CN113150832A - Self-heating three-section type biomass low-tar carbon gas co-production regulation and control device - Google Patents
Self-heating three-section type biomass low-tar carbon gas co-production regulation and control device Download PDFInfo
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- 239000002028 Biomass Substances 0.000 title claims abstract description 62
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 43
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 27
- 238000010438 heat treatment Methods 0.000 title claims abstract description 18
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 18
- 230000033228 biological regulation Effects 0.000 title claims description 8
- 238000000197 pyrolysis Methods 0.000 claims abstract description 112
- 238000002309 gasification Methods 0.000 claims abstract description 98
- 239000007789 gas Substances 0.000 claims abstract description 63
- 238000000034 method Methods 0.000 claims abstract description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 30
- 238000002407 reforming Methods 0.000 claims abstract description 28
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 20
- 230000003647 oxidation Effects 0.000 claims abstract description 19
- 238000009826 distribution Methods 0.000 claims abstract description 17
- 230000001105 regulatory effect Effects 0.000 claims abstract description 14
- 230000001276 controlling effect Effects 0.000 claims abstract description 13
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 10
- 238000005336 cracking Methods 0.000 claims abstract description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 22
- 229910052757 nitrogen Inorganic materials 0.000 claims description 11
- 239000000463 material Substances 0.000 claims description 10
- 239000002994 raw material Substances 0.000 claims description 10
- 239000000919 ceramic Substances 0.000 claims description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 8
- 239000001301 oxygen Substances 0.000 claims description 8
- 229910052760 oxygen Inorganic materials 0.000 claims description 8
- 238000001914 filtration Methods 0.000 claims description 7
- 238000006479 redox reaction Methods 0.000 claims description 7
- 238000012423 maintenance Methods 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
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- 238000006243 chemical reaction Methods 0.000 abstract description 15
- 230000015572 biosynthetic process Effects 0.000 abstract description 6
- 238000003786 synthesis reaction Methods 0.000 abstract description 6
- 238000002485 combustion reaction Methods 0.000 abstract description 5
- 238000006722 reduction reaction Methods 0.000 abstract description 5
- 239000000571 coke Substances 0.000 abstract description 4
- 230000003321 amplification Effects 0.000 abstract description 3
- 238000004523 catalytic cracking Methods 0.000 abstract description 3
- 238000003199 nucleic acid amplification method Methods 0.000 abstract description 3
- 239000012429 reaction media Substances 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- 238000011161 development Methods 0.000 description 4
- 238000011065 in-situ storage Methods 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 2
- 239000003575 carbonaceous material Substances 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 230000008646 thermal stress Effects 0.000 description 2
- 230000006978 adaptation Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000001754 furnace pyrolysis Methods 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
- C10J2300/092—Wood, cellulose
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Industrial Gases (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses an autothermal three-stage biomass low-tar carbon gas co-production regulating and controlling device which comprises an autothermal fluidized bed pyrolysis reactor, a homogeneous partial oxidation reforming reactor and a fixed bed gasification reactor. The fluidized bed pyrolysis reactor adopts air and water vapor as reaction media; the partial oxidation reforming section generates strong partial combustion reaction through pure oxygen and volatile components, releases a large amount of heat and promotes the tar to generate strong cracking; the biomass coke generated in the pyrolysis section enters the gasification reduction section through the gas locking and returning device, a small amount of residual tar after the gasification reduction reaction is subjected to deep catalytic cracking through the carbon bed, and the tar content at the outlet of the gasification furnace reaches an extremely low level. The invention converts the agriculture and forestry biomass waste into the synthesis gas and the biomass activated carbon with high added values in a sectional conversion mode, realizes self-heating and large-scale amplification of the pyrolysis process of the gasification furnace by utilizing the directional distribution of gasification media, and simultaneously realizes the efficient in-furnace removal of tar.
Description
Technical Field
The invention relates to the technical field of biomass gasification, in particular to a self-heating three-section type biomass low-tar carbon gas co-production regulating and controlling device.
Background
The high tar content and the low gasification efficiency are bottlenecks which restrict the industrial development of the biomass gasification technology. The traditional tar purification and removal methods comprise a water washing method, a ceramic filtration method, a thermal cracking method and a catalytic cracking method, and the methods bring various problems such as environmental pollution, system cost increase and the like. The development of a tar removal process with high efficiency and low cost becomes a key. At present, it is internationally generally accepted that a segmented gasification technology decomposes and combines pyrolysis, combustion and gasification processes of biomass, and can reduce tar content in a furnace. However, the traditional sectional gasification has small scale, is difficult to effectively enlarge, and simultaneously has lower gasification efficiency. The key point for solving the scale enlargement of the gasification furnace is the heating mode in the pyrolysis process, the preheating/heating of the fuel in the pyrolysis section of the traditional gasification furnace adopts an external heat conduction mode, and the biomass heating temperature rising rate is slow due to low biomass heat conductivity, the required retention time is long, the pyrolysis rate is slow, and the size of the gasification furnace is difficult to enlarge. Therefore, the development of advanced high-efficiency pyrolysis technology becomes critical. In addition, the gasification reaction in the sectional gasification furnace is an endothermic process, and as the reaction proceeds, the temperature of the gasification region decreases, resulting in a decrease in gasification efficiency and a low carbon conversion rate. In addition, biomass is used as a high-quality resource, energy conversion is carried out in a pyrolysis gasification mode, and carbon materials with high added values, such as biomass activated carbon, carbon catalyst carriers and the like, can be produced through specific operation regulation. The carbon gas co-production regulation and control technology based on the biomass gasification technology is also an important direction for biomass resource utilization in the future.
Therefore, the method improves the conversion efficiency of each stage of pyrolysis, combustion and gasification in the sectional gasification process, improves the in-situ cracking of tar in the furnace, and jointly produces the biomass carbon-based material with high added value through the adjustment of process parameters, thereby becoming the key for the development of the biomass sectional gasification technology.
Disclosure of Invention
The purpose of the invention is as follows: the invention discloses a self-heating three-section type low-tar carbon gas co-production regulation and control system aiming at the problems of high tar content and low gasification efficiency in the existing biomass gasification technology. Meanwhile, by controlling the air equivalence ratio and the water vapor in the gasification process, biomass activated carbon with high added value can be generated, so that the problems of low carbon conversion rate and low gasification efficiency in the gasification process are solved.
The technical scheme is as follows: an autothermal three-stage biomass low-tar carbon gas co-production regulating device comprises a fluidized bed pyrolysis reactor, a reforming reactor and a gasification reactor which are sequentially connected, wherein two ends of the reforming reactor are respectively connected with the upper end parts of the fluidized bed pyrolysis reactor and the gasification reactor; one side of the fluidized bed pyrolysis reactor is connected with a spiral feeder, the lower part of the fluidized bed pyrolysis reactor is provided with a fluidized bed air distribution plate, and the lower end part of the fluidized bed pyrolysis reactor is respectively provided with a pyrolysis air inlet and a pyrolysis water vapor inlet; a plurality of nozzles are uniformly arranged on the side wall of the reforming reactor in the length direction; a U-shaped material returning device is arranged between the fluidized bed pyrolysis reactor and the gasification reactor, and a nitrogen inlet and a first air inlet are respectively arranged on the U-shaped material returning device; the lower part of the gasification reactor is provided with a grate, the lower end part of the gasification reactor is provided with a discharge hole, one side of the gasification reactor is provided with a gasified gas outlet, the gasified gas outlet is connected with one end of a heat exchanger, the other end of the heat exchanger is connected with one end of a ceramic filtering device, and the other end of the ceramic filtering device is connected with a synthetic gas outlet.
Preferably, the lower end part of the fluidized bed pyrolysis reactor is respectively provided with a pyrolysis air inlet and a pyrolysis water vapor inlet, air and water vapor are used as pyrolysis reaction gas for oxidation-reduction reaction in the pyrolysis process, and the heat self-maintenance in the pyrolysis process is realized by adjusting the ratio of air/water vapor/biomass raw material; the air equivalence ratio is controlled to be between 0.08 and 0.15.
Preferably, in the reforming reactor, pure oxygen passes through the tangential nozzles, the number of the nozzles is 4-6, the oxygen equivalence ratio is adjusted within the range of 0-0.4, the control range is generally 0.2-0.3, the pure oxygen and tar and pyrolysis gas generated in the pyrolysis reactor undergo severe oxidation-reduction reaction to form high temperature of 1100-1200 ℃, and the tar is subjected to intense pyrolysis.
Preferably, the U-shaped return valve of the present invention uses a mixture of nitrogen, air and steam as the fluidizing gas to adjust the product distribution in the gasification reactor.
Preferably, the U-shaped return valve is used for separating the pyrolysis semicoke in the pyrolysis reactor and conveying the pyrolysis semicoke to the gasification reactor, and nitrogen/air/water vapor is used as fluidizing gas of the return valve, wherein the air equivalence ratio is adjusted within the range of 0-0.2, and the water vapor/biomass ratio is adjusted within the range of 0-1.
Preferably, the height of the bed in the gasification reactor according to the invention is controlled by the discharge velocity of the grate, the height of the bed being controlled between 700mm and 1000 mm.
Preferably, the heat exchanger of the invention is provided with a cold air inlet, the pyrolysis air inlet is connected with a hot air outlet of the heat exchanger, the nozzle is connected with an oxygen outlet of the heat exchanger, and the first air inlet is connected with an air outlet of the heat exchanger.
Preferably, the tar cracked by the oxidation reforming reactor is further catalytically cracked in a bed layer to realize deep removal of the tar; the product distribution in the fixed bed gasification reactor is realized by controlling the discharging speed and the air/steam equivalent ratio of the return valve.
Has the advantages that:
1. the invention relates to an autothermal three-stage biomass low-tar carbon gas co-production regulating and controlling device which is respectively an autothermal fluidized bed pyrolysis reactor, a homogeneous phase partial oxidation reforming reactor and a fixed bed gasification reactor. The fluidized bed pyrolysis reactor adopts air and steam as reaction media, generates heat through partial oxidation of biomass raw materials, and maintains the temperature required by the pyrolysis reaction. The volatile component (containing tar) generated by pyrolysis enters a partial oxidation reforming section, and strong partial combustion reaction is generated between pure oxygen and the volatile component to release a large amount of heat, so that a high-temperature oxidation area is formed, and the strong cracking of the tar is promoted. The biomass coke generated in the pyrolysis section enters the gasification reduction section through the gas locking and returning deviceIn the reactor, the biomass coke, carbon dioxide, water vapor and the like are subjected to gasification reduction reaction, the residual small amount of tar is subjected to deep catalytic cracking through a carbon bed, and the content of the tar at the outlet of the gasification furnace reaches an extremely low level (lower than 25 mg/Nm)3). Meanwhile, by controlling the proportion of the gasification medium, the incomplete gasification of the biomass coke can be realized, and the biomass activated carbon with porosity can be generated.
2. According to the invention, a certain amount of air/water vapor is sprayed into the fluidized bed pyrolysis reactor, so that a certain amount of heat can be released by utilizing the in-situ oxidation pyrolysis reaction of the biomass raw material to maintain the energy self-balance of the pyrolysis process, the pyrolysis temperature is controlled to be maintained between 500 ℃ and 600 ℃, and the full separation of volatile components in the biomass is ensured. The limit of heat supply of an external heat source in the traditional gasification furnace pyrolysis process can be overcome, the pyrolysis efficiency of the gasification furnace can be obviously improved, and the gasification furnace is suitable for structure amplification of the gasification furnace. Simultaneously, air and water vapor have a pore-forming effect on the semicoke in the biomass pyrolysis process, the generation of semicoke pores is facilitated, the subsequent gasification and the generation of activated carbon are obviously promoted, and the specific surface area of the biomass semicoke can reach 500m2More than g;
3. the U-shaped material return valve is used for connecting a fluidized bed pyrolysis reactor and a fixed bed gasification reactor, and is used for conveying pyrolysis semicoke and isolating volatile components. Meanwhile, the return speed and the reaction characteristics in the gasification reactor can be controlled by adjusting the flow of the fluidizing gas of the return valve, and the distribution of products at the outlet of the gasification furnace and the quality of the active carbon (indexes such as porosity, specific surface area and the like) are adjusted.
4. The invention designs a reasonable nozzle structure in the homogeneous phase partial oxidation reforming reactor, realizes the full mixing and combustion of pure oxygen and pyrolysis tar/combustible gas, generates high temperature, promotes the full cracking and conversion of the tar, and provides a high-temperature heat source for the subsequent gasification process.
5. The invention controls a reasonable carbon bed in the fixed bed gasification reactor, on one hand, the carbon bed is gasified to generate synthesis gas, on the other hand, the carbon bed can be used as a high-efficiency catalyst to deeply remove tar at the outlet of the homogeneous phase partial oxidation reforming reactor, thereby reducing the purification cost of the tar. Meanwhile, by controlling the gasification reaction time and the gasification medium flow, high-quality biomass activated carbon can be obtained, and the co-production regulation and control of carbon and gas are realized.
6. The invention converts the agriculture and forestry biomass waste into the synthesis gas and the biomass activated carbon with high added values in a sectional conversion mode, realizes self-heating and large-scale amplification of the pyrolysis process of the gasification furnace by utilizing the directional distribution of gasification media, and simultaneously realizes the efficient in-furnace removal of tar.
Drawings
FIG. 1 is a front view of the structure of the present invention;
FIG. 2 is a front view of a reforming reactor of the present invention;
FIG. 3 is a left side view of FIG. 2;
wherein, 1, a fluidized bed pyrolysis reactor; 2. a fluidized bed air distribution plate; 3. a biomass silo; 4. a screw feeder; 5. a pyrolysis air inlet; 6. a pyrolysis water vapor inlet; 7. a U-shaped material returning device; 8. a reforming reactor; 9. insulating layer: 10. a nozzle; 11. a nitrogen inlet; 12. a first air inlet; 13. A gasification reactor; 14. a grate; 15 is a gasified gas outlet; 16 is a discharge hole; 17 is a heat exchanger; 18 is a cold air inlet; 19 is a ceramic filter device; and 20 is a synthesis gas outlet.
Detailed Description
As shown in fig. 1, fig. 2 and fig. 3, the autothermal three-stage biomass low-tar carbon gas co-production regulating device comprises a fluidized bed pyrolysis reactor 1, a reforming reactor 8 and a gasification reactor 13 which are connected in sequence, wherein two ends of the reforming reactor 8 are respectively connected with the upper end parts of the fluidized bed pyrolysis reactor 1 and the gasification reactor 13; one side of the fluidized bed pyrolysis reactor 1 is connected with a screw feeder 4, the lower part of the fluidized bed pyrolysis reactor 1 is provided with a fluidized bed air distribution plate 2, and the lower end part of the fluidized bed pyrolysis reactor 1 is respectively provided with a pyrolysis air inlet 5 and a pyrolysis water vapor inlet 6; a plurality of nozzles 10 are uniformly arranged on the side wall of the reforming reactor 8 in the length direction; a U-shaped material returning device 7 is arranged between the fluidized bed pyrolysis reactor 1 and the gasification reactor 13, and a nitrogen inlet 11 and a first air inlet 12 are respectively arranged on the U-shaped material returning device 7; the lower part of the gasification reactor 13 is provided with a grate 14, the lower end part of the gasification reactor 13 is provided with a discharge hole 16, one side of the gasification reactor 13 is provided with a gasified gas outlet 15, the gasified gas outlet 15 is connected with one end of a heat exchanger 17, the other end of the heat exchanger 17 is connected with one end of a ceramic filtering device 19, and the other end of the ceramic filtering device 19 is connected with a synthetic gas outlet 20.
The self-heating three-section biomass low-tar carbon gas co-production regulating device comprises a biomass self-heating fluidized bed pyrolysis reactor 1, wherein the fluidized bed pyrolysis reactor is used for feeding materials through a spiral feeder 4, a fluidized bed air distribution plate 2 is arranged in the biomass self-heating fluidized bed pyrolysis reactor and is used for distributing air of fluidized gas, and the fluidized bed adopts mixed gas of a pyrolysis air inlet 5 and a pyrolysis water vapor inlet 6 as the fluidized gas and reaction gas in the pyrolysis process; the tar and combustible gas produced by the pyrolysis reactor enter the upper horizontal homogeneous partial oxidation reforming reactor 8 and undergo a severe oxidation reaction with hot air introduced through the nozzle 10 to produce carbon dioxide, water vapor and the like. The biomass semicoke generated by the pyrolysis reactor is sent into a fixed bed gasification reactor 13 through a U-shaped material returning device 7 for gasification and reduction to generate synthesis gas and active carbon. The U-shaped return valve uses a mixture of the nitrogen inlet 11, the first air inlet 12 and water vapor as a fluidizing gas for adjusting the product distribution in the gasification reactor. The height of the bed in the gasification reactor is controlled by the discharge velocity of the grate 14, typically between 700mm and 1000 mm. The gasified gas is led out from a gasified gas outlet 15 at the lower part of the gasification reactor through a draught fan, and the active carbon or ash slag is discharged from a bottom discharge hole 16.
The pyrolysis reactor 1 of the present invention uses air and steam as a pyrolysis reaction atmosphere for an oxidation-reduction reaction in a pyrolysis process, and the biomass raw material undergoes self-heating aerobic pyrolysis, and the heat self-maintenance in the pyrolysis process is realized by adjusting the ratio of air/steam/biomass raw material. In the actual operation process, the air equivalence ratio is controlled to be 0.08-0.15, so that the energy self-balance of the process can be ensured, and the biomass can not be burnt out.
The oxidation reforming reactor 8 adopts pure oxygen to pass through the tangential nozzles 10, the number of the nozzles is 4-6, the adjustment range of the oxygen equivalence ratio is 0-0.4, the control range is generally 0.1-0.3, the pure oxygen and tar and pyrolysis gas generated in the pyrolysis reactor 1 generate violent oxidation-reduction reaction to form high temperature of about 1100-1200 ℃, and the tar is subjected to violent cracking. Specific reactions include, but are not limited to:
H2+0.5O2→H2O (R1)
CO+0.5O2→CO2 (R2)
CH4+O2→CO2+2H2O (R3)
CmHn (tar) + O2→CO2+CO+H2O+H2 (R4)
The U-shaped return valve 7 is used for separating pyrolysis semicoke in the pyrolysis reactor 1 and conveying the pyrolysis semicoke to the gasification reactor 13, and simultaneously preventing pyrolysis tar and combustible gas from directly entering the gasification reactor 13. And nitrogen/air/water vapor is used as the fluidizing gas of the feed back valve, wherein the adjusting range of the air equivalence ratio is 0-0.2, the adjusting range of the water vapor/biomass ratio is 0-1, and the optimized value depends on the characteristics of the biomass raw material and the distribution of a target product.
The fixed bed gasification reactor 13 of the invention controls the height of the bed layer to be between 700mm and 1000mm by controlling the discharge speed of the grate, and the tar cracked by the homogeneous phase partial oxidation reforming reactor 8 is further catalytically cracked in the bed layer, thereby realizing the deep removal of the tar. By controlling the discharge rate, the return valve air/steam equivalence ratio, product distribution in the fixed-bed gasification reactor 13 can be achieved.
A certain amount of air/water vapor is sprayed into the fluidized bed pyrolysis reactor 1, so that a certain amount of heat can be released by utilizing the in-situ oxidation pyrolysis reaction of the biomass raw material to maintain the energy self-balance of the pyrolysis process, the pyrolysis temperature is controlled to be maintained between 500 ℃ and 600 ℃, the full separation of volatile matters in the biomass is ensured, and the pyrolysis air equivalence ratio is generally 0.08-0.15 for the biomass raw materials with different heat values. The pyrolysis reactor is operated by adopting micro positive pressure (+100Pa), and the pyrolysis gas can flow to the partial oxidation reforming reactor 8. The screw feeder 4 and the pyrolysis reactor 1 are welded by using a corrugated pipe to overcome the deformation caused by thermal stress.
The homogeneous partial oxidation reforming reactor 8 adopts pure oxygen to pass through the tangential nozzles 10, the number of the nozzles is 4-6, the oxygen equivalence ratio is adjusted within the range of 0-0.4, the general control range is generally 0.1-0.3, the pure oxygen and tar and pyrolysis gas generated in the pyrolysis reactor 1 undergo severe oxidation-reduction reaction to form high temperature of about 1100-1200 ℃, and the tar is subjected to strong cracking. By the rotational flow mixing, the gas retention time is controlled to be not less than 0.2 second, and the lowest temperature of the interface cold zone is not less than 1000 ℃, so that the tar is fully mixed and cracked. The homogeneous partial oxidation reforming reactor 8, the pyrolysis reactor 1 and the fixed bed gasification reactor 13 are connected in a high temperature resistant bellows welding mode, and the sealing performance of the connection part under high temperature thermal stress is ensured.
And the U-shaped return valve 7 is used for separating the pyrolysis semicoke in the pyrolysis reactor 1 and conveying the pyrolysis semicoke to the gasification reactor 13, and simultaneously blocking the pyrolysis tar and combustible gas from directly entering the gasification reactor 13. And nitrogen/air/water vapor is used as the fluidizing gas of the feed back valve, wherein the adjusting range of the air equivalence ratio is 0-0.2, the adjusting range of the water vapor/biomass ratio is 0-1, and the optimized value depends on the characteristics of the biomass raw material and the distribution of a target product.
The fixed bed gasification reactor 13 controls the height of the bed layer to be 700mm-1000mm by controlling the discharge speed of the grate, and the tar cracked by the homogeneous phase partial oxidation reforming reactor 8 is further catalytically cracked in the bed layer to realize the deep removal of the tar. By controlling the discharge rate, the return valve air/steam equivalence ratio, product distribution in the fixed-bed gasification reactor 13 can be achieved. When biomass activated carbon is taken as a main target product, the equivalent ratio of the whole oxygen of the gasification furnace is 0.15-0.2; when the synthesis gas is taken as a main target product, the integral oxygen equivalence ratio of the gasification furnace is controlled to be 0.3-0.4. The outlet of the gasification furnace adopts a centrifugal fan to lead the synthetic gas out of the furnace and form a gas flow channel in the gasification furnace (1 → 8 → 13 → 15 → 20).
The temperature of the synthetic gas at the outlet of the gasification furnace is about 600-700 ℃. In order to effectively utilize the part of heat and improve the overall efficiency, a gas heat exchanger 17 is arranged at the outlet of the gasification furnace, and cold air 18 is heated to 300-600 ℃ and used for air in each stage of the gasification furnace. The cooled syngas is passed through a ceramic filter 19 to remove particulates and small residual amounts of tar.
The above description is only of the preferred embodiments of the present invention, and it should be noted that: it will be apparent to those skilled in the art that various modifications and adaptations can be made without departing from the principles of the invention and these are intended to be within the scope of the invention.
Claims (8)
1. The utility model provides a low tar charcoal gas coproduction regulation and control device of self-heating syllogic living beings which characterized in that: the device comprises a fluidized bed pyrolysis reactor (1), a reforming reactor (8) and a gasification reactor (13) which are connected in sequence, wherein two ends of the reforming reactor (8) are respectively connected with the upper end parts of the fluidized bed pyrolysis reactor (1) and the gasification reactor (13); one side of the fluidized bed pyrolysis reactor (1) is connected with a spiral feeder (4), the lower part of the fluidized bed pyrolysis reactor (1) is provided with a fluidized bed air distribution plate (2), and the lower end part of the fluidized bed pyrolysis reactor (1) is respectively provided with a pyrolysis air inlet (5) and a pyrolysis water vapor inlet (6);
a plurality of nozzles (10) are uniformly arranged on the side wall of the reforming reactor (8) in the length direction;
a U-shaped material returning device (7) is arranged between the fluidized bed pyrolysis reactor (1) and the gasification reactor (13), and a nitrogen inlet (11) and a first air inlet (12) are respectively arranged on the U-shaped material returning device (7);
the lower part of the gasification reactor (13) is provided with a grate (14), the lower end part of the gasification reactor (13) is provided with a discharge hole (16), one side of the gasification reactor (13) is provided with a gasified gas outlet (15), the gasified gas outlet (15) is connected with one end of a heat exchanger (17), the other end of the heat exchanger (17) is connected with one end of a ceramic filtering device (19), and the other end of the ceramic filtering device (19) is connected with a synthetic gas outlet (20).
2. The self-heating three-stage biomass low-tar carbon gas co-production regulating device as claimed in claim 1, wherein the lower end of the fluidized bed pyrolysis reactor (1) is provided with a pyrolysis air inlet (5) and a pyrolysis water vapor inlet (6), respectively, air and water vapor are used as pyrolysis reaction gas for oxidation-reduction reaction in the pyrolysis process, and the self-maintenance of heat in the pyrolysis process is realized by adjusting the ratio of air/water vapor/biomass raw material; the air equivalence ratio is controlled to be between 0.08 and 0.15.
3. The self-heating three-stage biomass low-tar carbon gas co-production regulating device as claimed in claim 2, wherein the reforming reactor (8) is used for generating a severe redox reaction with tar and pyrolysis gas generated in the pyrolysis reactor (1) by passing pure oxygen through a tangential nozzle (10), the number of the nozzles is 4-6, the oxygen equivalence ratio regulating range is 0-0.4, and the control range is generally 0.2-0.3, so as to form a high temperature of 1100-1200 ℃, and the tar is subjected to a severe cracking.
4. The autothermal three-stage biomass low-tar char gas co-production regulation device of claim 1, wherein the U-shaped return valve (7) uses a mixture of nitrogen, air and steam as a fluidizing gas to regulate product distribution in the gasification reactor.
5. The self-heating three-stage biomass low-tar carbon gas co-production regulating device as claimed in claim 4, wherein the U-shaped return valve (7) is used for separating the pyrolysis semicoke in the pyrolysis reactor (1) and conveying the pyrolysis semicoke to the gasification reactor (13), and nitrogen/air/water vapor is used as a return valve fluidizing gas, wherein the air equivalence ratio regulating range is 0-0.2, and the water vapor/biomass ratio regulating range is 0-1.
6. The autothermal three-stage biomass low-tar char gas co-production control device according to claim 1, characterized in that the bed height in the gasification reactor (13) is controlled by the discharge velocity of the grate (14), and the bed height is controlled between 700mm and 1000 mm.
7. The self-heating three-stage biomass low-tar carbon gas co-production regulating device as claimed in claim 1, wherein the heat exchanger (17) is provided with a cold air inlet (18), the pyrolysis air inlet (5) is connected with a hot air outlet of the heat exchanger (17), the nozzle (10) is connected with an oxygen outlet of the heat exchanger (17), and the first air inlet (12) is connected with an air outlet of the heat exchanger (17).
8. The autothermal three-stage biomass low-tar carbon gas co-production regulating and controlling device according to claim 6 or 7, characterized in that tar cracked by the oxidation reforming reactor (8) is further catalytically cracked in a bed layer to realize deep removal of tar; the product distribution in the fixed-bed gasification reactor (13) is achieved by controlling the discharge speed and the return valve air/steam equivalence ratio.
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