CN115109606A - Pure hydrogen and poly-generation coupling system prepared from biomass waste - Google Patents
Pure hydrogen and poly-generation coupling system prepared from biomass waste Download PDFInfo
- Publication number
- CN115109606A CN115109606A CN202210796954.2A CN202210796954A CN115109606A CN 115109606 A CN115109606 A CN 115109606A CN 202210796954 A CN202210796954 A CN 202210796954A CN 115109606 A CN115109606 A CN 115109606A
- Authority
- CN
- China
- Prior art keywords
- communicated
- inlet end
- outlet end
- boiling
- hydrogen
- 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.)
- Granted
Links
Images
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
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/026—Dust removal by centrifugal forces
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/32—Purifying combustible gases containing carbon monoxide with selectively adsorptive solids, e.g. active carbon
-
- 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
- Y02P20/133—Renewable energy sources, e.g. sunlight
Abstract
The invention discloses a pure hydrogen and poly-generation coupling system prepared from biomass wastes, wherein dry-based biomass powder is added at the inlet end of a pre-cracking gasification mechanism, the smoke outlet of the pre-cracking gasification mechanism is communicated with the inlet end of a sub-temperature heat exchanger, the first outlet end of the sub-temperature heat exchanger is communicated with a smoke exhaust mechanism, the outlet end of the pre-cracking gasification mechanism is communicated with the inlet end of a carbonization hydrogen production mechanism, the smoke outlet of the carbonization hydrogen production mechanism is communicated with the inlet end of a high-temperature resistant cyclone dust collector, the outlet end of the high-temperature resistant cyclone dust collector is communicated with the inlet end of a heat exchanger through a high-temperature heat exchanger, and the outlet end of the heat exchanger is communicated with the inlet end of a washing tower through an induced draft fan. The invention obtains the hydrogen-rich high-purity non-hydrogen biogas through pre-cracking of a muffle type rotary kiln and thermal cracking, deep carbonization and carbon quenching of a suspension fluidized bed furnace, and obtains the pure hydrogen energy and the high-purity non-hydrogen biogas with the highest purity of 99.99 percent after pressure swing adsorption and separation treatment of an adsorption tower.
Description
Technical Field
The invention belongs to the technical field of biomass energy, and particularly relates to a pure hydrogen and poly-generation coupling system prepared from biomass wastes.
Background
There are many ways of hydrogen energy production: the hydrogen production forms of coal hydrogen production, natural gas hydrogen production, refinery gas hydrogen production, methanol hydrogen production, industrial byproduct hydrogen production, coke oven gas hydrogen production, water electrolysis hydrogen production, ammonia decomposition hydrogen production and the like are diversified. The hydrogen production process in China is different in hydrogen production routes selected according to different regions, industries and resources. The western China is rich in natural gas, mainly natural gas is used as the main gas, oil refining enterprises produce hydrogen by using dry gas, and the natural gas produces hydrogen more, and northern enterprises mostly use coal as a raw material to obtain hydrogen and develop downstream industries, so that the coal hydrogen production cost is low, but the environmental protection investment is large, and most of the enterprises are large-scale devices. The coke-oven gas hydrogen production is obtained by the byproduct hydrogen, and the waste is changed into valuable. Water electrolysis and methanol hydrogen production mainly adopt small-sized hydrogen demand, the cost is high, and the technology has no new breakthrough.
With the increasing shortage of petroleum resources, the demand for hydrogen energy is increasing. However, hydrogen in the current market is mainly prepared from fossil energy, and the problem of regeneration of energy resources cannot be solved. The combustion product of hydrogen is water, and the hydrogen produced by decomposing water is regenerated hydrogen, which is inexhaustible. However, the current water electrolysis technology has high energy consumption and high hydrogen cost, so that the method is eagerly to obtain renewable, recyclable, clean, environment-friendly, green and cheap pure hydrogen energy, and is an urgent problem to be solved.
Disclosure of Invention
The technical problem to be solved by the invention is to overcome the defects of the prior art and provide a coupling system for preparing pure hydrogen and poly-generation by using biomass wastes.
The technical scheme for solving the technical problems is as follows: adding dry-based biomass powder into an inlet end of a pre-cracking gasification mechanism and carrying out pre-cracking gasification on the dry-based biomass powder, wherein a smoke outlet of the pre-cracking gasification mechanism is communicated with an inlet end of a sub-temperature heat exchanger, a first outlet end of the sub-temperature heat exchanger is communicated with a smoke exhaust mechanism, an outlet end of the pre-cracking gasification mechanism is communicated with an inlet end of a carbonization hydrogen production mechanism, the carbonization hydrogen production mechanism carries out suspension boiling thermal cracking gasification, carbonization and hydrogen production on the biomass powder after the pre-cracking gasification, a smoke outlet of the carbonization hydrogen production mechanism is communicated with an inlet end of a high-temperature resistant cyclone dust collector, an outlet end of the high-temperature resistant cyclone dust collector is communicated with an inlet end of a heat exchanger through a high-temperature heat exchanger, an outlet end of the heat exchanger is communicated with an inlet end of a washing tower through an induced draft fan, an outlet end of the washing tower is communicated with an inlet end of a steam-water separator, and an outlet end of the steam-water separator are communicated with an inlet end of a first adsorption tower through a compressor, the first outlet end of the first adsorption tower is communicated with the inlet end of the first pure hydrogen tank, the outlet end of the first pure hydrogen tank is communicated with the inlet end of the second pure hydrogen tank, the second outlet end of the first adsorption tower is communicated with the inlet end of the gas storage tank, the first outlet end of the second adsorption tower is communicated with the inlet end of the first pure hydrogen tank, the second outlet end of the second adsorption tower is communicated with the inlet end of the gas storage tank, and the outlet end of the gas storage tank is communicated with the inlet end of the heat exchanger.
Further, the pre-cracking gasification mechanism is as follows: the inlet end of the muffle type rotary kiln is provided with a second screw conveyor for conveying dry-based biomass powder, the muffle type rotary kiln carries out pre-thermal cracking gasification on the dry-based biomass powder, the outlet end of a kiln hood at one end of the muffle type rotary kiln is provided with a first screw conveyor for conveying the pre-thermal cracking gasified biomass powder to a carbonization hydrogen production mechanism, and the output end of the first screw conveyor is communicated with the inlet end of the carbonization hydrogen production mechanism through a front blanking pipe; the second outlet end of the sub-temperature heat exchanger is communicated with the inlet end of the hydrogen production carbonization mechanism, and the gas outlet of the muffle type rotary kiln is communicated with the first burner at the bottom of the muffle type rotary kiln and the inlet end of the hydrogen production carbonization mechanism through a gas fan.
Furthermore, the temperature of the muffle type rotary kiln is 400-800 ℃, and the running time of the dry-based biomass powder in the muffle type rotary kiln is 6-12 min.
Further, the hydrogen mechanism is produced in carbonization: the suspension boiling pyrolysis furnace is internally provided with a rear retaining wall and a front retaining wall, the inner side wall of the suspension boiling pyrolysis furnace is provided with a side surface boiling bed, the side surface boiling bed is uniformly provided with air pipes, a front boiling bed is arranged between the front retaining wall and the side surface boiling bed, the lower side of the front boiling bed is provided with a front hot air bin, a rear boiling bed is arranged between the rear retaining wall and the front retaining wall, the lower side of the rear boiling bed is provided with a rear hot air bin, the front boiling bed and the rear boiling bed are uniformly provided with air caps, the suspension boiling pyrolysis furnace is internally provided with a partition wall and a smoke partition wall which divide the interior of the suspension boiling pyrolysis furnace into a front boiling chamber, a rear boiling chamber, a gas chamber, the front boiling chamber is communicated with the rear boiling chamber, the front boiling chamber is positioned on the upper sides of the front boiling bed and the rear boiling bed, the rear boiling chamber and the gas chamber are respectively communicated with a blanking settling hopper, the blanking settling hopper is communicated with a deep carbonization bin positioned below the settling hopper, the air inlet annular pipe is positioned in a heating chamber of the suspension boiling pyrolysis furnace, one side of the suspension boiling pyrolysis furnace is provided with the air inlet annular pipe, the heating chamber is internally provided with a heat exchange branch pipe positioned in the circumferential direction of the deep carbonization bin, and the heat exchange branch pipe is communicated with the air inlet annular pipe; the smoke outlet of the heating chamber is communicated with the inlet end of the kiln head cover through a high-temperature fan, the second outlet end of the sub-temperature heat exchanger is communicated with the inlet end of the heating chamber, and the gas outlet of the muffle type rotary kiln is communicated with the second burner and the third burner of the heating chamber through a gas fan; the outlet end of the high-temperature heat exchanger is communicated with the heating chamber through a combustion fan, the outlet end of the high-temperature resistant cyclone dust collector is communicated with the air inlet annular pipe through an air booster fan, and the outlet end of the heat exchanger is communicated with the third burner through a coal gas fan.
Furthermore, the outlet end of the fuel gas chamber is communicated with the inlet end of the high-temperature resistant cyclone dust collector, a fourth screw conveyor is arranged at the outlet end of the bottom of the high-temperature resistant cyclone dust collector, and the outlet end of the fourth screw conveyor is communicated with the fuel gas chamber through a rear blanking pipe.
Furthermore, the temperature of the front boiling chamber is 800-950 ℃, and the air speed is 0.8-2.0 m/s.
Furthermore, degree of depth carbomorphism storehouse bottom be provided with the third screw conveyer that is used for transporting the biochar, the degree of depth carbomorphism storehouse circumferencial direction that is located the outside of suspension boiling pyrolysis oven is provided with the heat preservation cotton, degree of depth carbomorphism storehouse circumferencial direction is provided with the water-cooling cover that is located the heat preservation cotton below, the inside water smoke shower nozzle that communicates each other with the water-cooling cover that is provided with in degree of depth carbomorphism storehouse.
Further, the smoke exhaust mechanism is as follows: the first outlet end of the sub-temperature heat exchanger is communicated with the inlet end of the cyclone dust collector, the outlet end of the cyclone dust collector is communicated with the inlet end of the bag-type dust collector, and the outlet end of the bag-type dust collector is communicated with the inlet end of the chimney through the exhaust fan.
The invention has the beneficial effects that: (1) the invention adopts all organic hydrocarbon solid wastes such as straws, weeds, household garbage, kitchen garbage, culture excrement and the like, and after iron removal, dehydration, tearing or crushing into powder and drying, after pre-cracking in a flame-isolated rotary kiln, thermal cracking in a suspension fluidized bed furnace, deep carbonization and carbon quenching, hydrogen-rich high-purity non-hydrogen biogas is obtained, and after pressure swing adsorption and separation treatment in an adsorption tower, pure hydrogen energy and high-purity non-hydrogen biogas with the highest purity of 99.99 percent are obtained, can poly-produce pure hydrogen, fuel gas, electric energy, hot water, steam and biomass carbon or carbon-based fertilizer, obtains a large amount of renewable, recyclable, clean and green products, changes organic garbage into valuable, prepares renewable, recyclable, clean, environment-friendly, green and cheap pure hydrogen, meanwhile, the problems of ecology and environmental protection are solved, and the invention has ecological significance, environmental protection significance and economic significance.
(2) The high-purity hydrogen is used as a regenerated, recyclable, clean, environment-friendly and cheap pure hydrogen energy source, is directly applied to hydrogen metallurgy, and can be compressed into liquid pure hydrogen or high-pressure pure hydrogen to be used as a clean green hydrogen energy automobile and other hydrogen energy fuel cells. CO + CH is separated out by the first adsorption tower and the second adsorption tower 4 Other high-purity non-hydrogen bio-combustible gas can be used as a burner for heating a heating chamber or used for poly-generation pipeline gas, steam, hot water, fuel cell stack power generation and other applications.
Drawings
FIG. 1 is a schematic structural diagram of an embodiment 1 of the coupling system for preparing pure hydrogen and poly-generation from biomass waste according to the present invention.
Fig. 2 is a schematic structural view of the smoke evacuation mechanism 1 in fig. 1.
Fig. 3 is a schematic structural diagram of the pre-cracking gasification mechanism 3 and the hydrogen-producing carbonization mechanism 4 in fig. 1.
Fig. 4 is a schematic structural diagram of the hydrogen production carbonization mechanism 4 in fig. 3.
Fig. 5 is a sectional view a-a in fig. 4.
Fig. 6 is a sectional view taken along line B-B in fig. 4.
Fig. 7 is a schematic structural view of the hydrogen production mechanism by carbonization 4 according to example 2.
Reference numerals: 1. a smoke exhaust mechanism; 101. a chimney; 102. a bag-type dust collector; 103. a cyclone dust collector; 104. an exhaust fan; 2. a sub-temperature heat exchanger; 3. a pre-cracking gasification mechanism; 301. a muffle type rotary kiln; 302. a gas fan; 303. a kiln head cover; 304. a high temperature fan; 305. a front blanking pipe; 306. a first screw conveyor; 307. a first burner; 308. a second screw conveyor; 4. a carbonization hydrogen production mechanism; 401. a front boiling chamber; 402. a suspended fluidized pyrolysis furnace; 403. a partition wall; 404. a rear boiling chamber; 405. a smoke barrier wall; 406. a gas chamber; 407. a blanking settling hopper; 408. an air inlet annular pipe; 409. heat preservation cotton;
410. a water mist spray head; 411. a third screw conveyor; 412. a deep carbonization bin; 413. a heat exchange branch pipe;
414. a rear retaining wall; 415. a rear hot air bin; 416. a front retaining wall; 417. a second burner; 418. a front hot air bin; 419. a side bubbling bed; 420. a fourth screw conveyor; 421. a post-blanking pipe; 422. water cooling jacket; 423. a third burner; 424. a heating chamber; 425. an air duct; 426. a front bubbling bed; 427. a hood; 428. a post-bubbling bed; 429. a combustion fan; 430. a coal gas booster fan; 431. a gas fan; 432. an electromagnetic coil; 5. a high temperature resistant cyclone dust collector; 6. a high temperature heat exchanger; 7. a heat exchanger; 8. a washing tower; 9. a steam-water separator; 10. a compressor; 11. a first adsorption column; 12. a second adsorption column; 13. a first pure hydrogen tank; 14. a second pure hydrogen tank; 15. a gas storage tank; 16. an induced draft fan.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Example 1
As shown in fig. 1, the coupling system for preparing pure hydrogen from biomass waste and for poly-generation in this embodiment is formed by connecting a smoke exhaust mechanism 1, a sub-temperature heat exchanger 2, a pre-cracking gasification mechanism 3, a carbonized hydrogen production mechanism 4, a high temperature resistant cyclone dust collector 5, a high temperature heat exchanger 6, a heat exchanger 7, a washing tower 8, a steam-water separator 9, a compressor 10, a first adsorption tower 11, a second adsorption tower 12, a first pure hydrogen tank 13, a second pure hydrogen tank 14, a gas storage tank 15, and an induced draft fan 16.
Adding dry-based biomass powder into the inlet end of a pre-cracking gasification mechanism 3 and carrying out pre-cracking gasification on the dry-based biomass powder, wherein a smoke outlet of the pre-cracking gasification mechanism 3 is communicated with the inlet end of a sub-temperature heat exchanger 2, a first outlet end of the sub-temperature heat exchanger 2 is communicated with a smoke exhaust mechanism 1, an outlet end of the pre-cracking gasification mechanism 3 is communicated with the inlet end of a hydrogen production carbonization mechanism 4, the hydrogen production carbonization mechanism 4 carries out suspension boiling thermal cracking gasification, carbonization and hydrogen production on the biomass powder after pre-cracking gasification, a smoke outlet of the hydrogen production carbonization mechanism 4 is communicated with the inlet end of a high-temperature resistant cyclone dust collector 5, an outlet end of the high-temperature resistant cyclone dust collector 5 is communicated with the inlet end of a heat exchanger 7 through a high-temperature heat exchanger 6, an outlet end of the heat exchanger 7 is communicated with the inlet end of a washing tower 8 through a draught fan 16, and an outlet end of the washing tower 8 is communicated with the inlet end of a steam-water separator 9, the outlet end of the steam-water separator 9 is communicated with the inlet end of a first adsorption tower 11 through a compressor 10, the first outlet end of the first adsorption tower 11 is communicated with the inlet end of a first pure hydrogen tank 13, the outlet end of the first pure hydrogen tank 13 is communicated with the inlet end of a second pure hydrogen tank 14, the second outlet end of the first adsorption tower 11 is communicated with the inlet end of a gas storage tank 15, the first outlet end of the second adsorption tower 12 is communicated with the inlet end of the first pure hydrogen tank 13, the second outlet end of the second adsorption tower 12 is communicated with the inlet end of the gas storage tank 15, and the outlet end of the gas storage tank 15 is communicated with the inlet end of a heat exchanger 7.
As shown in fig. 2, the smoke exhaust mechanism 1 is formed by connecting a chimney 101, a bag-type dust collector 102, a cyclone dust collector 103 and an exhaust fan 104, and the smoke exhaust mechanism 1 is as follows: the first outlet end of the sub-temperature heat exchanger 2 is communicated with the inlet end of a cyclone dust collector 103, the outlet end of the cyclone dust collector 103 is communicated with the inlet end of a bag-type dust collector 102, and the outlet end of the bag-type dust collector 102 is communicated with the inlet end of a chimney 101 through an exhaust fan 104.
The smoke outlet of a heating chamber of the muffle type rotary kiln 301 has the temperature of about 280-500 ℃, the smoke temperature is reduced to 180-220 ℃ after heat exchange by the sub-temperature heat exchanger 2, and then the smoke enters the cyclone dust collector 103 and the bag-type dust collector 102 for treatment, and is exhausted by the exhaust fan 104 and the chimney 101.
As shown in fig. 3, the pre-cracking gasification mechanism 3 is formed by connecting a muffle-type rotary kiln 301, a gas fan 302, a kiln head cover 303, a high-temperature fan 304, a front blanking pipe 305, a first screw conveyor 306, a first burner 307, and a second screw conveyor 308, and the pre-cracking gasification mechanism 3 is: the inlet end of the muffle type rotary kiln 301 is provided with a second screw conveyor 308 for conveying dry-based biomass powder, the temperature of the muffle type rotary kiln 301 is 400-800 ℃, and the running time of the dry-based biomass powder in the muffle type rotary kiln 301 is 6-12 min. The muffle type rotary kiln 301 is used for carrying out pre-thermal cracking gasification on dry-based biomass powder, the outlet end of a kiln head cover 303 at one end of the muffle type rotary kiln 301 is provided with a first screw conveyor 306 for conveying the biomass powder subjected to pre-thermal cracking gasification to the hydrogen production carbonization mechanism 4, and the output end of the first screw conveyor 306 is communicated with the inlet end of the hydrogen production carbonization mechanism 4 through a front blanking pipe 305.
The second outlet end of the sub-temperature heat exchanger 2 is communicated with the inlet end of the hydrogen production carbonization mechanism 4, and the gas outlet of the muffle type rotary kiln 301 is communicated with the first burner 307 at the bottom of the muffle type rotary kiln 301 and the inlet end of the hydrogen production carbonization mechanism 4 through a gas fan 302.
The heat source of the muffle-type rotary kiln 301 is mainly initial fuel gas generated by the heat source, and the initial fuel gas is injected into a plurality of first burners 307 from a fuel gas outlet of the muffle-type rotary kiln 301 through a fuel gas fan 302 to indirectly heat the muffle-type rotary kiln 301 by muffle. The combustion-supporting air heat exchange hot air of the muffle-type rotary kiln 301 comes from the sub-temperature heat exchanger 2, and redundant fuel gas provides energy for the second burner 417 and the third burner 423 of the heating chamber 424. And after cold air enters the sub-temperature heat exchanger 2 for heat exchange, hot combustion-supporting air is provided for the muffle type rotary kiln 301 and the first burner 307.
As shown in fig. 3 to 6, the hydrogen production carbonization mechanism 4 is formed by connecting a front boiling chamber 401, a suspension boiling pyrolysis furnace 402, a partition wall 403, a rear boiling chamber 404, a smoke partition wall 405, a gas chamber 406, a blanking settling hopper 407, an air inlet circular tube 408, heat insulation cotton 409, a water spray nozzle 410, a third screw conveyor 411, a deep carbonization bin 412, a heat exchange branch pipe 413, a rear retaining wall 414, a rear hot air bin 415, a front retaining wall 416, a second burner 417, a front hot air bin 418, a side boiling bed 419, a fourth screw conveyor 420, a rear blanking tube 421, a water cooling jacket 422, a third burner 423, a heating chamber 424, an air duct 425, a front boiling bed 426, an air cap 427, a rear boiling bed 428, a combustion fan 429, a gas booster fan 430 and a gas fan 431, and the hydrogen production carbonization mechanism 4 is: the suspended fluidized pyrolysis furnace 402 is internally provided with a rear retaining wall 414 and a front retaining wall 416, the maximum temperature of the suspended fluidized pyrolysis furnace 402 is not more than 1000 ℃, the inner side wall of the suspended fluidized pyrolysis furnace 402 is provided with a side fluidized bed 419, the side fluidized bed 419 is uniformly provided with an air pipe 425, a front fluidized bed 426 is arranged between the front retaining wall 416 and the side fluidized bed 419, the lower side of the front fluidized bed 426 is provided with a front hot air bin 418, the rear retaining wall 414 is provided with a rear fluidized bed 428 between the front retaining wall 416 and the rear retaining wall 428, the lower side of the rear fluidized bed 428 is provided with a rear hot air bin 415, the front fluidized bed 426 and the rear fluidized bed 428 are uniformly provided with air caps 427, the front fluidized bed 426 and the rear fluidized bed 428 are two groups of fluidized beds, and part of coarse particles in biomass powder can float twice and finally are collected and settled in the blanking settling hopper 407. The suspended boiling pyrolysis furnace 402 is internally provided with a partition wall 403 and a smoke partition wall 405 which divide the interior of the suspended boiling pyrolysis furnace 402 into a front boiling chamber 401, a rear boiling chamber 404 and a gas chamber 406, the front boiling chamber 401 is communicated with the rear boiling chamber 404, and the floating time of biomass powder in the front boiling chamber 401 and the rear boiling chamber 404 is about 3-20 s. The partition wall 403 and the smoke partition wall 405 can block part of biomass powder from going forward, so that the thermal cracking residence time of the biomass powder is increased, and the partition wall 403 and the smoke partition wall 405 mainly function in slightly blocking airflow of the front boiling chamber 401 and the rear boiling chamber 404, so that the airflow passes through the lower hole and the biomass powder falls off. The smoke barrier 405 is slightly longer than the partition 403.
The rear retaining wall 414, the front retaining wall 416, the partition wall 403 and the smoke partition wall 405 are all built by secondary clay bricks, the loose biomass powder with the bulk density of about 0.2-0.3 t/m3 is obtained. The rear retaining wall 414 is shorter than the front retaining wall 416, so as to facilitate the biomass powder to boil for a little longer time and to facilitate the biomass powder to move to the blanking settling hopper 407. The front boiling chamber 401 is positioned above the front boiling bed 426 and the rear boiling bed 428, the temperature of the front boiling chamber 401 is 800-950 ℃, and the wind speed is 0.8-2.0 m/s. The middle upper part of the front boiling chamber 401 and the rear boiling chamber 404 is negative pressure, and the pressure is generally-200 to-300 Pa. The rear boiling chamber 404 and the gas chamber 406 are respectively communicated with a blanking settling hopper 407, the blanking settling hopper 407 is communicated with a deep carbonization bin 412 positioned below the blanking settling hopper 407, the air inlet annular pipe 408 is positioned in a heating chamber 424 of the suspension boiling pyrolysis furnace 402, the air inlet annular pipe 408 is arranged on one side of the suspension boiling pyrolysis furnace 402, a heat exchange branch pipe 413 positioned in the circumferential direction of the deep carbonization bin 412 is arranged in the heating chamber 424, and the heat exchange branch pipe 413 is communicated with the air inlet annular pipe 408. The high-temperature parts of the outer walls of the suspension boiling pyrolysis furnace 402 and the heating chamber 424 are all built by adopting heat-insulating cotton felts, light heat-insulating bricks and secondary clay bricks, heat-insulating measures are enhanced, and the periphery is wrapped by adopting a steel structure to prevent heat loss.
The smoke outlet of the heating chamber 424 is communicated with the inlet end of the kiln head cover 303 through the high-temperature fan 304, the second outlet end of the sub-temperature heat exchanger 2 is communicated with the inlet end of the heating chamber 424, and the gas outlet of the muffle type rotary kiln 301 is communicated with the second burner 417 and the third burner 423 of the heating chamber 424 through the gas fan 302. The high-temperature flue gas with the temperature of 900-950 ℃ in the heating chamber 424 passes through the high-temperature fan 304 and the kiln head cover 303 through the smoke outlet of the heating chamber 424 and is pumped into the inner cylinder of the muffle type rotary kiln 301 to provide heat for the muffle type rotary kiln 301.
The outlet end of the high-temperature heat exchanger 6 is communicated with the heating chamber 424 through a combustion fan 429, the outlet end of the high-temperature resistant cyclone dust collector 5 is communicated with the air inlet annular pipe 408 through a coal gas booster fan 430, and the outlet end of the heat exchanger 7 is communicated with the third burner 423 through a coal gas fan 431. The outlet end of the gas chamber 406 is communicated with the inlet end of the high-temperature resistant cyclone dust collector 5, the outlet end of the bottom of the high-temperature resistant cyclone dust collector 5 is provided with a fourth screw conveyor 420, and the outlet end of the fourth screw conveyor 420 is communicated with the gas chamber 406 through a rear blanking pipe 421.
The bottom of the deep carbonization bin 412 is provided with a third screw conveyor 411 for conveying biochar, the circumferential direction of the deep carbonization bin 412 positioned outside the suspension boiling pyrolysis furnace 402 is provided with heat-insulating cotton 409, the circumferential direction of the deep carbonization bin 412 is provided with a water-cooling jacket 422 positioned below the heat-insulating cotton 409, and the deep carbonization bin 412 is internally provided with a water spray nozzle 410 communicated with the water-cooling jacket 422. The water spray nozzles 410 are three seamless steel pipes which are triangular cones and are supported on the side wall of the deep carbonization bin 412, a small hole with the diameter phi of 0.6mm is drilled in each seamless pipe and is used for quenching carbon and reducing the temperature, the sprayed water amount is adjustable, the water content of the generated biochar is controlled to be 12-15%, and subsequent storage and transportation or particle extrusion of the biochar products are facilitated. The water cooling jacket 422 is indirectly cooled circularly, the biochar is cooled to 30-50 ℃, and the biochar is discharged through a third screw conveyor 411.
Example 2
As shown in fig. 7, the annular gas inlet pipe 408, the heat exchange branch pipes 413, the heating chamber 424, and the like in embodiment 1 are replaced with the electromagnetic coil 432, and the electromagnetic coil 432 is energized to heat the hot reducing gas, so that the hot reducing gas is heated without burning part of the generated gas, and the yield of the gas is relatively increased. The separated 99.99 percent pure hydrogen is used as a cheap and green pure hydrogen energy source and can be widely applied to the fields of automobiles, aviation, hydrogen metallurgy, chemical engineering and the like; the concentration of the CO + CH4+ other mixed high-purity non-hydrogen fuel gas is still high, the mixed high-purity non-hydrogen fuel gas can be used as pipeline gas, and can also be used for power generation in forms of fuel cell stacks and the like or heating to produce saturated steam, hot water heating and the like, and a large amount of hot water can be produced after the suspended boiling pyrolysis furnace 402 is quenched.
Other components and the connection relationship of the components are the same as those in embodiment 1.
The working principle of the embodiment is as follows:
(1) preparing dry-base biomass powder: the method comprises the steps of removing iron from the hydrocarbon organic compound waste, dehydrating, tearing or crushing the organic waste into small pieces or powder with the particle size of 0-5 mm by using a tearing machine or a crusher, adding the small pieces or powder into a drying kiln, drying until the moisture content is controlled to be 10-12%, and forming dry-based biomass powder for later use. The invention is also suitable for thermal cracking gasification of hydrogen-rich high-purity biogas by adopting extruded particles or wood-processed small blocks of all biomass such as straws, livestock and poultry breeding excrement and the like.
(2) Pre-thermal cracking gasification: and (3) conveying the dry-based biomass powder into the muffle-type rotary kiln 301 through the second screw conveyer 308, controlling the temperature of the muffle-type rotary kiln 301 at 400-800 ℃, further drying, preheating and pre-cracking the dry-based biomass powder, wherein the running time of the dry-based biomass powder in the muffle-type rotary kiln 301 is 6-12 min.
(3) Suspension boiling thermal cracking gasification: the biomass powder after the pre-thermal cracking gasification in the muffle-type rotary kiln 301 flows into the front boiling chamber 401 from the front discharging pipe 305 through the first screw conveyer 306, passes through the front boiling bed 426 and the front hot air bin 418 through the wind cap 427 under the reducing gas with the temperature of 800-950 ℃ and the wind speed of 0.8-2.0 m/s, so that the powdery biomass powder which just falls flies to the upper part of the front boiling chamber 401 and slowly floats, and part of the biomass powder can repeatedly float upwards and downwards for several times.
The high-temperature reducing gas is sprayed obliquely and transversely to blow out the high-temperature reducing gas when passing through the side boiling bed 419 and the air pipe 425, so that the falling biomass powder can pass through holes below the partition wall 403 as soon as possible, enter the rear hot air bin 415, pass through the rear boiling bed 428 and the air cap 427, enter the front boiling chamber 401, and then perform the floating movement in the next period until the falling biomass powder is blown into the blanking settling hopper 407 of the rear boiling chamber 404 by the obliquely and transversely hot air to continue settling and fall, and the biomass carbon powder is formed.
The high-temperature flue gas can pass through the smoke barrier wall 405 and then enter the gas chamber 406, and then enters the high-temperature resistant cyclone dust collector 5 through the smoke exhaust port of the gas chamber 406, so that most of the biomass carbon powder overflowing the suspension boiling pyrolysis furnace 402 is recovered, and because the biomass carbon powder collected by the high-temperature resistant cyclone dust collector 5 is not carbonized completely, the biomass carbon powder needs to be hermetically added into the blanking settling hopper 407 through the fourth screw conveyor 420 and the rear feeding pipe 421 for deep carbonization.
The thermal cracking gasification treatment yield is high, the thermal cracking gasification biomass powder loose bulk can be treated in each square meter year and can reach 8 ten thousand tons, the thermal cracking gasification dry-based biomass material can reach the scale of 50-60 ten thousand tons in a common production line year, and the method has the remarkable characteristics of low investment ratio and high capacity.
(4) Deep carbonization and carbon quenching hydrogen production: the second burner 417 and the third burner 423 on the periphery of the heating chamber 424 heat the muffle thereof, and simultaneously heat the hot reducing gas in the heat exchange branch pipe 413 by raising the temperature, further expand the hot reducing gas to increase the pressure, and further increase the boiling power. The sensible heat of the hot reducing gas is 700-800 ℃, the temperature is raised through heating of the heating chamber 424 to reach 800-950 ℃, and then the sensible heat passes through the rear hot air bin 415 and the front hot air bin 418, passes through the front boiling bed 426, the rear boiling bed 428, the side boiling bed 419, the hood 427 and the air pipe 425, and provides boiling power for the front boiling chamber 401 and the rear boiling chamber 404 and supplements sensible heat of thermal cracking.
When the biomass powder of the blanking settling hopper 407 falls to the deep carbonization bin 412, the temperature of the material is 800-950 ℃, deep pyrolysis and carbonization are continuously carried out to reduce volatilization in the biomass powder and also promote the generation of CO2 until the material reaches the technical requirements of the process, the material further falls off, after leaving the heating chamber 424, deep carbonization is continuously carried out to gradually reduce the content of volatile matters to 2-15%, the shell is insulated by insulation cotton 409, when the biomass powder continuously falls to water mist sprayed by the water mist spray nozzle 410, carbon powder with high temperature and sensible heat meets the water mist and quickly extinguishes the water mist, and simultaneously generates a large amount of saturated steam, because the saturated steam is blocked by the third screw conveyor 411 and the material in a closed manner in a descending manner, the saturated steam only can ascend, when the saturated steam ascends to the deep carbonization bin 412, the saturated steam reacts with hot C and CO at a temperature of more than 800 ℃, and a certain amount of H2 and CO are generated by cracking, the hydrogen-containing mixed gas continuously goes upward until passing through the deep carbonization bin 412 and the blanking settling hopper 407, and then enters the gas chamber 406 to be discharged out of the suspended boiling pyrolysis furnace 402 to form hydrogen-rich mixed gas.
The water mist nozzle 410 is used for quenching charcoal and reducing temperature, and the amount of sprayed mist water can be adjusted, so that the water content of the generated biochar is controlled to be 12-15%, and subsequent storage and transportation or granule extrusion of the biochar products are facilitated. The water cooling jacket 422 is indirectly cooled circularly, the biochar is cooled to 30-50 ℃, and the biochar is discharged through a third screw conveyor 411.
(5) The high-temperature hydrogen-rich clean gas in the high-temperature resistant cyclone dust collector 5 is subjected to heat exchange and cooling through a high-temperature heat exchanger 6 to obtain low-temperature hydrogen-rich clean gas, the low-temperature hydrogen-rich clean gas enters a heat exchanger 7 for cooling, the high-purity hydrogen-rich biological gas with the concentration of 98.00 percent in total is subjected to pressurization to 1.0-1.2 MPa through a compressor 10, the high-purity hydrogen-rich biological gas enters a first adsorption tower 11 and a second adsorption tower 12, and 99.99 percent high-purity hydrogen is obtained at the outlet of a second pure hydrogen tank 14 and serves as regenerated, circulated, clean and green hydrogen energy sources which directly correspond to hydrogen metallurgy and can be compressed into liquid pure hydrogen to be used as clean green hydrogen energy automobiles and other hydrogen energy fuels.
CO + CH is separated from the first adsorption tower 11 and the second adsorption tower 12 4 The other high-concentration non-hydrogen gas may be used as the third burner 423 to heat the heating chamber 424. About 0.5 Nm/kg of organic hydrocarbon waste material can be obtained 3 The high-purity hydrogen-rich biogas with the concentration of more than 98 percent has the heat value of 4200-4500 Kcal/Nm 3 And each kilogram of organic hydrocarbon waste material is pyrolyzed and gasified to obtain 2100-2250 Kcal/Nm 3 Heat of the biogas. In the pyrolysis gasification process, each kilogram of organic hydrocarbon waste material needs to absorb about 500-700 Kcal/Nm 3 The heat of the organic hydrocarbon material is generated by pyrolysis gasification of the self-produced high-purity biogas and PSA pressure swing adsorption of the separated CO + CH 4 + other non-hydrogen combustible gases, a portion of the heat may be used for other purposes in addition to satisfying its own application.
The organic hydrocarbon waste is thermally cracked and gasified at 900 ℃ to generate biological high-purity fuel gas with the main components shown in the table 1.
The invention also adds the working procedure of carbon quenching to promote the generation of hydrogen, and the finally obtained hydrogen-rich gas has higher concentration.
Main components of biomass hydrogen-rich high-purity fuel gas table 1
Adding the hydrogen-rich high-purity biogas to 1.0-1.2 MPa by an air compressor, and performing PSA (pressure swing adsorption) to obtain pure hydrogen and CO + CH with the purity of more than 99.99 percent at most 4 + other mixed high purity non-hydrogen bio-combustible gases. The hydrogen with the purity of 99.99 percent can be directly used for hydrogen metallurgy, and can also be subjected to pressure liquefaction treatment to obtain liquid hydrogen energy for hydrogen energy automobiles or other uses.
The biochar obtained by high-temperature pyrolysis gasification of hydrocarbon wastes such as biomass materials and organic garbage per ton can produce 200-350 kg according to the ash content and the fixed carbon content of the materials entering the furnace. According to the fixed carbon and volatile matter content of hydrocarbon waste fed into the furnace, the temperature and time of thermal cracking gasification are different, the biochar can generally form charcoal, activated carbon, semi coke, formed coke, biomass carbon, carbon-based fertilizer or bio-organic fertilizer and other products with different qualities, and the high-quality biochar of the charcoal, the activated carbon, the semi coke and the formed coke can be used as clean biochar and has wide application. If the ash content in the hydrocarbon organic compound fed into the furnace is high, the dry distillation residue is the carbon-based fertilizer or the raw base fertilizer, and the carbon-based fertilizer or the raw base fertilizer is used as the carbon-based organic fertilizer, so that the carbon-based fertilizer can not only fertilize the soil, is beneficial to the rapid growth of plants, but also can fix carbon and reduce emission, the fixed carbon can be locked in the soil for hundreds of years and thousands of years and can not be decomposed any more, and the CO which is 3.66 times of the fixed carbon can be relatively reduced 2 The discharge amount is shown in Table 2.
Main indexes of corn stalk biomass charcoal table 2
The above description is only a preferred embodiment of the present invention, and is not intended to limit the scope of the present invention.
Claims (8)
1. The utility model provides a pure hydrogen and polygeneration coupled system are prepared to biomass waste which characterized in that: adding dry-based biomass powder into the inlet end of a pre-cracking gasification mechanism (3) and carrying out pre-cracking gasification on the dry-based biomass powder, wherein a smoke outlet of the pre-cracking gasification mechanism (3) is communicated with the inlet end of a sub-temperature heat exchanger (2), a first outlet end of the sub-temperature heat exchanger (2) is communicated with the smoke outlet mechanism (1), an outlet end of the pre-cracking gasification mechanism (3) is communicated with the inlet end of a carbonization hydrogen production mechanism (4), the carbonization hydrogen production mechanism (4) carries out suspension boiling thermal cracking gasification, carbonization and hydrogen production on the biomass powder after pre-cracking gasification, a smoke outlet of the carbonization hydrogen production mechanism (4) is communicated with the inlet end of a high-temperature resistant cyclone dust collector (5), an outlet end of the high-temperature resistant cyclone dust collector (5) is communicated with the inlet end of a heat exchanger (7) through a high-temperature heat exchanger (6), and an outlet end of the heat exchanger (7) is communicated with the inlet end of a washing tower (8) through a draught fan (16), the outlet end of a washing tower (8) is communicated with the inlet end of a steam-water separator (9), the outlet end of the steam-water separator (9) is communicated with the inlet end of a first adsorption tower (11) through a compressor (10), the first outlet end of the first adsorption tower (11) is communicated with the inlet end of a first pure hydrogen tank (13), the outlet end of the first pure hydrogen tank (13) is communicated with the inlet end of a second pure hydrogen tank (14), the second outlet end of the first adsorption tower (11) is communicated with the inlet end of a gas storage tank (15), the first outlet end of the second adsorption tower (12) is communicated with the inlet end of the first pure hydrogen tank (13), the second outlet end of the second adsorption tower (12) is communicated with the inlet end of the gas storage tank (15), and the outlet end of the gas storage tank (15) is communicated with the inlet end of a heat exchanger (7).
2. The coupling system for preparing pure hydrogen and poly-generation by using biomass waste as claimed in claim 1, wherein the pre-cracking gasification mechanism (3) comprises: a second spiral conveyor (308) for conveying dry-based biomass powder is arranged at the inlet end of the muffle-type rotary kiln (301), the muffle-type rotary kiln (301) carries out pre-thermal cracking gasification on the dry-based biomass powder, a first spiral conveyor (306) for conveying the biomass powder subjected to pre-thermal cracking gasification to the hydrogen production carbonization mechanism (4) is arranged at the outlet end of a kiln head cover (303) at one end of the muffle-type rotary kiln (301), and the output end of the first spiral conveyor (306) is communicated with the inlet end of the hydrogen production carbonization mechanism (4) through a front discharging pipe (305);
the second outlet end of the sub-temperature heat exchanger (2) is communicated with the inlet end of the hydrogen production carbonization mechanism (4), and the gas outlet of the muffle type rotary kiln (301) is communicated with the first burner (307) at the bottom of the muffle type rotary kiln (301) and the inlet end of the hydrogen production carbonization mechanism (4) through a gas fan (302).
3. The coupling system for preparing pure hydrogen and poly-generation from biomass waste as claimed in claim 2, wherein: the temperature of the muffle type rotary kiln (301) is 400-800 ℃, and the running time of the dry-based biomass powder in the muffle type rotary kiln (301) is 6-12 min.
4. The coupling system for preparing pure hydrogen and poly-generation by using biomass wastes according to claim 2, wherein the carbonization hydrogen-production mechanism (4) comprises: a rear retaining wall (414) and a front retaining wall (416) are arranged in the suspension boiling pyrolysis furnace (402), a side boiling bed (419) is arranged on the inner side wall of the suspension boiling pyrolysis furnace (402), an air pipe (425) is uniformly arranged on the side boiling bed (419), a front boiling bed (426) is arranged between the front retaining wall (416) and the side boiling bed (419), a front hot air bin (418) is arranged on the lower side of the front boiling bed (426), a rear boiling bed (428) is arranged between the rear retaining wall (414) and the front retaining wall (416), a rear hot air bin (415) is arranged on the lower side of the rear boiling bed (428), air caps (427) are uniformly arranged on the front boiling bed (426) and the rear boiling bed (428), a partition wall (403) and a smoke partition wall (405) which divide the interior of the suspension boiling pyrolysis furnace (402) into a front boiling chamber (401), a rear boiling chamber (404), a chamber (406) are arranged in the suspension boiling pyrolysis furnace (402), the front boiling chamber (401) is communicated with the rear boiling chamber (404), the front boiling chamber (401) is positioned on the upper sides of a front boiling bed (426) and a rear boiling bed (428), the rear boiling chamber (404) and a fuel gas chamber (406) are respectively communicated with a blanking settling hopper (407), the blanking settling hopper (407) is communicated with a deep carbonization bin (412) positioned below the blanking settling hopper (407), an air inlet annular pipe (408) is positioned in a heating chamber (424) of the suspension boiling pyrolysis furnace (402), one side of the suspension boiling pyrolysis furnace (402) is provided with the air inlet annular pipe (408), the heating chamber (424) is provided with a heat exchange branch pipe (413) positioned in the circumferential direction of the deep carbonization bin (412), and the heat exchange branch pipe (413) is communicated with the air inlet annular pipe (408);
the smoke outlet of the heating chamber (424) is communicated with the inlet end of the kiln head cover (303) through a high-temperature fan (304), the second outlet end of the sub-temperature heat exchanger (2) is communicated with the inlet end of the heating chamber (424), and the gas outlet of the muffle type rotary kiln (301) is communicated with a second burner (417) and a third burner (423) of the heating chamber (424) through a gas fan (302);
the outlet end of the high-temperature heat exchanger (6) is communicated with the heating chamber (424) through a combustion fan (429), the outlet end of the high-temperature resistant cyclone dust collector (5) is communicated with the air inlet annular pipe (408) through an air pressure increasing fan (430), and the outlet end of the heat exchanger (7) is communicated with the third burner (423) through a coal gas fan (431).
5. The coupling system for preparing pure hydrogen and poly-generation by using biomass wastes according to claim 4 is characterized in that: the outlet end of the gas chamber (406) is communicated with the inlet end of the high-temperature resistant cyclone dust collector (5), the outlet end of the bottom of the high-temperature resistant cyclone dust collector (5) is provided with a fourth screw conveyor (420), and the outlet end of the fourth screw conveyor (420) is communicated with the gas chamber (406) through a rear discharging pipe (421).
6. The coupling system for preparing pure hydrogen and poly-generation by using biomass wastes according to claim 4 is characterized in that: the temperature of the front boiling chamber (401) is 800-950 ℃, and the wind speed is 0.8-2.0 m/s.
7. The coupling system for preparing pure hydrogen and poly-generation from biomass waste as claimed in claim 4, wherein: the deep carbonization bin (412) is provided with a third screw conveyor (411) for conveying biochar at the bottom, heat-preservation cotton (409) is arranged in the circumferential direction of the deep carbonization bin (412) positioned outside the suspension boiling pyrolysis furnace (402), a water cooling jacket (422) positioned below the heat-preservation cotton (409) is arranged in the circumferential direction of the deep carbonization bin (412), and a water spray nozzle (410) communicated with the water cooling jacket (422) is arranged inside the deep carbonization bin (412).
8. The coupling system for preparing pure hydrogen and poly-generation by using biomass waste as claimed in claim 1, wherein the smoke exhaust mechanism (1) comprises: the first outlet end of the sub-temperature heat exchanger (2) is communicated with the inlet end of a cyclone dust collector (103), the outlet end of the cyclone dust collector (103) is communicated with the inlet end of a bag-type dust collector (102), and the outlet end of the bag-type dust collector (102) is communicated with the inlet end of a chimney (101) through an exhaust fan (104).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210796954.2A CN115109606B (en) | 2022-07-06 | 2022-07-06 | Pure hydrogen and poly-generation coupling system prepared from biomass waste |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210796954.2A CN115109606B (en) | 2022-07-06 | 2022-07-06 | Pure hydrogen and poly-generation coupling system prepared from biomass waste |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN115109606A true CN115109606A (en) | 2022-09-27 |
| CN115109606B CN115109606B (en) | 2023-09-08 |
Family
ID=83332884
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210796954.2A Active CN115109606B (en) | 2022-07-06 | 2022-07-06 | Pure hydrogen and poly-generation coupling system prepared from biomass waste |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115109606B (en) |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR1029308A (en) * | 1950-01-04 | 1953-06-02 | Koppers Gmbh Heinrich | Combined gas and steam generator |
| GB704047A (en) * | 1951-07-14 | 1954-02-17 | Koppers Co Inc | Improvements in or relating to recirculation underjet coking retort oven |
| KR950008661A (en) * | 1993-09-11 | 1995-04-19 | 오정무 | Bituminous coal two-stage pyrolysis method and apparatus |
| JP2001049262A (en) * | 1999-08-10 | 2001-02-20 | Giichi Suzuki | Equipment for treatment of renedering charcoal furnace exhaust gas smokeless and harmless and waste-heat utilization plant |
| CN102134497A (en) * | 2010-02-23 | 2011-07-27 | 山西工霄商社有限公司 | Crop straw carbonizing method and device |
| CN104017590A (en) * | 2014-06-24 | 2014-09-03 | 华南农业大学 | Continuous pyrolysis carbonization method of agricultural and forestal biomasses |
| CN105505415A (en) * | 2016-02-03 | 2016-04-20 | 江苏河海给排水成套设备有限公司 | Multi-section pyrolysis, boiling, carbonization and secondary oxidization treatment device for garbage |
| CN208260255U (en) * | 2018-04-16 | 2018-12-21 | 南京红森林食品有限公司 | A kind of cake semi-finished product conveying precipitation separation device |
| CN213089807U (en) * | 2020-08-13 | 2021-04-30 | 武汉安洋科技有限责任公司 | Fluidized bed furnace based on fluidized bed combustion technology optimizes fluidized bed structure |
| CN113136230A (en) * | 2020-01-17 | 2021-07-20 | 北京航天石化技术装备工程有限公司 | Garbage pyrolysis process system |
| CN113862009A (en) * | 2021-10-28 | 2021-12-31 | 烟台市红森林节能环保科技有限公司 | Method for preparing green hydrogen energy and co-producing biochar by pyrolysis and gasification of organic waste III |
-
2022
- 2022-07-06 CN CN202210796954.2A patent/CN115109606B/en active Active
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR1029308A (en) * | 1950-01-04 | 1953-06-02 | Koppers Gmbh Heinrich | Combined gas and steam generator |
| GB704047A (en) * | 1951-07-14 | 1954-02-17 | Koppers Co Inc | Improvements in or relating to recirculation underjet coking retort oven |
| KR950008661A (en) * | 1993-09-11 | 1995-04-19 | 오정무 | Bituminous coal two-stage pyrolysis method and apparatus |
| JP2001049262A (en) * | 1999-08-10 | 2001-02-20 | Giichi Suzuki | Equipment for treatment of renedering charcoal furnace exhaust gas smokeless and harmless and waste-heat utilization plant |
| CN102134497A (en) * | 2010-02-23 | 2011-07-27 | 山西工霄商社有限公司 | Crop straw carbonizing method and device |
| CN104017590A (en) * | 2014-06-24 | 2014-09-03 | 华南农业大学 | Continuous pyrolysis carbonization method of agricultural and forestal biomasses |
| CN105505415A (en) * | 2016-02-03 | 2016-04-20 | 江苏河海给排水成套设备有限公司 | Multi-section pyrolysis, boiling, carbonization and secondary oxidization treatment device for garbage |
| CN208260255U (en) * | 2018-04-16 | 2018-12-21 | 南京红森林食品有限公司 | A kind of cake semi-finished product conveying precipitation separation device |
| CN113136230A (en) * | 2020-01-17 | 2021-07-20 | 北京航天石化技术装备工程有限公司 | Garbage pyrolysis process system |
| CN213089807U (en) * | 2020-08-13 | 2021-04-30 | 武汉安洋科技有限责任公司 | Fluidized bed furnace based on fluidized bed combustion technology optimizes fluidized bed structure |
| CN113862009A (en) * | 2021-10-28 | 2021-12-31 | 烟台市红森林节能环保科技有限公司 | Method for preparing green hydrogen energy and co-producing biochar by pyrolysis and gasification of organic waste III |
Non-Patent Citations (3)
| Title |
|---|
| 姜伟忠;袁正仲;: "焦炉炭化室密封料的研究与应用", 宝钢技术, no. 01 * |
| 孟光范;赵保峰;张晓东;陈雷;许海朋;孙立;: "生物质二次裂解制取氢气的研究", 太阳能学报, vol. 30, no. 06 * |
| 曹柏林, 严祝贵, 王永义, 吴龙友: "内分离循环沸腾床分离器的试验研究", 化工学报, no. 04 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN115109606B (en) | 2023-09-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102703131B (en) | Two-stage gasification method and gasification device for fuels with wide size distribution | |
| CN100381352C (en) | Method and device for plasma producing hydrogen by using garbage biomass and water as raw material | |
| CN101100621A (en) | Method and device for preparing biomass hydrogen-rich combustion gas | |
| WO2012010058A1 (en) | Method and apparatus for biomass pyrolysis gasification via two interconnected furnaces | |
| CN102977927A (en) | Apparatus for preparing synthesis gas based on dual fluidized bed biomass gasification and preparation method thereof | |
| CN1888017B (en) | Cracking and gasifying reforming furnace | |
| CN108531220B (en) | System and method for biomass microwave pyrolysis high-yield gas | |
| CN105885950B (en) | A kind of three combination pyrolytic gasifications of solid waste and coke tar cracking integral system | |
| CN101407722A (en) | Biomass high temperature pyrolysis and gasification and high temperature pyrolysis gas catalytic purification system | |
| CN103666505A (en) | Equipment for reducing and transforming household garbage or organic waste into energy resources | |
| CN105710114B (en) | Domestic garbage and agricultural and forestry waste carbonization cycle comprehensive treatment system and method | |
| CN112961695A (en) | Solid waste anaerobic pyrolysis and high-temperature melting treatment process and system | |
| CN110903855A (en) | Material pyrolysis gasification process, system and application | |
| CN101885975A (en) | Device and process for bio-oil and carbon powder coproduction | |
| CN110616089B (en) | Gasification device for producing synthesis gas from high-moisture organic material | |
| CN107202325B (en) | Rotary controllable pyrolysis carbonization kiln | |
| CN106987280A (en) | A kind of system and method for fluid bed refuse pyrolysis | |
| CN104479742B (en) | Biomass gas preparation system | |
| CN101974351A (en) | Scale fixed bed biomass gasification power generation production technology and complete equipment | |
| CN102260538B (en) | Method and device for air-floatation flow-state high-temperature heat-transfer gasification of biomass | |
| CN101967402A (en) | Biomass gasification reaction system | |
| CN115109606B (en) | Pure hydrogen and poly-generation coupling system prepared from biomass waste | |
| CN113732014A (en) | Clean gasification power generation method and device for household garbage | |
| CN1207370C (en) | Method and device for gasifying coal | |
| CN202465607U (en) | External heating type microwave plasma gasification furnace |
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 |