CN110160029B - System and method for co-production of biomass charcoal and steam - Google Patents

System and method for co-production of biomass charcoal and steam Download PDF

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Publication number
CN110160029B
CN110160029B CN201910450973.8A CN201910450973A CN110160029B CN 110160029 B CN110160029 B CN 110160029B CN 201910450973 A CN201910450973 A CN 201910450973A CN 110160029 B CN110160029 B CN 110160029B
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gas
combustion
ashes
air
chamber
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CN110160029A (en
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王勤辉
余春江
方梦祥
程乐鸣
骆仲泱
张守军
解桂林
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Zhejiang University ZJU
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Zhejiang University ZJU
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • 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
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
    • F22B31/08—Installation of heat-exchange apparatus or of means in boilers for heating air supplied for combustion
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22G—SUPERHEATING OF STEAM
    • F22G7/00—Steam superheaters characterised by location, arrangement, or disposition
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L15/00—Heating of air supplied for combustion
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Materials Engineering (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)

Abstract

The invention relates to a system and a method for co-production of biomass charcoal and steam, wherein the system comprises: the fluidized bed gasifier, the gas-solid separation mechanism and the gas boiler are connected in sequence; the inner wall of the gas staged combustion ashes boiler is a water-cooled wall, and a combustion chamber and a waste heat recovery chamber which are communicated with each other at the bottom are arranged in the gas staged combustion ashes boiler by separating the water-cooled wall; the combustion ashes chamber and the inlet flue are provided with fuel staged combustion air pipes, the waste heat recovery chamber is internally provided with a heating surface, and the gas boiler is connected with a tail flue for discharging flue gas at the side of the waste heat recovery chamber; the gas boiler is connected with a steam drum for collecting superheated steam generated by the water-cooled wall, the separation water-cooled wall and the superheater; the steam drum supplies saturated steam to the water cooling wall, the separation water cooling wall and the superheater for circulation. The invention can efficiently produce carbon particles and superheated steam by improving the structure of the system.

Description

System and method for co-production of biomass charcoal and steam
Technical Field
The invention relates to the technical field of biomass clean utilization, in particular to a biomass carbon steam co-production system and method.
Background
The biomass resources in China are very rich, the annual output of agriculture and forestry wastes is more than 10 hundred million tons, and the energy structure in the current stage can be optimized by developing the utilization technology of the biomass resources, so that the utilization limitation of fossil energy resources is overcome.
At present, biomass resources are mainly utilized by biomass direct combustion and biomass gasification. The biomass gasification can convert volatile matters rich in biomass into combustible gases such as CH 4、H2, CO and the like through pyrolysis and thermochemical oxidation reaction, and compared with a direct combustion technology, the biomass gasification combustion has the characteristics of high comprehensive efficiency, high benefit, low investment cost and raw material diversity, and is gradually applied and popularized at present.
Although biomass gasification combustion technology provides a path for effective utilization of biomass resources, the existing technology has some problems in practical application.
For example, most of the existing technologies use a burner or an internal combustion engine to utilize the combustible gas generated by biomass gasification, and a certain amount of tar gas and fine ash particles are necessarily generated during biomass gasification, so that the tar is easy to separate out when a temperature gradient exists, and the pipelines and equipment are blocked. Therefore, the combustible gas needs to be subjected to deep purification treatment before entering the combustor or the internal combustion engine, which greatly increases the production and operation costs, and meanwhile, related equipment needs to be cleaned regularly, so that the maintenance cost is increased. In addition, the existing gas combustion process is high in combustion temperature, and the combustion atmosphere is difficult to organize, so that the emission concentration of NO x in the flue gas is high.
In addition, the technology adopting the burner or the internal combustion engine cannot form a large-scale application mode, and cannot meet the market demand.
In addition, the existing biomass gasification combustion process only pays attention to the efficient utilization of combustible gas, and the fixed carbon in biomass is often ignored, and is usually treated together with ash as waste, so that the existing biomass gasification combustion process is imperfect from the viewpoint of comprehensive utilization efficiency of resources.
Disclosure of Invention
The invention aims to overcome the defects of the prior art and provide a biomass charcoal vapor co-production system and method, which can efficiently produce charcoal particles and superheated steam.
The technical scheme provided by the invention is as follows:
A system for co-production of biomass char, comprising: the fluidized bed gasifier, the gas-solid separation mechanism and the gas staged combustion ashes boiler are sequentially connected;
The inner wall of the gas staged combustion ashes boiler is a water-cooled wall, and a separation water-cooled wall is arranged in the gas staged combustion ashes boiler to divide the gas staged combustion ashes boiler into a combustion chamber and a waste heat recovery chamber, wherein the bottom of the combustion chamber is communicated with the waste heat recovery chamber; the combustion chamber and the inlet flue are internally provided with fuel staged combustion air pipes, the waste heat recovery chamber is internally provided with a superheater and an evaporator, and the fuel gas staged combustion ashes boiler is connected with a tail flue for discharging flue gas at the side of the waste heat recovery chamber;
The gas staged combustion ashes boiler is connected with a saturated steam drum used for collecting and separating the water-cooling wall; the steam drum supplies saturated water to the water cooling wall, the separated water cooling wall and the evaporator, and simultaneously, saturated steam is sent to the superheater for circulation.
In the invention, the waste heat recovery chamber is provided with a heating surface, which can be a superheater and an evaporator, but is not limited to the heating surface.
By improving the structure of the system, the invention can effectively produce biochar particles and superheated steam, avoid the problems of deposition and high-temperature corrosion of alkali metal substances contained in biomass in a heating surface, and realize low nitrogen oxide emission of flue gas.
The combustion ashes chamber realizes staged combustion by the fuel staged combustion air pipe which carries out layered air supply along the height of the combustion chamber so as to control the formation of nitrogen oxides in the combustion process. The outlet side of the combustion ember chamber is provided with an SNCR device. The arrangement of SNCR can further reduce nitrogen oxides in the flue gas, so that the final emission concentration of NO x reaches the national ultra-low emission standard.
Preferably, the heating surface comprises an evaporator and a superheater from bottom to top.
A section of cooling chamber for cooling flue gas is reserved between the inlet of the waste heat recovery chamber and the superheater, so that the temperature of the flue gas at the inlet of the superheater is not higher than 800 ℃, and deposition and high-temperature corrosion of alkali metal substances in the heating surface of the superheater are avoided.
In the invention, a gasification air preheater and a burn-out air preheater are sequentially arranged in the tail flue, and both preheaters are formed by two stages of preheaters. The high-temperature air generated by the gasification air preheater is connected with the fluidized bed gasification furnace by adopting an air pipeline, and the hot air generated by the ashes air preheater is connected with the ashes burning chamber and is sent into the ashes burning chamber in a layered manner along the height direction. The structure can effectively utilize the heat of high-temperature flue gas, the high-temperature flue gas exchanges heat with the gasification air preheater and the ashes air preheater, and the normal-temperature air is heated by the two-stage preheater of the gasification air preheater to form high-temperature air with the temperature of about 450 ℃ as gasification wind in the fluidized bed gasification furnace. Because the air with higher temperature is sent into the lower part of the fluidized bed gasification furnace, the gasification reaction of the biomass fuel entering the furnace is facilitated, and the biomass raw material with the moisture content of about 50% can be treated.
In the invention, the tail flue is internally provided with the economizer, and the economizer is connected with the steam drum by adopting a pipeline. The economizer can effectively utilize the heat of high-temperature flue gas to heat warm water into saturated water for the water-cooled wall, the separated water-cooled wall and the evaporator.
The economizer is arranged between two stages of preheaters of the gasification air preheater.
The tail flue is also provided with two stages of preheaters of the burn-out air preheater in sequence, and the two stages of preheaters and the fuel air pipe are connected in sequence by adopting an air pipeline. The structure can effectively utilize the heat of high-temperature flue gas, heat normal-temperature air into high-temperature air, and then the high-temperature air is used as fuel air in the burning-out chamber, and the high-temperature air is sent into the burning-out chamber through the multi-layer fuel air pipes.
The fuel staged combustion air duct comprises a plurality of groups which are arranged at intervals along the flowing direction of high-temperature gasification gas. By adopting the air staged combustion mode, the high-temperature gasification gas is prevented from being burnt in the burn-out chamber to form a high-temperature combustion area and a high-oxygen concentration area, the high-efficiency stable combustion of the low-oxygen concentration of the high-temperature gasification gas and the uniform temperature distribution are realized, and the generation of NO x is greatly reduced. Preferably, the fuel staged combustion air pipes comprise 2-15 groups, more preferably 4-10 groups, and at least one group of air pipes are arranged at the inlet flue of the combustion ashes chamber, so that gasification gas is combusted before entering the combustion chamber, the temperature of the gas entering the combustion chamber is always kept stable, and stable combustion of the gas in the combustion ashes chamber is ensured.
Preferably, the temperature of the outlet side of the combustion chamber is controlled to be about 900 ℃ and an SNCR device is provided. The fuel air pipes comprise a plurality of groups which are arranged at intervals along the flowing direction of the high-temperature gasification gas. The combination of air staged combustion + SNCR techniques can further control NO x production.
The gas-solid separation mechanism comprises two groups of cyclone separators which are connected in series. The series connection means that the air outlet of the first cyclone separator is connected with the air inlet of the second cyclone separator, so that the mixed gas of the high-temperature gasification gas and the carbon particles continuously passes through the gas-solid separation twice.
The invention also provides a method for co-production of biomass charcoal and steam by using the system, which comprises the following steps:
1) The biomass and the gasified wind generate partial gasification reaction in the fluidized bed gasifier to generate high-temperature gasification gas and carbon particles;
2) Separating high-temperature gasification gas and carbon particles in a gas-solid separation mechanism, collecting the carbon particles, and enabling the high-temperature gasification gas to enter a gas staged combustion ashes boiler;
3) The high-temperature gasification gas is subjected to combustion reaction with fuel wind fed in a highly layered manner in an inlet flue and a combustion chamber of the gas-fired boiler to generate smoke, and the formation of nitrogen oxides is controlled by controlling the combustion atmosphere and the temperature distribution of the combustion chamber; the steam drum provides saturated water for a water cooling wall, a separation water cooling wall and an evaporator in the gas boiler, and simultaneously provides saturated steam for the superheater; the heat of the flue gas and the heat generated by the combustion reaction are respectively subjected to heat exchange with the water-cooling wall, the saturated water separating the water-cooling wall and the evaporator and the saturated steam in the superheater to form superheated steam;
4) And (3) enabling the flue gas generated in the step (3) to enter a tail flue after passing through the waste heat recovery chamber.
The gasified wind in the step 1) is obtained by heating normal-temperature air through a gasified air preheater. After heat exchange is carried out between the high-temperature flue gas and the gasification air preheater, the normal-temperature air is heated to form high-temperature air which is used as gasification wind in the fluidized bed gasification furnace, so that the heat of the high-temperature flue gas is effectively utilized.
The fuel wind in the step 3) is obtained by heating normal-temperature air through a burn-out air preheater. After the high-temperature flue gas exchanges heat with the ashes air preheater, the external normal-temperature air is heated into high-temperature air which is used as fuel air in the combustion chamber and is introduced into the combustion chamber through a multi-layer fuel air pipe.
The saturated water provided by the steam drum in the step 3) is formed by heating external warm water through heat exchange between the economizer and high-temperature flue gas. The saturated water is heated by heating surfaces such as a water cooling wall, a separation water cooling wall, an evaporator and the like to form saturated steam, and then the saturated steam returns to the steam drum. Saturated steam from the steam drum enters a high-temperature superheater to form high-temperature superheated steam.
The flue gas generated by the combustion reaction in the step 3) is treated by the SNCR device, so that the emission of nitrogen oxides in the flue gas is further reduced.
The invention is characterized in that a section of cooling chamber for cooling flue gas is reserved between the inlet of the waste heat recovery chamber in the step 3) and the superheater, so that the temperature of the flue gas at the inlet of the superheater is not higher than 800 ℃;
In the step 4), the flue gas enters the tail flue and then exchanges heat with the gasification air preheater, the economizer and the ashes burning air preheater respectively.
Compared with the prior art, the invention has the beneficial effects that:
(1) The invention can efficiently produce carbon particles and superheated steam by improving the structure of the system.
(2) According to the invention, the air entering the gasification furnace is heated to a higher temperature through the high-temperature air preheater, so that on one hand, the combustion share of biomass in the gasification furnace can be reduced, the biomass charcoal yield can be improved, and on the other hand, the processing capacity of high-moisture biomass raw materials can be improved.
(3) According to the invention, the air staged combustion measure is adopted, and the combustion atmosphere of the combustion chamber is controlled, so that the high-temperature gasification gas is efficiently and stably combusted in the combustion chamber and uniformly distributed in temperature, the production of nitrogen oxides in the combustion process is reduced, and meanwhile, the SNCR is adopted at the outlet of the combustion chamber to further reduce a small amount of generated nitrogen oxides into nitrogen, so that the concentration of NOx in the flue gas is controlled at a lower level.
Drawings
Fig. 1 is a schematic structural diagram of a biomass charcoal vapor co-production system in the invention.
Wherein, 1, a fluidized bed gasifier; 2. a primary cyclone separator; 3. a secondary cyclone separator; 4. a gas staged combustion ashes boiler; 5. a combustion ember chamber; 6. a fuel staged combustion air duct; 7. an SNCR device; 8. a waste heat recovery chamber; 9. a water cooling wall; 10. an evaporator; 11. a superheater; 12. a tail flue; 13. a gasification air preheater; 14. an economizer; 15. a burnout air preheater; 16. and (3) a steam drum.
Detailed Description
The invention will now be described in further detail with reference to specific examples and figures.
As shown in fig. 1, the biomass charcoal vapor co-production system comprises: a fluidized bed gasification furnace 1, gas-solid separation mechanisms 2,3, a gas staged combustion ashes boiler 4, a steam drum 16 and a tail flue 12.
The outlet of the fluidized bed gasification furnace 1 is connected with a gas-solid separation mechanism, and the gas-solid separation mechanism comprises two groups of cyclone separators which are connected in series, namely a primary cyclone separator 2 and a secondary cyclone separator 3. The air outlet of the primary cyclone separator 2 is connected with the air inlet of the secondary cyclone separator 3, so that the gas-solid mixture of the high-temperature gasified gas and the carbon particles continuously passes through the gas-solid separation twice. The air outlet of the secondary cyclone separator 3 is connected with the gas staged combustion ashes boiler 4, so that high-temperature gasification gas can be introduced into the combustion ashes chamber 5 of the gas boiler 4.
The inner wall of the gas boiler 4 is a water-cooled wall 9, and a combustion ashes chamber 5 and a waste heat recovery chamber 8 which are communicated with each other at the bottom are arranged in the gas boiler 4 by separating the water-cooled wall.
The fuel staged combustion air pipes 6 are arranged in the combustion ashes chamber 5 and the inlet flue thereof, the fuel staged combustion air pipes comprise a plurality of groups, the fuel staged combustion air pipes are arranged at intervals along the flowing direction of the high-temperature gasification gas, the number of the fuel staged combustion air pipes 6 in the combustion ashes chamber 5 is arranged according to the actual size of the combustion ashes chamber 5, for example, the fuel staged combustion air pipes 6 comprise 4-10 groups. At least 1 group of fuel staged combustion air pipes are arranged in the inlet flue of the combustion ember chamber 5. The SNCR device 7 is provided on the outlet side of the combustion chamber 5, and the generation of NO x can be effectively controlled by using a combination of air staged combustion and SNCR.
A heating surface is arranged in the waste heat recovery chamber 8: comprising a superheater 11 and an evaporator 10, the gas staged combustion ember boiler 4 is connected with a steam drum 16 for collecting saturated water vapor generated by a water cooling wall (comprising a separation water cooling wall) 9 and the evaporator 10, and the steam drum 16 supplies saturated water to the water cooling wall (comprising the separation water cooling wall) 9 and the evaporator 10 to form saturated vapor, and simultaneously, the saturated vapor is sent to the superheater 11 to form superheated vapor. The gas staged combustion ashes boiler 4 is connected with a tail flue 12 for discharging flue gas at the side of the waste heat recovery chamber 8. In addition, a cooling chamber for cooling the flue gas is arranged between the inlet of the waste heat recovery chamber and the superheater, and the temperature of the flue gas at the inlet of the superheater is not higher than 800 ℃.
A gasification air preheater 13, an economizer 14 and a burn-out air preheater 15 are arranged in the tail flue 12 in sequence.
The gasification air preheater 13 is connected with the fluidized bed gasification furnace 1 by adopting an air pipeline, and the normal-temperature air is heated by the two-stage preheater of the gasification air preheater 13 to form high-temperature air which is used as gasification wind in the fluidized bed gasification furnace. The structure can effectively utilize the heat of high-temperature flue gas and improve the capability of the gasifier for treating biomass raw materials with high moisture and low heat value, the high-temperature flue gas exchanges heat with the two-stage preheater of the gasification air preheater 13, and normal-temperature air is heated by the gasification air preheater 13 to form high-temperature air with the temperature of 300-500 ℃ to be used as gasification wind in the fluidized bed gasifier 1.
The economizer 14 is connected with the drum 16 by a pipeline, and external warm water can be introduced into the system through the pipeline, so that the warm water is heated to form saturated water and then introduced into the drum 16, and saturated steam is formed after the drum 16 is heated by the water cooling wall (comprising a separation water cooling wall) 9 and the evaporator 10, and then the saturated steam is returned to the drum 16. The saturated steam from the drum 16 enters the high temperature superheater 11 to form high temperature superheated steam. The ashes air preheater 15 is connected with the fuel staged combustion air pipe 6 by an air pipe, and external normal temperature air can be introduced into the system through the air pipe. The structure can effectively utilize the heat of high-temperature flue gas, and forms high-temperature air with the temperature of 150-200 ℃ after heat exchange with the flue gas, and the high-temperature air is used as fuel air in the combustion chamber 8 and is introduced into the combustion chamber 5 through the fuel staged combustion air pipe 6.
The process flow comprises the following steps:
The outside normal temperature air is heated to 300-500 ℃ by the gasification air preheater 13 and then is used as gasification wind to be sent into the fluidized bed gasification furnace 1.
Biomass is fed into the fluidized bed gasification furnace 1, and the biomass can be selected from straw, wood dust, processing scraps and the like. The gasification wind and biomass fed into the fluidized bed gasification furnace 1 are subjected to partial gasification reaction, the reaction temperature is 650-700 ℃, high-temperature gasification gas and carbon particles are generated by the reaction, and the carbon particles carried by the high-temperature gasification gas are separated to be used as carbon products when passing through the primary cyclone separator 2 and the secondary cyclone separator 3 respectively.
The external normal temperature air is heated to 150-200 ℃ after heat exchange with the ashes air preheater 15 respectively, and is used as fuel air of the fuel gas fractional combustion ashes boiler 4 to be sent into the fuel gas fractional combustion ashes boiler 4 through the multi-stage fuel air pipe 6. The high-temperature gasified gas from the secondary cyclone separator 3 enters a combustion burning chamber 5 of the gas staged combustion burning boiler 4 to be burnt with fuel wind fed by a multi-stage fuel air pipe 6, and the reaction temperature of the combustion burning chamber 5 is 900-950 ℃. The emission concentration of nitrogen oxides of the flue gas generated by the combustion ashes chamber 5 after being treated by the SNCR device 7 reaches the national ultra-low emission standard (less than 50mg/Nm 3), and the temperature of the flue gas at the outlet of the gas staged combustion ashes boiler 4 is 500-600 ℃.
The external warm water is heated by the economizer 14 to form saturated water, the saturated water is sent into the steam drum 16 for steam-water separation, and the separated saturated water is respectively sent into the water cooling wall (comprising a separation water cooling wall) 9 and the evaporator 10 and further heated to form saturated steam which is returned into the steam drum 16 for steam-water separation. The saturated steam is sent to the superheater 11 to form superheated steam with different pressures for direct external use. And the flue gas from the tail flue 12 is conveyed to a flue gas treatment system for deep purification treatment.
Specific examples:
The biomass selects furfural slag, the feeding amount is 24t/h, partial gasification reaction is carried out between the furfural slag and 300 ℃ high-temperature gasification wind from a gasification air preheater 13 in a fluidized bed gasification furnace 1, the reaction temperature is about 650 ℃, and high-temperature gasification gas, carbon particles and a small amount of fine ash particles are produced by the reaction. The carbon particles are separated along with the high-temperature gasification gas by a primary cyclone separator 2 and a secondary cyclone separator 3, and the yield of the carbon particles is 2.52t/h. The produced carbon particles can be used as carbon products for producing active carbon, carbon-based fertilizer and the like.
The high-temperature gasified gas from the secondary cyclone separator 3 enters the combustion chamber 5 of the gas boiler 4 and is combusted with the fuel wind fed by the multi-stage fuel wind pipe 6, and the combustion temperature is about 900 ℃. The concentration of NO x in the flue gas generated by combustion is about 96mg/Nm 3 measured by a flue gas analyzer before the SNCR device 7, and is 38mg/Nm 3 (converted into 6% oxygen content) measured after the SNCR device 7, which is lower than the limit value of the ultralow emission standard concentration 50mg/Nm3 in the NO x country. The superheated steam from the superheater 11 has a pressure of 3.2Mpa and a temperature of 420 c and can be used for power generation or industrial heating.

Claims (3)

1. A system for co-production of biomass char, comprising: the fluidized bed gasifier, the gas-solid separation mechanism and the gas staged combustion ashes boiler are sequentially connected;
the inner wall of the gas staged combustion ashes boiler is a water-cooled wall, a separation water-cooled wall is arranged in the gas staged combustion ashes boiler, and the gas staged combustion ashes boiler is divided into a combustion ashes chamber and a waste heat recovery chamber, the bottoms of which are communicated; a fuel staged combustion air pipe is arranged in the combustion ashes chamber and the inlet flue; a heating surface is arranged in the waste heat recovery chamber, and a tail flue for discharging flue gas is connected to the waste heat recovery chamber side of the gas staged combustion ashes boiler;
the gas staged combustion ashes boiler is connected with a saturated steam drum used for collecting and separating the water-cooling wall; the steam drum supplies saturated water to the water cooling wall, the separation water cooling wall and the evaporator to form saturated steam, and meanwhile, the saturated steam is sent to the superheater to form superheated steam;
An SNCR device is arranged on the outlet side of the combustion ashes chamber;
the heating surface comprises an evaporator and a superheater from bottom to top;
The fuel staged combustion air pipes comprise 4-10 groups, and are arranged at intervals along the flowing direction of the high-temperature gasification gas; at least ensuring that the inlet flue of the combustion ashes chamber is provided with a group of air pipes;
A cooling chamber for cooling the flue gas is arranged between the inlet of the waste heat recovery chamber and the superheater, and the temperature of the flue gas at the inlet of the superheater is not higher than 800 ℃;
The gasification air preheater and the ashes air preheater are sequentially arranged in the tail flue, each of the gasification air preheater and the ashes air preheater is composed of two stages of preheaters, high-temperature air generated by the gasification air preheater is connected with the fluidized bed gasifier through an air pipeline, and hot air generated by the ashes air preheater is connected with the ashes burning chamber and is sent into the ashes burning chamber in a layered manner along the height direction;
the tail flue is internally provided with an economizer, and the economizer is connected with the steam drum by adopting a pipeline;
the economizer is arranged between the gasification air preheater and the ashes air preheater;
The gas-solid separation mechanism comprises two groups of cyclone separators which are connected in series;
the external normal-temperature air is heated to 300-500 ℃ through a gasification air preheater respectively and then is used as gasification wind to be sent into a fluidized bed gasification furnace; the reaction temperature in the fluidized bed gasifier is 650-700 ℃;
After exchanging heat between the external normal-temperature air and the ashes air preheater, heating to 150-200 ℃, and sending the air serving as fuel air of the fuel gas staged combustion ashes boiler 4 into the fuel gas staged combustion ashes boiler through a fuel staged combustion air pipe.
2. A method for co-production of biomass char using the system of claim 1, comprising:
1) The biomass and the gasified wind generate partial gasification reaction in the fluidized bed gasifier to generate high-temperature gasification gas and carbon particles;
2) Separating high-temperature gasification gas and carbon particles in a gas-solid separation mechanism, collecting the carbon particles, and allowing the high-temperature gasification gas to enter a gas boiler;
3) The high-temperature gasification gas is combusted with fuel wind fed along a high-level layer by a fuel-level combustion air pipe in an inlet flue and a combustion ashes combustion chamber of the gas-fired boiler to generate smoke, and the formation of nitrogen oxides is controlled by controlling the combustion atmosphere and the temperature distribution of the combustion chamber; the steam drum provides saturated water for a water cooling wall, a separation water cooling wall and an evaporator in the gas boiler, and simultaneously provides saturated steam for the superheater; the heat of the flue gas and the heat generated by the combustion reaction are respectively subjected to heat exchange with the water-cooling wall, the separated water-cooling wall, the saturated water of the evaporator and the saturated steam in the superheater to form superheated steam;
4) And (3) enabling the flue gas generated in the step (3) to enter a tail flue after passing through the waste heat recovery chamber.
3. The method of claim 2, wherein the flue gas generated by the combustion chamber reaction in step 3) is treated by the SNCR apparatus and then enters the waste heat recovery chamber.
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CN115287099A (en) * 2022-07-03 2022-11-04 中国船舶重工集团公司第七0三研究所 Vehicle-mounted small system with biomass gasification device and steam generator

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