected with the carbon collection box (41); a liquid outlet below the condensing system (6) is connected with an inlet of an oil collector (42) of the product collecting system (4); a gas outlet above the condensing system (6) is connected with a gas inlet of a combustion chamber (71) in the combustion heating system (7); the outlet of the combustion chamber (71) is connected with the inlet of the radiation heat exchange tube (33); the outlet of the radiation heat exchange tube (33) is connected with an air preheater (72) of the combustion heat exchange system (7); the flue gas outlet of the air preheater (72) is connected with the flue gas inlet of the feeding system (2); and a flue gas outlet of the feeding system (2) is communicated with the tail gas purifying system (8).
2. Pyrolysis apparatus according to claim 1, characterized in that the pyrolysis chamber (31) has a width of 800-3000 mm, a width-to-length ratio of 1/6-1/9 and an aspect ratio of 1/1-2/1.
3. Pyrolysis apparatus according to claim 1, characterized in that the distance between the outer contour of the reversing wheel (32) and the drive link plate (34) is not more than 10mm; the reversing rotating wheels (32) are distributed at equal intervals along the length direction of the pyrolysis chamber (31), and the outer contour intervals of the front reversing rotating wheel and the rear reversing rotating wheel (32) are not more than 10mm.
4. The pyrolysis apparatus according to claim 1, characterized in that the drive link plate (34) drives the material forward in the pyrolysis direction; the rotation direction of the reversing rotary wheel (32) is opposite to the rotation direction of the transmission chain plate (34).
5. Pyrolysis apparatus according to claim 1, characterized in that the gas-solid separation system (5) is at least one of a cyclone, a ceramic filter, a bag-type dust collector.
6. A method of pyrolysis of organic solid waste based on the pyrolysis apparatus of any one of claims 1 to 5, comprising the steps of:
s1, feeding auxiliary fuel and hot air into a combustion chamber (71), and feeding high-temperature flue gas generated by combustion into a radiation heat exchange tube (33) to heat a pyrolysis chamber (31);
s2, organic solid waste enters a feeding system (2) through a hopper (1), is dried by low-temperature flue gas at a flue gas outlet of an air preheater (72), and then enters a transmission chain plate (34) of a reverse progressive pyrolysis system (3);
s3, driving a transmission chain plate (34) and a reverse rotating wheel (32), fully pyrolyzing raw materials under the forward transmission of the transmission chain plate (34) and the turning of the reverse rotating wheel (32), enabling generated solid products to enter a carbon collection box (41) through a discharge hole (313), enabling pyrolysis gas to enter a gas-solid separation system (5) through a pyrolysis gas pipe (312), and enabling separated dust to enter the carbon collection box (41);
s4, the purified pyrolysis gas enters a condensing system (6), liquid products generated by condensation enter an oil collector (42), and non-condensable combustible gas is sent into a combustion chamber (71) to participate in combustion;
s5, secondary hot flue gas discharged from a flue gas outlet of the radiation heat exchange tube (33) is input into a flue gas inlet of the air preheater (72) to heat cold air, the hot air is conveyed to the combustion chamber (71) to be used for combustion oxygen supply, the low-temperature flue gas after heat exchange is input into the feeding system (2) to dry and supply heat for raw materials, and the cold flue gas discharged from the feeding system (2) is sent into the tail gas treatment system (2) to be purified and then is exhausted.
7. The pyrolysis method according to claim 6, wherein in the step S3, the rotational speed of the reversing wheel (32) is 5-30 r/min, the conveying speed of the driving link plate (34) is 2-20 m/min, and the reaction temperature of the pyrolysis is 400-800 ℃.
8. The pyrolysis method according to claim 6, wherein in the step S5, the air temperature after preheating by the air preheater (72) is 200-300 ℃, and the drying temperature of the feeding system (2) is 150-200 ℃.
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