CN113416583B - Biomass in-situ nitrogen-control gasification co-production hot carbon device - Google Patents
Biomass in-situ nitrogen-control gasification co-production hot carbon device Download PDFInfo
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- CN113416583B CN113416583B CN202110862419.8A CN202110862419A CN113416583B CN 113416583 B CN113416583 B CN 113416583B CN 202110862419 A CN202110862419 A CN 202110862419A CN 113416583 B CN113416583 B CN 113416583B
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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
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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
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
- C10J2300/0909—Drying
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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
- 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
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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
- 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
Abstract
The invention provides a biomass in-situ nitrogen-control gasification co-production hot carbon device, which is based on a double-bed decoupling gasification combustion design, uses heat generated by a gasification combustion area in a pyrolysis area through a heat exchange plate, realizes the combination of a biomass decoupling gasification combustion technology and in-situ nitrogen control, can realize the synchronous, high-efficiency and clean production of biochar and biomass gas hot products by biomass, can utilize the advantage of easy regulation and control of the process of the technology, regulates and controls the quality and quantity of the products, finally realizes the flexible and high-value utilization of biomass resources, and can also utilize a large amount of volatile matters after biomass pyrolysis to carry out NO in flue gasxReduction is carried out to realize NO in the processxAnd (4) controlling in situ.
Description
Technical Field
The invention relates to the field of biomass conversion, relates to gasification co-production of hot carbon and control of emission of nitric oxides, and particularly relates to a biomass in-situ nitrogen-control gasification co-production hot carbon device.
Background
Resources are an important foundation for the survival and development of human society. Along with the rapid development of world economy, the consumption of fossil resources is continuously increased, and meanwhile, increasingly serious environmental pollution is brought. The clean and efficient utilization of resources is a necessary choice for the future global sustainable development road. The biomass is large in biomass and wide in distribution range, is a carbon neutral renewable resource, and plays an increasingly important role in social production. However, biomass resources have large quality difference, generally have high nitrogen content and high water content, and due to the lack of flexible and efficient clean utilization technology, in the agricultural and forestry processing industries, crop straws and biomass processing leftovers generally discharge a large amount of pollutants in the utilization process, and the overall utilization efficiency is not high due to seasonal factors of the resources and the like; in the light industry, various byproduct biomass residues are basically regarded as useless wastes and even become an environmental pollution source. With the increasing exhaustion and consumption of fossil resources and the increasing emphasis on environmental protection, China gradually increases the development of biomass resources, but needs to firstly define an inherited utilization approach suitable for the biomass resources and simultaneously overcome the problems of low efficiency, high pollution emission and the like in biomass conversion and utilization.
Biomass is synchronously converted into industrial or civil biochar and biomass gas/heat products in an adjustable gasification (combustion) mode, so that the requirement of biomass processing industry on quick cleaning treatment of biomass waste is met, and the resource/energy regeneration of the biomass waste can be flexibly realized in a large scale. For example, CN103725328A discloses a method and an apparatus for dual fast fluidized bed gasification of biomass, wherein a fast fluidized bed gasifier a is used to complete pyrolysis gasification of biomass, and a fast fluidized bed combustion furnace B is used to complete combustion of char and combustible gas, so that the biomass is gasified by using its own components, and only combustion improver pure oxygen is required to be provided additionally. However, because the biomass waste, especially the biomass waste in the light industry, has the characteristics of high water content and high nitrogen content, the traditional gasification (combustion) process has the defects of low temperature, unstable process, low conversion efficiency, large dust emission and NO combustion smokexAnd the emission seriously exceeds the standard and the like. The method mainly comprises the steps of arranging a drying device at the front end to perform dewatering and dehumidifying on the raw materials. But this usually results in a complex process flow, high process energy consumption and low system energy efficiency.
Controlling the emission of high concentration NO from high nitrogen containing feedstock during the thermal conversion of fuelxThe smoke technology mainly comprises air classification technology andfuel staging technology, with air staging technology being most commonly used. The main principle of the air staging technique is to stage the combustion of the fuel by reducing the amount of air fed into the furnace from the main combustion zone to 70-75% of the total combustion air (equivalent to about 80% of the theoretical air), to burn the fuel under oxygen-deficient, fuel-rich conditions, wherein the excess air factor in the first combustion zone is less than 1, thereby reducing the rate and extent of combustion in the combustion zone, not only delaying the combustion process, but also reducing NO in a reducing atmospherexGeneration rate of (3), suppression of NOxAnd finally, secondary air and tertiary air are fed above the main combustion area to be mixed with the flue gas generated by the main combustion area, and the whole combustion process of the fuel is finally finished under the condition that the air coefficient is greater than 1. Fuel staging control of NOxThe principle of emissions is similar to air staging, which utilizes a fuel rich, oxygen lean (oxygen supply constant, fuel overfeed) thermal conversion environment formed by multiple fuel supplies to suppress NOxAnd finally, fully supplying oxygen to complete the fuel burning-out process.
Biomass raw materials usually contain up to 60-80% of volatile components, and a large amount of solid fuel is converted into volatile substances at a relatively low temperature, wherein the volatile substances comprise condensable biomass oil and non-condensable gas, and the non-condensable gas comprises CO and H2And CH4And the like, a combustible gas having reducing power. Under gasification conditions (i.e., partial supply of oxygen but not complete combustion of oxygen demand), the volatilized biomass oil forms a large number of free radicals, which are further cracked into small molecular compounds, and CO and H are simultaneously generated2And CH4And reducing combustible gas. The micromolecule biomass oil gas has obvious NOxThe reduction capability is based on, if the biomass decoupling gasification combustion technology is combined with in-situ nitrogen control, the subsequent denitration process is not needed, and NO in the flue gasxThe concentration can meet the standard of emission.
In summary, aiming at biomass with high water content and high nitrogen content, there is a need to develop a device combining biomass decoupling gasification combustion technology and in-situ nitrogen control, which can realize synchronous, efficient and clean production of biochar and biomass gas heat by biomassThe product can utilize the advantage of easy regulation and control of the process of the technology, regulate and control the quality and quantity of the product, finally realize flexible and high-value utilization of biomass resources, and can also utilize a large amount of volatile matters after biomass pyrolysis to NO in flue gasxReduction is carried out to realize NO in the processxAnd (4) controlling in situ.
Disclosure of Invention
In view of the problems in the prior art, the invention provides a biomass in-situ nitrogen-controlled gasification co-production hot carbon device, which is based on a double-bed decoupling gasification combustion design, uses heat generated by a gasification combustion area in a pyrolysis area through a heat exchange plate, realizes the combination of a biomass decoupling gasification combustion technology and in-situ nitrogen control, can realize the synchronous, efficient and clean production of biochar and biomass gas hot products by biomass, can utilize the advantage of the technology that the process is easy to regulate and control, regulates and controls the quality and quantity of the products, finally realizes the flexible and high-valued utilization of biomass resources, and can also utilize a large amount of volatile matters after biomass pyrolysis to carry out NO in flue gasxReduction is carried out to realize NO in the processxAnd (4) controlling in situ.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention aims to provide a biomass in-situ nitrogen-control gasification co-production hot carbon device, which comprises a coupling furnace, wherein the coupling furnace is divided into a pyrolysis zone and a gasification combustion zone by a heat exchange plate, and the heat exchange plate extends from the top end to the middle lower part of the coupling furnace; a first furnace bottom plate corresponding to the lower part of the pyrolysis zone inclines downwards from outside to inside, a second furnace bottom plate below the gasification combustion zone and close to the pyrolysis zone inclines downwards from outside to inside, a third furnace bottom plate below the gasification combustion zone and far away from the pyrolysis zone inclines upwards from inside to outside, an air distribution plate is arranged on the second furnace bottom plate, and a coke collecting port is arranged on the third furnace bottom plate; a biomass feed port and a heat carrier inlet are formed in the top of the pyrolysis zone; a gasification combustion outlet is formed in the top of the gasification combustion area, a secondary air inlet is formed in the middle of the gasification combustion area, and a tertiary air inlet is formed in the upper part of the gasification combustion area;
the device also comprises a gas-solid separator and a heat exchanger, wherein an inlet of the gas-solid separator is connected with the gasification combustion outlet, a solid outlet of the gas-solid separator is connected with the heat carrier inlet, a gas outlet of the gas-solid separator is connected with a heat source inlet of the heat exchanger, and a heat source outlet of the heat exchanger is connected with a smoke evacuation pipe.
The device is based on a double-bed decoupling gasification combustion design, heat generated by a gasification combustion area is used for a pyrolysis area through a heat exchange plate, integration of double beds in the prior art is achieved, in the actual use process, the pyrolysis area is used for drying and pyrolyzing biomass, semicoke particles generated by pyrolysis enter the bottom of the gasification combustion area through a gap below the heat exchange plate, primary air entering from an air distribution plate converts the semicoke particles into fluidization and gasifies and combusts, large-particle coke generated is discharged through a coke collecting port, gasified gas and smoke generated continue to be gasified under the action of secondary air to achieve an in-situ nitrogen control effect, then redundant biomass tar and pyrolysis gas are thoroughly burnt out under the action of tertiary air, and finally high-temperature smoke is subjected to gas-solid separation, and heat generated by the biomass is collected through a heat exchanger.
Wherein, be used for providing the air distribution plate, secondary air intake and the tertiary air import of wind through the setting, divide into three region with the gasification burning district: the area close to the bottom corresponds to the primary air and the semicoke particles and is used for realizing fluidization and gasification combustion of the semicoke particles; the area near the middle part corresponds to secondary air, generated gasification gas and small-particle coke which is not collected and is mainly used for NO generated by semicoke combustion and volatile matter combustionxCan be converted into N under the strong reduction action of oil gas (including free radical) generated by volatile decomposition2To achieve in-situ process control NO in the devicexThe effect of (1); the area close to the top corresponds to the tertiary air and redundant biomass tar and pyrolysis gas, and is used for realizing full burnout of combustible components under the action of the tertiary air and releasing heat which can be obtained by combustion in the biomass as much as possible; that is, the secondary air inlet and the tertiary air inlet of the device can provide the biomass oil gas and the biomass small-particle cokeThe gasification combustion requires air.
The biomass in-situ nitrogen-controlling gasification co-production thermal carbon device is based on a double-bed decoupling gasification combustion design, the heat generated by a gasification combustion area is used for a pyrolysis area through a heat exchange plate, the biomass decoupling gasification combustion technology is combined with in-situ nitrogen control, biomass can be synchronously, efficiently and cleanly produced into biochar and biomass gas thermal products, the advantages of the technology that the process is easy to regulate and control can be utilized, the quality and quantity of the products can be regulated and controlled, the flexible and high-valued utilization of biomass resources can be finally realized, and a large amount of volatile components generated after biomass pyrolysis can be utilized to carry out NO (nitric oxide) in flue gasxReduction is carried out to realize NO in the processxAnd (4) controlling in situ.
The device can realize the gasification and co-production of hot carbon by biomass fuel in the same device and can be used for treating NO in flue gas in the gasification processxPerforming in-situ control to make the smoke NOxDirectly discharging low concentration; meanwhile, the device can adjust the air supply amount of the primary air in the using process according to the requirements of end users so as to control the yield ratio of heat and carbon, so that the application of the device is highly matched with the requirements of the users.
As the preferable technical scheme, the device further comprises a primary air preheater, the primary air preheater is arranged on the smoke evacuation pipe, and a material outlet of the primary air preheater is connected with the air distribution plate.
Because the flue gas that discharges from the heat source export of heat exchanger still has higher temperature, in order to can realize good fluidization effect with the semicoke granule that the pyrolysis produced simultaneously, preheat for the air through set up the air preheater on the flue gas evacuation pipe.
In a preferred embodiment of the present invention, the inclination angle of the first hearth is 50 to 60 degrees, for example, 50 degrees, 51 degrees, 52 degrees, 53 degrees, 55 degrees, 56 degrees, 58 degrees, or 60 degrees, but is not limited to the above-mentioned values, and other values not shown in the above-mentioned range are also applicable.
It is worth to say that the inclination angle of the first furnace bottom plate is up to 50-60 degrees, the first furnace bottom plate belongs to a large inclination angle design, and semi-coke particles obtained after biomass is dried and pyrolyzed can be fully ensured to smoothly enter a bottom combustion area of a gasification combustion area.
In a preferred embodiment of the present invention, the inclination angle of the second hearth plate is 15 to 25 degrees, for example, 15 degrees, 17 degrees, 18 degrees, 19 degrees, 20 degrees, 21 degrees, 22 degrees, 23 degrees, or 25 degrees, but is not limited to the above-mentioned values, and other values not shown in the above-mentioned range are also applicable.
It is worth to say that the inclination angle of the second furnace bottom plate is reduced to 15-25 degrees, so that the sliding speed of the semicoke particles sliding from the first furnace bottom plate can be effectively reduced, the semicoke particles can be fully ensured to be blown up by the air distribution plate arranged on the second furnace bottom plate and to be in a fluidized state, and gasification combustion of the semicoke particles is facilitated.
It is worth to say that the air distribution plate on the second furnace bottom plate is further provided with an adjustable air cap system for adjusting the position of the air supply port and the air volume.
In a preferred embodiment of the present invention, the inclination angle of the third hearth plate is 25 to 45 degrees, for example, 25 degrees, 28 degrees, 30 degrees, 32 degrees, 35 degrees, 37 degrees, 40 degrees, 43 degrees, or 45 degrees, but is not limited to the above-mentioned values, and other values not shown in the above-mentioned range are also applicable.
It is worth to be noted that the inclination direction of the third furnace bottom plate of the present invention is different from the inclination directions of the first furnace bottom plate and the second furnace bottom plate, so that large granular coke after gasification combustion can fall on the third furnace bottom plate under the dual actions of primary air flow from the air distribution plate and gravity, and then the collection of the coke is realized through the coke collection port, and the third furnace bottom plate realizes the simple screening function of the coke, and only the large granular coke is collected, while the small granular coke is fluidized and gasified and combusted.
It is worth to be noted that the inclination directions and the inclination angles of the first furnace bottom plate, the second furnace bottom plate and the third furnace bottom plate have a synergistic effect, so that the semi-coke particles generated by pyrolysis can be fluidized, gasified and combusted, and the coke is collected.
In a preferred embodiment of the present invention, the volume ratio of the pyrolysis zone to the gasification combustion zone is 1 (2-4), for example, 1:2, 1:2.5, 1:3, 1:3.5, or 1:4, but the present invention is not limited to the above-mentioned values, and other values not shown in the above-mentioned range are also applicable.
It is worth to say that the pyrolysis zone of the present invention is used for drying and pyrolyzing solid biomass, and requires a small space, while the gasification combustion zone of the present invention is used for gasifying and combusting fluidized gas-solid mixture, and requires a large space. Therefore, after a plurality of experimental researches, the volume ratio of the pyrolysis zone to the gasification combustion zone is preferably 1 (2-4).
As a preferable technical scheme of the invention, the top of the gasification combustion zone is a conical top, and the gasification combustion outlet is positioned at the center of the gasification combustion zone.
It is worth to say that the top of the gasification combustion zone is a conical top, so that the high-temperature flue gas finally obtained in the gasification combustion zone can be collected and poured into a gas-solid separator.
As a preferable technical scheme of the invention, the top of the pyrolysis zone is a conical top, the heat carrier inlet is positioned at the center of the pyrolysis zone, and the biomass feed inlet is positioned on the side wall of the pyrolysis zone.
It is worth to say that the top of the pyrolysis zone is a conical top, which is beneficial to connecting a heat carrier inlet at the center of the pyrolysis zone with a solid outlet of a gas-solid separator which is also conical on one hand, and on the other hand, can prevent gas generated after drying and pyrolysis of biomass from flowing upwards to enter the gas-solid separator.
As a preferable technical scheme of the invention, the heat exchanger is a boiler heat exchanger.
It is worth to be noted that, the heat exchanger of the present invention corresponds to a device using heat generated by biomass, and those skilled in the art can reasonably select the heat exchanger according to actual needs, which is similar to the heat exchanger of the boiler heat exchanger of the present invention that can use high-temperature flue gas.
As a preferable technical scheme of the invention, the gas-solid separator is a cyclone separator.
It is worth to say that the cyclone separator has good gas-solid separation effect and small occupied area, and is beneficial to popularization and application of the device.
Compared with the prior art, the invention at least has the following beneficial effects:
(1) the device is based on a double-bed decoupling gasification combustion design, the heat generated by a gasification combustion area is used for a pyrolysis area through a heat exchange plate, the integration of double beds in the prior art is realized, biomass can be in the same coupling furnace, the gasification co-production of hot carbon and the combination of in-situ nitrogen control are realized through the respective control of the pyrolysis area and the gasification combustion area, and the energy utilization rate of the biomass is greatly improved;
(2) the device can control the ratio of heat and carbon output in the co-production process of heat and carbon by regulating the position of the air inlet of the primary air and the air supply quantity according to the user requirements, thereby realizing the fit with the user requirements;
(3) in the process of realizing the co-production of hot carbon by biomass gasification by using the device, a large amount of volatile components generated after biomass pyrolysis are utilized to carry out NO treatment on flue gas through the ingenious layout of the positions and the connection of the pyrolysis zone and the gasification combustion zonexReduction is carried out to realize NO in the processxIn-situ control to low NOxThe emission effect is achieved, the denitration cost is saved, and secondary pollution such as ammonia escape caused by tail denitration processes such as ammonia spraying denitration and the like is avoided;
(4) according to the device, the bottom of the pyrolysis zone is arranged obliquely downwards, namely, the first furnace bottom plate corresponding to the bottom of the pyrolysis zone is inclined downwards from outside to inside, so that semicoke in the pyrolysis zone smoothly falls into the gasification combustion zone, and the air distribution plate of the bottom combustion zone of the gasification combustion zone is arranged obliquely, namely, the second furnace bottom plate below the gasification combustion zone and close to the pyrolysis zone is inclined downwards from outside to inside, so that the air supply direction is inclined, the semicoke is blown to the position above the coke collecting port to perform fluidized combustion, and large granular carbon falls into the coke collecting port; the device only utilizes airflow buoyancy and self gravity for collecting the coke, does not have other power equipment, saves the cost and improves the effective utilization rate of biomass energy;
(5) according to the device, the coupling furnace is divided into the pyrolysis zone and the gasification combustion zone by the heat exchange plate, so that heat in the gasification combustion zone can supply heat to the pyrolysis zone through the heat exchange plate and is used for drying and pyrolyzing biomass;
(6) the device is provided with a gas-solid separator above the pyrolysis zone, so that the micro particle coke carrying heat is taken as heat carrier particles to continuously circulate to the pyrolysis zone to supplement heat for biomass; the flue gas that the gas-solid separator separated carries a large amount of heats, for the boiler heat supply back earlier, preheats for the air again, has both guaranteed the thermal recovery of flue gas, utilizes the air that preheats again to make the temperature field distribution of gasification combustion area bottom more even for gasification combustion process is more stable, has improved the gasification combustion efficiency of living beings.
Drawings
FIG. 1 is a schematic diagram of a device for in-situ nitrogen-controlled gasification and co-production of thermal carbon from biomass according to embodiments 1-3 of the present invention;
in the figure: 1-a coupling furnace; 2-a pyrolysis zone; 3-a gasification combustion zone; 4-a heat exchange plate; 5-third air inlet; 6-secondary air inlet; 7-a coke collection port; 8-air distribution plate; 9-primary air conveying pipe; 10-primary air preheater; 11-a flue gas emptying pipe; 12-a heat exchanger; 13-gas-solid separator; 14-a gasification combustion outlet; 15-inlet of heat carrier; 16-biomass feed inlet.
Detailed Description
The technical scheme of the invention is further explained by the specific implementation mode in combination with the attached drawings.
To better illustrate the invention and to facilitate the understanding of the technical solutions thereof, typical but non-limiting examples of the invention are as follows:
example 1
The embodiment provides a biomass in-situ nitrogen-controlling gasification co-production hot char device, as shown in fig. 1, the device comprises a coupling furnace 1, the coupling furnace 1 is divided into a pyrolysis zone 2 and a gasification combustion zone 3 by a heat exchange plate 4, and the heat exchange plate 4 extends from the top end of the coupling furnace 1 to the middle lower part; a first furnace bottom plate corresponding to the lower part of the pyrolysis zone 2 inclines downwards from outside to inside, a second furnace bottom plate which is arranged below the gasification combustion zone 3 and is close to the pyrolysis zone 2 inclines downwards from outside to inside, a third furnace bottom plate which is arranged below the gasification combustion zone 3 and is far away from the pyrolysis zone 2 inclines upwards from inside to outside, a wind distribution plate 8 is arranged on the second furnace bottom plate, and a coke collection port 7 is arranged on the third furnace bottom plate; a biomass feeding hole and a heat carrier inlet 15 are formed in the top of the pyrolysis zone 2; a gasification combustion outlet 14 is formed in the top of the gasification combustion zone 3, a secondary air inlet 6 is formed in the middle of the gasification combustion zone 3, and a tertiary air inlet 5 is formed in the upper part of the gasification combustion zone 3;
the device also comprises a gas-solid separator 13 and a heat exchanger 12, wherein the inlet of the gas-solid separator 13 is connected with the gasification combustion outlet 14, the solid outlet of the gas-solid separator 13 is connected with the heat carrier inlet 15, the gas outlet of the gas-solid separator 13 is connected with the heat source inlet of the heat exchanger 12, and the heat source outlet of the heat exchanger 12 is connected with the flue gas emptying pipe 11;
the device also comprises a primary air preheater 10, wherein the primary air preheater 10 is arranged on the flue gas emptying pipe 11, and a material outlet of the primary air preheater 10 is connected with the air distribution plate 8;
the inclination angle of the first furnace bottom plate is 50 degrees, the inclination angle of the second furnace bottom plate is 20 degrees, the inclination angle of the third furnace bottom plate is 30 degrees, the volume ratio of the pyrolysis zone 2 to the gasification combustion zone 3 is 1:3, the top of the gasification combustion zone 3 is a conical top, the gasification combustion outlet 14 is positioned in the center of the gasification combustion outlet, the top of the pyrolysis zone 2 is a conical top, the heat carrier inlet 15 is positioned in the center of the pyrolysis zone, the biomass feed inlet is positioned in the side wall of the biomass feed inlet, the heat exchanger 12 is a boiler heat exchanger 12, and the gas-solid separator 13 is a cyclone separator.
Application example 1
The application example provides a method for performing in-situ nitrogen control gasification and co-production of hot carbon by using the device in embodiment 1, and the method comprises the following steps:
the biomass with high water content and high nitrogen content enters the pyrolysis zone 2 of the coupling furnace 1 through a biomass feeding hole 16, and heat from the gasification combustion zone 3 acts on the biomass through a heat exchange plate 4 and dries and pyrolyzes the biomass;
the semicoke particles generated in the pyrolysis zone 2 slide down from the pyrolysis zone 2 into the gasification combustion zone 3 by virtue of the large-inclination design of the first furnace bottom plate, then the sliding speed of the generated semicoke particles on the second furnace bottom plate is effectively reduced under the action of the second furnace bottom plate designed at a small inclination angle, and simultaneously preheated primary air is blown into the air distribution plate 8 on the second furnace bottom plate to blow up the generated semicoke particles to enable the generated semicoke particles to be in a fluidized state, and simultaneously, coke is generated after gasification combustion; the generated large-particle coke falls on a third furnace bottom plate under the dual action of primary air flow and gravity, and then the coke collection process is finished through a coke collection port 7;
volatile matters such as biomass oil gas (including tar and pyrolysis gas) generated in the pyrolysis zone 2 enter the gasification combustion zone 3 from the pyrolysis zone 2 along a gap below the heat exchange plate 4 to provide reducing atmosphere for the volatile matters and flue gas generated after semicoke combustion in the gasification combustion zone, and NO is reduced in situxFurther remarkably reducing NO in the discharged flue gasxConcentration, and the in-situ nitrogen control effect is realized; under the action of primary air the small-particle coke which is not collected is entrained by air flow and heat carrier and lifted, and under the action of secondary air the volatile component and O in the air2NO in flue gas from gasification combustion, volatile matter combustion and semicoke combustionxIs reduced into N under the strong reducing atmosphere formed by the biomass tar and the pyrolysis gas2To achieve in-situ control of NO in the gasification processxTo realize low NO of the flue gasxDischarging to realize the in-situ nitrogen control effect; thoroughly burning out the redundant biomass tar and pyrolysis gas under the action of tertiary air to obtain high-temperature flue gas;
the high-temperature flue gas enters a gas-solid separator 13 through a gasification combustion outlet 14, heat carrier solid particles at about 800 ℃ obtained by gas-solid separation carry heat to be recycled into a pyrolysis zone 2, heat is further supplemented for the pyrolysis process, the high-temperature flue gas at about 900 ℃ obtained by gas-solid separation supplies heat for a boiler heat exchanger 12, and is preheated to about 250 ℃ through primary air by a primary air preheater 10, the temperature of the flue gas is reduced to about 140 ℃ (above the dew point), and the flue gas is discharged through a flue gas emptying pipe 11.
When the demand of a user on carbon production is large, the adjustable air cap system of the air distribution plate 8 can be adjusted to reduce the number of primary air supply ports or reduce the number of the primary air supply ports, so that the primary air supply rate is reduced, gasification combustion is performed under the condition of oxygen deficiency and fuel enrichment, more coke particles are not combusted, less coke particles are blown up, and more coke particles are collected; when the demand of a user for heat production is large, the air supply rates of primary air, secondary air and tertiary air can be properly increased, so that combustible gas and more coke particles are completely combusted and more heat is released, and the device can realize the control of the heat and carbon yield ratio in the heat and carbon co-production process according to the demand of the user so as to meet the demand of a terminal user; in addition, when the content of volatile matters in the biomass is high, more combustible gas and tar are left at the bottom of the gasification combustion area 3, and the secondary air and the tertiary air are arranged to effectively promote the reburning of the volatile matters.
The pyrolysis zone 2 and the gasification combustion zone 3 in the device are mutually independently controlled and mutually connected and communicated, so that the combination of the process of biomass gasification co-production of hot carbon and in-situ nitrogen control is realized, and NO is generated in gasification combustionxTwo sources of production are nitrogen in the volatiles and nitrogen in the char particles from the pyrolysis process.
Example 2
The embodiment provides a biomass in-situ nitrogen-controlling gasification co-production hot char device, as shown in fig. 1, the device comprises a coupling furnace 1, the coupling furnace 1 is divided into a pyrolysis zone 2 and a gasification combustion zone 3 by a heat exchange plate 4, and the heat exchange plate 4 extends from the top end of the coupling furnace 1 to the middle lower part; a first furnace bottom plate corresponding to the lower part of the pyrolysis zone 2 inclines downwards from outside to inside, a second furnace bottom plate which is arranged below the gasification combustion zone 3 and is close to the pyrolysis zone 2 inclines downwards from outside to inside, a third furnace bottom plate which is arranged below the gasification combustion zone 3 and is far away from the pyrolysis zone 2 inclines upwards from inside to outside, a wind distribution plate 8 is arranged on the second furnace bottom plate, and a coke collection port 7 is arranged on the third furnace bottom plate; a biomass feed port and a heat carrier inlet 15 are formed in the top of the pyrolysis zone 2; a gasification combustion outlet 14 is formed in the top of the gasification combustion zone 3, a secondary air inlet 6 is formed in the middle of the gasification combustion zone 3, and a tertiary air inlet 5 is formed in the upper part of the gasification combustion zone 3;
the device also comprises a gas-solid separator 13 and a heat exchanger 12, wherein the inlet of the gas-solid separator 13 is connected with the gasification combustion outlet 14, the solid outlet of the gas-solid separator 13 is connected with the heat carrier inlet 15, the gas outlet of the gas-solid separator 13 is connected with the heat source inlet of the heat exchanger 12, and the heat source outlet of the heat exchanger 12 is connected with the flue gas emptying pipe 11;
the device also comprises a primary air preheater 10, wherein the primary air preheater 10 is arranged on the flue gas emptying pipe 11, and a material outlet of the primary air preheater 10 is connected with the air distribution plate 8;
the inclination angle of the first furnace bottom plate is 55 degrees, the inclination angle of the second furnace bottom plate is 15 degrees, the inclination angle of the third furnace bottom plate is 25 degrees, the volume ratio of the pyrolysis zone 2 to the gasification combustion zone 3 is 1:2, the top of the gasification combustion zone 3 is a conical top, the gasification combustion outlet 14 is positioned in the center of the gasification combustion outlet, the top of the pyrolysis zone 2 is a conical top, the heat carrier inlet 15 is positioned in the center of the pyrolysis zone, the biomass feed inlet is positioned in the side wall of the biomass feed inlet, the heat exchanger 12 is a boiler heat exchanger 12, and the gas-solid separator 13 is a cyclone separator.
Example 3
The embodiment provides a biomass in-situ nitrogen-controlling gasification co-production hot char device, as shown in fig. 1, the device comprises a coupling furnace 1, the coupling furnace 1 is divided into a pyrolysis zone 2 and a gasification combustion zone 3 by a heat exchange plate 4, and the heat exchange plate 4 extends from the top end of the coupling furnace 1 to the middle lower part; a first furnace bottom plate corresponding to the lower part of the pyrolysis zone 2 inclines downwards from outside to inside, a second furnace bottom plate which is arranged below the gasification combustion zone 3 and is close to the pyrolysis zone 2 inclines downwards from outside to inside, a third furnace bottom plate which is arranged below the gasification combustion zone 3 and is far away from the pyrolysis zone 2 inclines upwards from inside to outside, a wind distribution plate 8 is arranged on the second furnace bottom plate, and a coke collection port 7 is arranged on the third furnace bottom plate; a biomass feed port and a heat carrier inlet 15 are formed in the top of the pyrolysis zone 2; a gasification combustion outlet 14 is formed in the top of the gasification combustion zone 3, a secondary air inlet 6 is formed in the middle of the gasification combustion zone 3, and a tertiary air inlet 5 is formed in the upper part of the gasification combustion zone 3;
the device also comprises a gas-solid separator 13 and a heat exchanger 12, wherein the inlet of the gas-solid separator 13 is connected with the gasification combustion outlet 14, the solid outlet of the gas-solid separator 13 is connected with the heat carrier inlet 15, the gas outlet of the gas-solid separator 13 is connected with the heat source inlet of the heat exchanger 12, and the heat source outlet of the heat exchanger 12 is connected with the flue gas emptying pipe 11;
the device also comprises a primary air preheater 10, wherein the primary air preheater 10 is arranged on the flue gas emptying pipe 11, and a material outlet of the primary air preheater 10 is connected with the air distribution plate 8;
the inclination angle of the first furnace bottom plate is 60 degrees, the inclination angle of the second furnace bottom plate is 25 degrees, the inclination angle of the third furnace bottom plate is 45 degrees, the volume ratio of the pyrolysis zone 2 to the gasification combustion zone 3 is 1:4, the top of the gasification combustion zone 3 is a conical top, the gasification combustion outlet 14 is positioned in the center of the gasification combustion outlet, the top of the pyrolysis zone 2 is a conical top, the heat carrier inlet 15 is positioned in the center of the pyrolysis zone, the biomass feed inlet is positioned in the side wall of the biomass feed inlet, the heat exchanger 12 is a boiler heat exchanger 12, and the gas-solid separator 13 is a cyclone separator.
Comparative example 1
This comparative example provides a biomass processing apparatus, except that the first, second and third hearth plates were replaced with a horizontal integrated type hearth plate, and a grid plate was provided in the middle of the integrated type hearth plate and near the pyrolysis zone, and the other conditions were exactly the same as in example 1.
In the process of treating biomass by using the device of the comparative example 1, semicoke particles generated in the pyrolysis zone are gradually accumulated in gaps below the pyrolysis zone and the heat exchange plate, so that the smooth proceeding of gasification and co-production of hot carbon is seriously hindered, and the in-situ nitrogen control effect is not ideal.
Comparative example 2
This comparative example provides a biomass processing apparatus, except that the second furnace floor plate was set to the same inclination angle as the first furnace floor plate, that is, the first furnace floor plate and the second furnace floor plate were integrated into an integral type first furnace floor plate, and the arrangement of the air distribution plate corresponding to the second furnace floor plate was unchanged, the other conditions were exactly the same as those in example 1.
In the process of treating biomass by using the device of comparative example 2, the semicoke particles generated in the pyrolysis zone 2 rapidly slide down by virtue of the integral first furnace bottom plate and then are accumulated between the integral first furnace bottom plate and the third furnace bottom plate, so that the semicoke particles cannot be effectively fluidized by primary air blown out from the air distribution plate, and the gasification and combustion of the subsequent semicoke particles are not facilitated.
Comparative example 3
This comparative example provides a biomass processing apparatus under exactly the same conditions as example 1 except that the tertiary air intake was omitted entirely.
In the process of processing the biomass by using the device in the comparative example 3, the small-particle coke which is not collected is entrained by the airflow and the heat carrier to rise under the action of the primary air, and volatile matters and O in the air are volatilized under the action of the secondary air2NO in flue gas from gasification combustion, volatile matter combustion and semicoke combustionxIs reduced into N under the strong reducing atmosphere formed by the biomass tar and the pyrolysis gas2To achieve in-situ control of NO in the gasification processxTo realize low NO of the flue gasxDischarging to realize the in-situ nitrogen control effect; however, the residual biomass tar and pyrolysis gas are not burnt out due to the absence of the tertiary air, so that the heat energy of the biomass is not sufficiently recovered.
In summary, the invention provides a biomass in-situ nitrogen-controlling gasification co-production thermal carbon device, based on a double-bed decoupling gasification combustion design, the heat generated by a gasification combustion area is used in a pyrolysis area through a heat exchange plate, the biomass decoupling gasification combustion technology is combined with in-situ nitrogen control, and biomass synchronous, efficient and clean production of biochar and biochar can be realizedThe process of the technology can be easily regulated and controlled to regulate and control the quality and quantity of the product, so that the biomass resource can be flexibly and highly utilized, and a large amount of volatile components generated after biomass pyrolysis can be utilized to carry out NO treatment on the flue gasxReduction is carried out to realize NO in the processxAnd (4) controlling in situ.
The applicant states that the present invention is described by the above embodiments to explain the detailed structural features of the present invention, but the present invention is not limited to the above detailed structural features, that is, it is not meant to imply that the present invention must be implemented by relying on the above detailed structural features. It should be understood by those skilled in the art that any modifications of the present invention, equivalent substitutions of selected components of the present invention, additions of auxiliary components, selection of specific modes, etc., are within the scope and disclosure of the present invention.
The preferred embodiments of the present invention have been described in detail, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and the invention is not described in any way for the possible combinations in order to avoid unnecessary repetition.
In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the disclosure of the present invention as long as it does not depart from the spirit of the present invention.
Claims (7)
1. The device for co-production of hot carbon by biomass in-situ nitrogen-controlled gasification is characterized by comprising a coupling furnace, wherein the coupling furnace is divided into a pyrolysis zone and a gasification combustion zone by a heat exchange plate, and the heat exchange plate extends from the top end of the coupling furnace to the middle lower part; a first furnace bottom plate corresponding to the lower part of the pyrolysis zone inclines downwards from outside to inside, a second furnace bottom plate below the gasification combustion zone and close to the pyrolysis zone inclines downwards from outside to inside, a third furnace bottom plate below the gasification combustion zone and far away from the pyrolysis zone inclines upwards from inside to outside, an air distribution plate is arranged on the second furnace bottom plate, and a coke collecting port is arranged on the third furnace bottom plate; a biomass feed port and a heat carrier inlet are formed in the top of the pyrolysis zone; a gasification combustion outlet is formed in the top of the gasification combustion area, a secondary air inlet is formed in the middle of the gasification combustion area, and a tertiary air inlet is formed in the upper part of the gasification combustion area; wherein the inclination angle of the first furnace bottom plate is 50-60 degrees, the inclination angle of the second furnace bottom plate is 15-25 degrees, and the inclination angle of the third furnace bottom plate is 25-45 degrees;
the device also comprises a gas-solid separator and a heat exchanger, wherein an inlet of the gas-solid separator is connected with the gasification combustion outlet, a solid outlet of the gas-solid separator is connected with the heat carrier inlet, a gas outlet of the gas-solid separator is connected with a heat source inlet of the heat exchanger, and a heat source outlet of the heat exchanger is connected with a smoke evacuation pipe.
2. The device of claim 1, further comprising a primary air preheater disposed on the flue gas evacuation pipe, wherein a material outlet of the primary air preheater is connected to the grid plate.
3. The apparatus of claim 1, wherein the volume ratio of the pyrolysis zone to the gasification combustion zone is 1 (2-4).
4. The apparatus of claim 1, wherein the top of the gasification combustion zone is a conical top and the gasification combustion outlet is located at the center thereof.
5. The apparatus of claim 1 wherein the top of the pyrolysis zone is a conical top with the heat carrier inlet at its center and the biomass feed inlet at its side walls.
6. The apparatus of claim 1, wherein the heat exchanger is a boiler heat exchanger.
7. The apparatus of claim 1, wherein the gas-solid separator is a cyclone separator.
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