CN113136230A - Garbage pyrolysis process system - Google Patents
Garbage pyrolysis process system Download PDFInfo
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- CN113136230A CN113136230A CN202010052544.8A CN202010052544A CN113136230A CN 113136230 A CN113136230 A CN 113136230A CN 202010052544 A CN202010052544 A CN 202010052544A CN 113136230 A CN113136230 A CN 113136230A
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- heat carrier
- fluidized bed
- pyrolysis
- solid heat
- garbage
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- 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
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- 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
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
- C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
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- 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
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
- C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
- C10B49/22—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique
Abstract
The invention belongs to the technical field of garbage treatment, and particularly relates to a garbage pyrolysis process system. The solid heat carrier feeding hopper is positioned above the solid heat carrier feeding device, the solid heat carrier feeding device is connected with the circulating fluidized bed feeding port, and the heat carrier receiving bin is positioned above the solid heat carrier feeding device; an outlet of the solid heat carrier feeding device is connected with an inlet of a heat carrier of the fluidized bed furnace, a return port at the bottom of the fluidized bed furnace is connected with an inlet of the solid heat carrier return device, and an outlet of the solid heat carrier return device is connected to the circulating fluidized bed; the upper part of the circulating fluidized bed is provided with a high-temperature flue gas cyclone separator, the lower part of the circulating fluidized bed is provided with an air blower, a flue gas secondary cyclone separator is connected with the high-temperature flue gas cyclone separator, the high-temperature flue gas cyclone separator is arranged above a heat carrier receiving bin, and a garbage feeding hopper is positioned above a garbage feeding device. Can realize the fast pyrolysis of garbage to generate high-quality pyrolysis products and realize the large-scale pyrolysis reaction.
Description
Technical Field
The invention belongs to the technical field of garbage treatment, and particularly relates to a garbage pyrolysis process system.
Background
At present, the phenomenon of city enclosing of garbage in China is more and more serious along with the development of urban economy, and the garbage incineration technology is widely applied to large and medium-sized cities in China by virtue of the advantages of reduction and high resource utilization degree. However, the disposal of the domestic waste by incineration inevitably generates dioxin. Dioxin control has become one of the biggest limiting factors for popularizing waste incineration disposal technology. The incineration fundamentally and difficultly strictly controls the emission of dioxin and heavy metals, and zero emission engineering is advocated in all countries in the world, especially the near zero emission of dioxin substances, so that a new technical garbage pyrolysis technology is urgently needed in the market.
The garbage pyrolysis technology means that larger cellulose, lignin, hemicellulose, plastics and other components in the garbage are cracked in a heating environment to generate small gaseous molecules such as CO, CO2, H2O, CH4 and the like, tar and residual carbon. The present pyrolysis technique is classified with the heating methods and can be divided into indirect heating and direct heating, indirect heating is mainly in order to introduce the high temperature flue gas that the fuel burning produced into pyrolysis reactor jacket or directly burn in outer jacket, realize the heat-conduction through heating pyrolysis reactor inner wall and provide the required heat of rubbish pyrolysis, the thermal transmission of this mode is only realized at pyrolysis gas inner wall, thereby make this kind of mode pyrolysis reaction handling capacity not big, pyrolysis reactor size is big simultaneously, mainly regard the jacket rotary kiln as the representative. The direct heating includes gas heat carrier heating and solid heat carrier heating. The gas heat carrier heating mainly uses high-temperature hot flue gas generated by fuel combustion to be directly introduced into the pyrolysis reactor and directly contacted with pyrolysis materials, mainly represented by a rotary kiln and a fixed bed, the mode cannot obtain high-quality pyrolysis gas, and the dedusting load of the system is large. The solid heat carrier is heated by taking some external quartz sand, ceramic balls or ash or semicoke generated by the solid heat carrier as a heat carrier to be in direct contact with materials, so that the heat exchange efficiency is extremely high, and meanwhile, the quality of pyrolysis gas is high. The double-tower fluidized pyrolysis is a typical mode in the solid heat carrier heating technology, namely the pyrolysis process and the combustion process are separately carried out in two fluidized beds, the heat emitted by combustion can be utilized to balance the heat required by the pyrolysis reaction, and the condition that the synthesis gas produced by a pyrolysis reactor is diluted is avoided, so that high-calorific-value gas, carbon and oil are finally produced, and therefore attention is paid. However, the processing scale of the double-tower fluidized bed technology is not large and is basically below 200t/d, the difference from the current incineration processing capacity of a grate furnace is large, and the double-tower fluidized bed technology is a bottleneck for large-scale popularization of the pyrolysis technology at home and abroad. For the fluidized pyrolysis technology, another disadvantage is that the dust content of the produced pyrolysis oil gas is large, the tar component of the pyrolysis product is complex, the tar mist formed along with the reduction of the temperature of the pyrolysis gas contains a large amount of liquid drops with the diameter of less than 1 μm, and the tar mist is easy to bond and condense with water, coke, dust and the like to form a sticky liquid substance, so that the stability and the safe operation of equipment are influenced.
The invention provides a different combination pyrolysis process of a garbage fluidized bed and a circulating fluidized bed, which solves the problem that the conventional garbage pyrolysis device cannot realize large-scale production on the basis of continuing using a solid heat carrier heating technology, is 2-3 times of the processing capacity of the common garbage pyrolysis device, simultaneously adopts pyrolysis gas as a fluidized medium for pyrolysis of a fluidized bed furnace, ensures the high quality of the pyrolysis gas, and ensures that the cyclone dust removal is arranged in the fluidized bed furnace to maintain the high-temperature environment of a dust removal device, thereby solving the problem that pyrolysis tar and dust block a subsequent system in the subsequent process.
Disclosure of Invention
The invention aims to provide a garbage pyrolysis process system, which can realize quick pyrolysis of garbage to generate high-quality pyrolysis products, can realize large-scale pyrolysis reaction, and simultaneously solves the problem that pyrolysis tar and dust block a subsequent system in the pyrolysis process.
In order to achieve the purpose, the invention comprises a fluidized bed, a circulating fluidized bed, a garbage feeding hopper, a garbage feeding device, a solid heat carrier feeding hopper, a solid heat carrier feeding device, a high-temperature flue gas cyclone separator, a heat carrier receiving bin, a heat carrier feeding device, a solid heat carrier returning device, a cyclone separator, a tar separator, a flue gas secondary cyclone separator, a pyrolysis gas induced draft fan, an air blower and a fluidized bed separator.
The solid heat carrier feeding hopper is positioned above the solid heat carrier feeding device, the solid heat carrier feeding device is connected with a feeding port of the circulating fluidized bed, and the heat carrier receiving bin is positioned above the solid heat carrier feeding device; an outlet of the solid heat carrier feeding device is connected with an inlet of a heat carrier of the fluidized bed furnace, a return port at the bottom of the fluidized bed furnace is connected with an inlet of the solid heat carrier return device, and an outlet of the solid heat carrier return device is connected to the circulating fluidized bed; the upper part of the circulating fluidized bed is provided with a high-temperature flue gas cyclone separator, the lower part of the circulating fluidized bed is provided with a blower, a flue gas secondary cyclone separator is connected with the high-temperature flue gas cyclone separator, the high-temperature flue gas cyclone separator is arranged above a heat carrier receiving bin, a garbage feeding hopper is positioned above a garbage feeding device, and the garbage feeding device is connected with a fluidized bed furnace; the cyclone separator is positioned at the upper part of the fluidized bed furnace; the cyclone separator is connected with the tar separator, and the lower part of the circulating fluidized bed is connected with the fluidized bed and the pyrolysis gas induced draft fan.
Organic garbage particles and a high-temperature solid heat carrier in the fluidized bed furnace form a certain bed thickness under the fluidization effect of a fluidizing medium, the garbage particles and the solid heat carrier are fully heated, mixed and pyrolyzed, organic matters are pyrolyzed at 500-1000 ℃ due to thermal instability to generate pyrolysis oil gas and garbage carbon, the high-temperature pyrolysis oil gas generated by pyrolysis enters a cyclone separator and a tar separator after being dedusted at the top, part of the separated pyrolysis gas is sent back to the fluidized bed furnace by a pyrolysis gas induced draft fan to serve as the fluidizing medium, the other part of the separated pyrolysis gas is used as supplementary fuel and is supplied to a circulating fluidized bed to be combusted in the circulating fluidized bed to heat the solid heat carrier to 600-1100 ℃, heat required by pyrolysis reaction in the fluidized bed furnace is provided, and the pyrolysis gas with excessive heat can be sold after being purified.
The circulating fluidized bed burns and produces high temperature flue gas and carries solid heat carrier and realize gas-solid separation through high temperature flue gas cyclone, and high temperature flue gas can send to follow-up system after flue gas secondary cyclone removes dust and carry out waste heat recovery, and the high temperature solid heat carrier that separates gets off gets into heat carrier and accepts storehouse buffer memory, and solid heat carrier feed arrangement sends the high temperature solid heat carrier in the heat carrier accepts the storehouse into the fluidized bed furnace as the raw materials of rubbish pyrolytic reaction. And after pyrolysis is finished, the cooled solid heat carrier and the generated residual carbon are sent into the circulating fluidized bed through the solid heat carrier returning device to heat the solid heat carrier, so that the circulation of heating, pyrolysis and heating of the solid heat carrier in the system is realized.
The solid heat carrier feeding device and the solid heat carrier returning device can be of a mechanical spiral feeding structure or a U-shaped and L-shaped airflow feeding structure, and the garbage feeding device and the solid heat carrier supplementing device are of mechanical spiral feeding structures.
The distribution direction of the solid heat carrier can be in a parallel direction or a series direction.
The parallel distribution direction of the solid heat carrier is sequentially set to be a circulating fluidized bed, a high-temperature flue gas cyclone separator, a common heat carrier receiving bin, 1-3 branch heat carrier feeding devices, 1-3 fluidized beds and 1-3 branch heat carrier returning devices.
Furthermore, the circulating fluidized bed and the common heat carrier receiving bin are used by 1-3 fluidized beds, and each fluidized bed is matched with a corresponding garbage feeding hopper and a garbage feeding device, and a corresponding solid heat carrier feeding device and a solid heat carrier returning device. The common heat carrier receiving bin is positioned above 1-3 branch heat carrier feeding devices, an outlet of each solid heat carrier feeding device is connected with an inlet of a corresponding fluidized bed furnace heat carrier, a bottom return port of each fluidized bed furnace is connected with an inlet of the corresponding solid heat carrier returning device, and 1-3 branch heat carrier returning devices are connected to the circulating fluidized bed;
the 1-3 boiling furnaces are arranged around the common heat carrier receiving bin at a certain angle, the cross section area of each boiling furnace is circular or quadrangular, the arrangement is mainly determined by the implementation of field arrangement,
the series direction is sequentially set into a circulating fluidized bed, a high-temperature flue gas cyclone separator, a heat carrier receiving bin, a heat carrier feeding device, a fluidized bed furnace (the fluidized bed furnace is divided into two boiling chambers, a partition plate is arranged between the two boiling chambers, and small holes or gaps are arranged on the partition plate), and a heat carrier returning device, as shown in fig. 4.
Further, pyrolysis gas generated in the first boiling chamber carries the solid heat carrier to enter the boiling furnace through the small holes or gaps of the partition plates of the boiling furnace, and garbage carbon which is not pyrolyzed continues to be subjected to high-speed mixing pyrolysis in the second boiling chamber. Two boiling chambers of the fluidized bed furnace are connected in series to operate, so that the retention time of the garbage pyrolysis reaction is prolonged, and the quality of pyrolysis products is further improved.
The top of the fluidized bed furnace is provided with 2-4 internal dust removal devices connected in parallel, so that the problems that pyrolysis tar and dust are mixed to cause system blockage due to local low temperature of the system and the separated dust is blocked in a caking mode in the conveying process and needs to be transported and disposed under the condition that the dust removal devices are arranged externally in a traditional device are solved, the separated dust returns to the fluidized bed furnace, the system flow is greatly simplified, and the risk of stable operation of the system is reduced.
The fluidized bed furnace adopts the pyrolysis gas after tar separation as the fluidized medium in the fluidized bed furnace, thereby avoiding other gases as the fluidized medium and greatly reducing the heat value of the pyrolysis gas.
The beneficial effects obtained by the invention are as follows:
the invention provides a pyrolysis process combining fluidized bed combustion and a fluidized bed furnace, which can realize the fast pyrolysis of garbage to generate high-quality pyrolysis products, can realize the large-scale pyrolysis reaction, and simultaneously solves the problem that pyrolysis tar and dust block a subsequent system in the pyrolysis process.
Drawings
FIG. 1 is a schematic view A of a process system for pyrolysis of waste;
FIG. 2 is a schematic view B of a process system for pyrolysis of waste;
FIG. 3 is a schematic diagram C of a parallel arrangement of a refuse pyrolysis process;
FIG. 4 is a schematic view D of a series arrangement of a refuse pyrolysis process;
in the figure: 1. fluidized bed furnaces (a-c); 2. circulating fluidized bed; 3. garbage feed hoppers (a-c); 4. garbage feeding devices (a-c); 5. a solid heat carrier replenishing hopper; 6. a solid heat carrier feeding device; 7. a high temperature flue gas cyclone separator; 8. a heat carrier receiving bin; 9. heat carrier feeding devices (a-c); 10. solid heat carrier material returning devices (a-c); 11. cyclone separators (a-c); 12. a tar separator; 13. a secondary flue gas cyclone separator; 14. a pyrolysis gas induced draft fan; 15. a blower; 100. a partition plate of a fluidized bed furnace.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments.
Fig. 1 and 2 show a garbage pyrolysis process system combining fluidized bed combustion and fluidized bed pyrolysis, which comprises 1-3 fluidized beds (1 a-1 c), a circulating fluidized bed 2, 1-3 branch heat carrier feeding devices (3 a-3 c), 1-3 garbage feeding devices (4 a-4 c), a solid heat carrier replenishing hopper 5, a solid heat carrier replenishing device 6, 1 high-temperature flue gas separator 7, 1 heat carrier receiving bin 8, 1-3 branch heat carrier feeding devices (9 a-9 c), 1-3 branch heat carrier returning devices (10 a-10 c), a cyclone separator 11, a tar separator 12, a flue gas secondary cyclone separator blower 13, a pyrolysis gas induced draft fan 14, 15 and a fluidized bed separator 100.
The solid heat carrier feeding hopper 5 is positioned above the solid heat carrier feeding device 6, the solid heat carrier feeding device 6 is connected with a feeding port of the circulating fluidized bed 2, and the solid heat carrier existing in the solid heat carrier feeding hopper 5 is added into the circulating fluidized bed 2 by the heat carrier feeding device 6. The heat carrier receiving bin 8 is positioned above the solid heat carrier feeding devices (9 a-9 c), and the heat carrier feeding devices (9 a-9 c) are connected with the heat carrier receiving bin 8 at a certain angle; outlets of the solid heat carrier feeding devices (9 a-9 c) are connected with heat carrier inlets of the fluidized beds (1 a-1 c), bottom material return ports of the fluidized beds (1 a-1 c) are connected with inlets of the solid heat carrier material return devices (10 a-10 c), and outlets of the solid heat carrier material return devices (10 a-10 c) are connected to the circulating fluidized bed 2; a high-temperature flue gas cyclone separator 7 is arranged at the upper part of the circulating fluidized bed 2, an air blower 15 is arranged at the lower part of the circulating fluidized bed 2, a flue gas secondary cyclone separator 13 is connected with the high-temperature flue gas cyclone separator 7, the high-temperature flue gas cyclone separator 7 is arranged above a heat carrier receiving bin 8, garbage feed hoppers (3 a-3 c) are positioned above garbage feeding devices (4 a-4 c), and the garbage feeding devices (4 a-4 c) are connected with fluidized beds (1 a-1 c); the cyclone separator 11 is positioned at the upper part of the fluidized bed furnaces (1 a-1 c); the cyclone separator 11 is connected with the tar separator 12, and the lower part of the circulating fluidized bed 2 is connected with the fluidized beds (1 a-1 c) and the pyrolysis gas induced draft fan 14. The outlet of the blower 15 is connected with the combustion-supporting air inlet of the circulating fluidized bed 2, and fluidized air is introduced through the blower 15 to realize fluidization of the solid heat carrier.
The fluidized bed furnace (1 a-1 c) is a device for carrying out organic garbage pyrolysis reaction, organic garbage particles and a high-temperature solid heat carrier in the fluidized bed furnace (1 a-1 c) form a certain bed thickness under the fluidization action of a fluidizing medium, the garbage particles and the solid heat carrier are fully heated, mixed and pyrolyzed, organic matters are unstable at high temperature to generate pyrolysis oil gas and garbage carbon, the temperature in the fluidized bed furnace can be 500-1000 ℃, and the internal pressure is normal pressure.
The top of the fluidized bed furnaces (1 a-1 c) is provided with an internal dust removal device, so that a high-temperature environment in the dust removal process is maintained, and the phenomenon that tar generated by pyrolysis is easy to adhere to and block pipelines and equipment under the condition that the temperature of a subsequent system is reduced is avoided. The high-temperature oil gas that produces rises to fluidized bed furnace (1a ~ 1c) top entrained dust and gets into cyclone 11, and cyclone 11 is 2 ~ 4 parallelly connected, and the oil gas flow of every whirlwind is the same basically, and the import speed maintains in the speed interval of the high-efficient separation of whirlwind, and the whirlwind dipleg is equipped with the air-lock device, can reach more than 90% to the dust collection efficiency of average particle diameter at 10 ~ 20 microns.
In order to meet the actual use requirement, the cross section area of the fluidized bed furnaces (1 a-1 c) is circular, quadrangular or other.
The pyrolysis gas loop, namely high-temperature pyrolysis oil gas generated by pyrolysis in the boiling furnaces (1 a-1 c), enters the oil-gas separator 12 for separation after being dedusted at the top, and a part of the separated pyrolysis gas is sent back to the boiling furnaces (1 a-1 c) by the pyrolysis gas induced draft fan to be used as a fluidizing medium, so that the problem of pyrolysis gas quality generated by diluting other inert gases as the fluidizing medium is avoided. The other part of the waste heat is used as supplementary fuel to be supplied to the circulating fluidized bed 2 to heat the solid heat carrier, and the waste heat is used for decomposing gas and purifying the gas for sale.
The circulating fluidized bed 2 mainly has the functions of heating a solid heat carrier, providing heat required by pyrolysis reaction in the fluidized beds (1 a-1 c), combusting carbon generated by pyrolysis in the circulating fluidized bed 2 to generate high-temperature flue gas, and dedusting the high-temperature flue gas to be sent to a subsequent system for waste heat recovery.
As another aspect of the present invention, the distribution direction of the solid heat carrier may be a parallel direction or a series direction.
The solid heat carrier parallel distribution direction is set to be a circulating fluidized bed 2, a high-temperature flue gas cyclone separator 7, a common heat carrier receiving bin 8, 1-3 branch heat carrier feeding devices (9 a-9 c), 1-3 fluidized beds (1 a-1 c) and 1-3 branch heat carrier returning devices (10 a-10 c) in sequence.
Further, the circulating fluidized bed 2 and the common heat carrier receiving bin 8 are used together by 1-3 boiling furnaces 1, the common heat carrier receiving bin 8 can be a bin with any shape, and the reasonable arrangement of each branch feeding device and the corresponding boiling furnace is mainly considered. Each fluidized bed furnace (1 a-1 c) is matched with a corresponding garbage feeding hopper and a garbage feeding device, and a corresponding heat carrier feeding device (9 a-9 c) and a heat carrier returning device (10 a-10 c), as shown in figure 3.
The common heat carrier receiving bin 8 is located above the heat carrier feeding device 9, the number of the heat carrier feeding devices 9 can be 1-3, and the number of the heat carrier feeding devices 9 is 9 a-9 c respectively, as shown in fig. 3, inlets of the heat carrier feeding devices 9 a-9 c are connected with the common heat carrier receiving bin 8 at a certain angle, and the specific angle is determined according to actual engineering use and arrangement.
Outlets of the heat carrier feeding devices 9a to 9c are correspondingly connected with heat carrier inlets of the fluidized beds 1a to 1c, return ports at the bottoms of the fluidized beds 1a to 1c are correspondingly connected with inlets of the heat carrier returning devices 10a to 10c, and outlets of the heat carrier returning devices 10a to 10c are jointly connected to the circulating fluidized bed 2. Different frequencies of motors of the heat carrier feeding devices 9a to 9c are respectively adjusted to ensure that the heat carrier and the fed garbage respectively enter corresponding fluidized bed furnaces in a certain proportion, the fluidized bed furnaces can pyrolyze garbage particles with different treatment capacities so as to meet different treatment capacity combination requirements, and meanwhile, the in-bed pyrolysis temperature can also be realized according to different solid heat carriers and garbage particle proportions so as to meet different pyrolysis product requirements. The generated high-temperature pyrolysis oil gas rises to the built-in cyclone 11 a-11 c at the top of the fluidized bed furnace along the fluidized bed furnaces 1 a-1 c and carries certain ash content for dust removal.
Furthermore, 1-3 branch heat carrier feeding devices (9 a-9 c) can be a mechanical spiral feeding and frequency conversion motor, and can distribute the amount of high-temperature solid heat carriers of each fluidized bed furnace by changing the frequency of the motor, so that heat required by pyrolysis reaction in each fluidized bed furnace (1 a-1 c) is provided, and U-shaped and L-shaped return materials conveyed by air flow can be provided, and the flow of the high-temperature solid heat carriers of each fluidized bed furnace is distributed by changing the feeding air volume.
Furthermore, the same reaction temperature can be maintained in each of the fluidized bed furnaces (1 a-1 c), and different reaction temperatures can be maintained, so that pyrolysis products with different qualities can be obtained.
Furthermore, the parallel arrangement can enable the garbage pyrolysis treatment capacity of the whole device to be 2-4 times larger than that of a common fluidized bed pyrolysis device.
Another aspect of the invention is: the series connection direction is sequentially provided with a circulating fluidized bed 2, a high-temperature flue gas cyclone separator 7, a heat carrier receiving bin 8, a heat carrier feeding device 9, two fluidized beds (1a/1b) and a heat carrier returning device 10, wherein the fluidized beds 1 can be two fluidized beds 1a/1b, the two fluidized beds 1a/1b are separated through a fluidized bed partition plate 100, and a plurality of small holes or gaps are designed on the partition, as shown in fig. 4.
Wherein, the high-temperature solid heat carrier in the circulating fluidized bed 2 is carried to the cyclone separator 7 by the high-temperature flue gas and enters the heat carrier receiving bin 8. The heat carrier receiving bin 8 is located above the heat carrier feeding device 9, an outlet of the heat carrier feeding device 9 is correspondingly connected with a heat carrier inlet of the fluidized bed furnace 1a, pyrolysis is carried out in a fluidized state of the fluidized bed furnace 1a, a built-in cyclone and a pyrolysis gas outlet are not arranged in the fluidized bed furnace 1a, the pyrolysis gas carries the solid heat carrier to enter the fluidized bed furnace 1b through a small hole or a gap formed in a partition plate 100 of the fluidized bed furnace, garbage carbon which is not pyrolyzed continues to be subjected to high-speed mixed pyrolysis in the fluidized bed furnace 2b, the generated pyrolysis gas enters 2-4 built-in cyclone separators 11 which are connected in parallel for dust removal, the oil-gas flow of each cyclone is basically the same, the inlet speed is maintained in a speed interval of cyclone high-efficiency separation, and the cyclone dipleg is provided with a gas locking device, and the dust removal efficiency of 10-20 microns in average particle size can reach more than 90%. The oil gas after dust removal enters an oil-gas separation 12 to separate tar and then returns to the fluidized bed furnace 1a/1b for fluidization. The two fluidized bed furnaces 1a/1b realize two-stage pyrolysis of the garbage, prolong the retention time of the garbage in the fluidized bed furnaces and improve the quality of pyrolysis products.
The bottom material return port of the fluidized bed furnace 1b is correspondingly connected with the inlet of the heat carrier material return device 10, and the outlet of the heat carrier material return device 10 is connected to the material return port of the circulating fluidized bed 2.
By adjusting different frequencies of the motors of the heat carrier feeding devices 9 respectively, the heat carriers are ensured to enter the fluidized bed furnace 1a respectively in a certain proportion with the fed garbage, and heat required by pyrolysis reaction in the fluidized bed furnace 1a is provided.
Optionally, the fluidized bed furnace 1b is connected with the heat carrier receiving bin 8 through setting up the heat carrier feed device 9b, and through adjusting the different frequencies of heat carrier feed device 9b motor, realize the heat supply of fluidized bed furnace 2b pyrolytic reaction, maintain the pyrolysis temperature of rubbish in fluidized bed furnace 1b at 500 ~ 1000 ℃.
The solid heat carrier can be quartz sand, high-temperature ceramic balls, catalyst particles, ash or semicoke and the like, wherein if the catalyst is adopted as the solid heat carrier in a proper temperature interval of the fluidized bed furnace, the garbage pyrolysis reaction can reduce the generation of tar.
In the system starting stage, auxiliary combustion needs to be added into the circulating fluidized bed 2, for example, coal or natural gas heats the solid heat carrier in the circulating fluidized bed 2 to 600-1100 ℃, high-temperature flue gas carries the solid heat carrier to enter a high-temperature flue gas cyclone separator 7, the solid heat carrier and the high-temperature flue gas are separated by using high-speed centrifugal force, and the high-temperature solid heat carrier enters a common heat carrier receiving bin through an outlet of the cyclone separator.
The dedusted high-temperature pyrolysis oil gas is connected to an inlet of the tar separation 12 through a main pipe, and the tar and pyrolysis gas separation is completed in the tar separation 12.
The tar separation 12 can be sprayed and cooled to be below the initial boiling point of oil through circulating water, a large amount of circulating water and pyrolysis oil gas are in direct contact with the tar separation 12, and oil and water are subjected to physical standing separation or high-speed centrifugal separation after being cooled.
The tar separation 12 may separate oil and pyrolysis gas by indirect condensation according to the quality of the tar.
The tar separation 12 can be performed by spraying a large amount of circulating oil, and the tar in the pyrolysis gas is washed into the wash oil by utilizing the similar compatibility principle, so that the pyrolysis oil-gas separation is realized.
Wherein, a part of the separated pyrolysis gas is sent back to the fluidized furnaces 1 a-1 c through a pyrolysis gas induced draft fan 14 to be used as fluidizing air, the other part of the separated pyrolysis gas is sent to the circulating fluidized bed 2 to be used as supplementary fuel, and the redundant pyrolysis gas is further subjected to tar removal, and is stored or sold after deacidification.
The patent has the remarkable effects that:
the different combination pyrolysis process of the garbage fluidized bed and the circulating fluidized bed provided by the system can realize parallel connection or serial connection according to the combination mode of the distribution directions of the solid heat carriers on the basis of keeping the heating advantages of the solid heat carriers. The solid heat carrier parallel distribution direction sets gradually circulating fluidized bed, high temperature flue gas cyclone, storehouse is accepted to public heat carrier, 1 ~ 3 branch road heat carrier feed arrangement, 1 ~ 3 fluidized bed furnaces, 1 ~ 3 branch road heat carrier return charge devices, solves the problem that conventional rubbish pyrolysis device can not realize the macro-scale, is that ordinary rubbish pyrolysis device throughput is 2 ~ 3 times.
The device comprises a circulating fluidized bed, a high-temperature flue gas cyclone separator, a heat carrier receiving bin, a heat carrier feeding device, a fluidized bed furnace and a heat carrier returning device which are sequentially arranged in the serial direction, wherein the fluidized bed furnace is divided into two boiling chambers, a partition plate is arranged between the two boiling chambers, and small holes or gaps are formed in the partition plate. Two boiling chambers of the fluidized bed furnace are connected in series to operate, so that the retention time of the garbage pyrolysis reaction is prolonged, and the quality of pyrolysis products is further improved.
The pyrolysis gas is used as a fluidized medium for pyrolysis of the fluidized bed furnace, so that the high quality of the pyrolysis gas is guaranteed, 2-4 built-in parallel cyclone dust removal devices are arranged in the fluidized bed furnace to maintain the high-temperature environment of the dust removal device, and the problem that pyrolysis tar and dust block a system in the follow-up process is solved.
Claims (10)
1. A garbage pyrolysis process system is characterized in that: the solid heat carrier feeding hopper is positioned above the solid heat carrier feeding device, the solid heat carrier feeding device is connected with the circulating fluidized bed feeding port, and the heat carrier receiving bin is positioned above the solid heat carrier feeding device; an outlet of the solid heat carrier feeding device is connected with an inlet of a heat carrier of the fluidized bed furnace, a return port at the bottom of the fluidized bed furnace is connected with an inlet of the solid heat carrier return device, and an outlet of the solid heat carrier return device is connected to the circulating fluidized bed; the upper part of the circulating fluidized bed is provided with a high-temperature flue gas cyclone separator, the lower part of the circulating fluidized bed is provided with a blower, a flue gas secondary cyclone separator is connected with the high-temperature flue gas cyclone separator, the high-temperature flue gas cyclone separator is arranged above a heat carrier receiving bin, a garbage feeding hopper is positioned above a garbage feeding device, and the garbage feeding device is connected with a fluidized bed furnace; the cyclone separator is positioned at the upper part of the fluidized bed furnace; the cyclone separator is connected with the tar separator, and the lower part of the circulating fluidized bed is connected with the fluidized bed and the pyrolysis gas induced draft fan.
2. The waste pyrolysis process system of claim 1, wherein: organic garbage particles and a high-temperature solid heat carrier in a fluidized bed furnace form a certain bed thickness under the fluidization action of a fluidizing medium, the garbage particles and the solid heat carrier are fully heated, mixed and pyrolyzed, organic matters are pyrolyzed at 500-1000 ℃ due to thermal instability to generate pyrolysis oil gas and garbage carbon, the high-temperature pyrolysis oil gas generated by pyrolysis enters a cyclone separator and a tar separator after being dedusted at the top, part of the separated pyrolysis gas is sent back to the fluidized bed furnace by a pyrolysis gas induced draft fan to serve as the fluidizing medium, the other part of the separated pyrolysis gas serves as supplementary fuel and is supplied to a circulating fluidized bed for internal combustion heating of the solid heat carrier to 600-1100 ℃, heat required by pyrolysis reaction in the fluidized bed furnace is provided, and the surplus pyrolysis gas is sold after purification.
3. The waste pyrolysis process system of claim 1, wherein: high-temperature flue gas generated by combustion of a circulating fluidized bed carries a solid heat carrier to realize gas-solid separation through a high-temperature flue gas cyclone separator, the high-temperature flue gas is dedusted by a flue gas secondary cyclone separator and then is sent to a subsequent system for waste heat recovery, the separated high-temperature solid heat carrier enters a heat carrier receiving bin to be cached, and a solid heat carrier feeding device sends the high-temperature solid heat carrier in the heat carrier receiving bin to a fluidized bed furnace to serve as a raw material for garbage pyrolysis reaction; and after pyrolysis is finished, the cooled solid heat carrier and the generated residual carbon are sent into the circulating fluidized bed through the solid heat carrier returning device to heat the solid heat carrier, so that the circulation of heating, pyrolysis and heating of the solid heat carrier in the system is realized.
4. The waste pyrolysis process system of claim 1, wherein: the solid heat carrier feeding device and the solid heat carrier returning device are of a mechanical spiral feeding structure or a U-shaped and L-shaped airflow feeding structure, and the garbage feeding device and the solid heat carrier supplementing device are of a mechanical spiral feeding structure.
5. The waste pyrolysis process system of claim 1, wherein: the distribution direction of the solid heat carrier is a parallel direction or a serial direction.
6. The waste pyrolysis process system of claim 5, wherein: the parallel distribution direction of the solid heat carrier is sequentially set to be a circulating fluidized bed, a high-temperature flue gas cyclone separator, a common heat carrier receiving bin, 1-3 branch heat carrier feeding devices, 1-3 fluidized beds and 1-3 branch heat carrier returning devices.
7. The waste pyrolysis process system of claim 6, wherein: the circulating fluidized bed and the common heat carrier receiving bin are used together by 1-3 fluidized beds, and each fluidized bed is matched with a corresponding garbage feeding hopper and a garbage feeding device as well as a corresponding solid heat carrier feeding device and a corresponding solid heat carrier returning device; the common heat carrier receiving bin is positioned above 1-3 branch heat carrier feeding devices, an outlet of each solid heat carrier feeding device is connected with an inlet of a corresponding fluidized bed furnace heat carrier, a bottom return port of each fluidized bed furnace is connected with an inlet of the corresponding solid heat carrier returning device, and 1-3 branch heat carrier returning devices are connected to the circulating fluidized bed; the 1-3 boiling furnaces are arranged around the common heat carrier receiving bin at a certain angle, and the cross section area of each boiling furnace is circular or quadrilateral.
8. The waste pyrolysis process system of claim 5, wherein: the series direction is sequentially set into a circulating fluidized bed, a high-temperature flue gas cyclone separator, a heat carrier receiving bin, a heat carrier feeding device and a fluidized bed furnace, wherein the fluidized bed furnace is divided into two boiling chambers, a partition plate is arranged between the chambers, and small holes or gaps and the heat carrier returning device are arranged on the partition plate.
9. The waste pyrolysis process system of claim 8, wherein: pyrolysis gas generated in the first boiling chamber carries a solid heat carrier to enter the boiling furnace through small holes or gaps of partition plates of the boiling furnace, and garbage carbon which is not pyrolyzed continuously undergoes high-speed mixing pyrolysis in the second boiling chamber; two boiling chambers of the fluidized bed furnace are connected in series to operate, so that the retention time of the garbage pyrolysis reaction is prolonged, and the quality of pyrolysis products is further improved.
10. The waste pyrolysis process system of claim 1, wherein: the top of the fluidized bed furnace is provided with 2-4 internal dust removal devices connected in parallel.
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| CN202010052544.8A CN113136230A (en) | 2020-01-17 | 2020-01-17 | Garbage pyrolysis process system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115109606A (en) * | 2022-07-06 | 2022-09-27 | 山东省红森林新材料科技有限公司 | Pure hydrogen and poly-generation coupling system prepared from biomass waste |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115109606A (en) * | 2022-07-06 | 2022-09-27 | 山东省红森林新材料科技有限公司 | Pure hydrogen and poly-generation coupling system prepared from biomass waste |
| CN115109606B (en) * | 2022-07-06 | 2023-09-08 | 山东省红森林新材料科技有限公司 | Pure hydrogen and poly-generation coupling system prepared from biomass waste |
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