CN111718762B - Fluidized bed coal gasification and biomass low-temperature carbonization coupling system and working method - Google Patents
Fluidized bed coal gasification and biomass low-temperature carbonization coupling system and working method Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 27
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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
- C10J3/46—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
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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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- 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
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Abstract
The invention provides a fluidized bed coal gasification and biomass low-temperature carbonization coupling system and a working method, and belongs to the technical field of coal and biomass co-gasification. The system comprises a circulating fluidized bed gasification furnace, a carbonization furnace, a two-stage cyclone separator, a two-stage cooler, an air preheater, a waste water evaporator, a coal gas cooler, a bag-type dust remover, a stirrer, a cold-pressing forming machine and a corresponding conveying device. The invention uses the heat carried by the gasified synthesis gas of the fluidized bed to provide energy for the biomass carbonization furnace so as to obtain the biomass carbon required by co-gasification, and utilizes the acidic organic waste liquid generated in the low-temperature carbonization process of the biomass to enhance the gasification reactivity of the high-carbon fly ash of the fluidized bed gasification furnace, thereby realizing the high-efficiency circulating gasification of the high-carbon fly ash. The invention overcomes the defects of low carbon conversion rate of the fluidized bed gasification furnace caused by high carbon content in the fly ash and the defect that the biomass carbonization furnace needs additional heating equipment, and has the advantages of gradient utilization of heat, high carbon conversion rate and no pollution discharge.
Description
Technical Field
The invention belongs to the technical field of coal and biomass co-gasification. More particularly, the invention relates to a coupling system for fluidized bed coal gasification and biomass low-temperature carbonization.
Background
In the field of fluidized bed coal gasification, the operation temperature of the gasification furnace is generally controlled at 900-. The low operation temperature leads to high carbon content of materials in the furnace, so that part of the powdered carbon is carried out of the gasification furnace by the coarse gas, wherein the carbon powder with larger particles is separated by the primary cyclone separator and then directly returned to the hearth for circular gasification, and part of the carbon powder with finer particles is separated by the secondary cyclone separator and the subsequent bag-type dust collector and mixed with the coal ash to form high-carbon fly ash. The content of the volatile components of the fine powder carbon in the high-carbon fly ash is almost zero, and the high-carbon fly ash has the defects of poor reaction activity, difficult ignition and stable combustion, difficult burnout and the like, brings great difficulty to the further conversion of the high-carbon fly ash, and simultaneously reduces the carbon conversion rate of a gasification furnace.
In addition, biomass can fix atmospheric CO through photosynthesis during growth2Considered as a renewable resource with zero carbon emission, and therefore in recent years CO reduction by using biomass2Emissions studies are being attempted in various fields. WhereinThe biomass charcoal is added in the coal gasification process, so that the formation of a more developed pore structure on the surface of coal can be promoted, and meanwhile, the catalytic action is generated due to the migration of alkali metal and alkaline earth metal substances in the raw materials to the outer surface. It is understood that the gasification processes of both are effectively combined, and a synergistic effect of both is utilized in the mixed gasification process, whereby a better gasification reactivity is inevitably obtained. On the other hand, the low-temperature carbonization treatment can destroy the fiber structure of the biomass to improve the grindability of the biomass and simultaneously improve the energy density of the biomass, thereby effectively improving the low-quality characteristic of the biomass and being beneficial to the co-gasification utilization of the biomass and coal. However, the biomass carbonization process is an endothermic process in itself, requiring an external heat source to supply heat. The additional fuel required by the equipment increases the running cost, and the biomass generates acidic organic waste liquid in the low-temperature carbonization process, and the treatment and cost problems of the waste liquid limit the large-scale application of the technology.
In the previous research, the applicant finds that the acidic organic waste liquid generated by biomass carbonization can promote the dissolution and dispersion of calcium-based minerals enriched in the high-carbon fly ash, improve the in-situ catalytic activity of the minerals and multiply accelerate the gasification reaction rate of the high-carbon fly ash. Meanwhile, the high-carbon fly ash can adsorb most of organic matters in the biomass carbonization waste liquid, the volatile component content of the high-carbon fly ash is correspondingly increased, and the grading utilization of the biomass volatile components and the cyclic utilization of the carbonization waste liquid with the high-carbon fly ash as a carrier are realized on the technical principle.
In the patent publication "a system and process for preparing synthesis gas by co-gasification of coal and biomass" with publication No. CN103450948A, it comprises an independently operated internal circulating fluidized bed gasifier and an independently operated roasting preconditioner. In the process, the high-carbon fly ash carried by the crude gas is not recycled; meanwhile, a carbonization furnace used for baking the biomass independently supplies heat, the problem of treatment of pyrolysis waste liquid is not considered, and the defects in the aspects of energy utilization and environmental protection exist.
Disclosure of Invention
In order to solve the technical problems, the invention aims to design a coal-biochar co-gasification system integrating fluidized bed coal gasification and biomass low-temperature carbonization, and enhance the reactivity of high-carbon fly ash by using acidic organic waste liquid generated by low-temperature carbonization of biomass to form a fluidized bed coal gasification and biomass low-temperature carbonization coupling system, so that heat carried by fluidized bed coal gasification synthesis gas and waste liquid generated by carbonization are fully utilized, the problem of low carbon conversion rate caused by high carbon particle content in fly ash of a fluidized bed gasification furnace is solved, and efficient comprehensive utilization of coal and biomass is realized.
The technical scheme of the invention is as follows:
a fluidized bed coal gasification and biomass low-temperature carbonization coupling system comprises a circulating fluidized bed gasification furnace, a carbonization furnace, a primary cyclone separator, a secondary cyclone separator, a primary cooler, a secondary cooler, an air preheater, a waste water evaporator, a coal gas cooler, a bag-type dust remover, a stirrer, a cold-pressing forming machine and a corresponding conveying device. An upper output port and a lower input port of the circulating fluidized bed gasification furnace are respectively communicated with a primary cyclone separator, and an output port of the primary cyclone separator is communicated with an input port of an air preheater through a pipeline; a first output port of the air preheater is communicated with a hot carrier gas input port of the carbonization furnace through a pipeline, a second output port of the air preheater is communicated with a heat source input port of the waste water evaporator through a pipeline, and a third output port of the air preheater is communicated with a hot air input port of the circulating fluidized bed gasification furnace through a pipeline; the gas production output port of the carbonization furnace is communicated with a downstream primary cooler, a downstream secondary cooler and a bag-type dust remover in sequence, and the gas production output port of the carbonization furnace is communicated with the feed port of the circulating fluidized bed gasification furnace through a pipeline; the waste water outlet of the secondary cooler is communicated with the waste water inlet of the waste water evaporator through a pipeline; the heat source output port of the waste water evaporator is sequentially communicated with a downstream secondary cyclone separator, a gas cooler and a bag-type dust collector on one hand, and is connected with a water vapor inlet of the circulating fluidized bed gasification furnace on the other hand; the input port of the stirrer is respectively communicated with the output ports of the secondary cyclone separator, the bag-type dust collector and the primary cooler, and the output port of the stirrer is communicated with the input port of the cold-pressing forming machine; and the output port of the cold-pressing forming machine is communicated with the conveying device, and the pressed raw materials are conveyed back to the gasification furnace for recycling.
The invention discloses a method for using a fluidized bed coal gasification and biomass low-temperature carbonization coupling system, which comprises the following steps:
(1) the raw coal and the biomass are screened to obtain coal dust and biomass particles with the particle size of less than 8 mm.
(2) And (2) feeding the coal powder treated in the step (1) and a gasifying agent into a circulating fluidized bed gasification furnace together for gasification reaction to obtain crude coal gas carrying carbon particles. After the crude gas carrying carbon particles is treated by a primary cyclone separator, the carbon particles with larger particle size are separated, and the separated carbon particles directly return to a hearth from a lower input port of the circulating fluidized bed to continuously participate in gasification reaction.
(3) And (3) continuously feeding the raw gas treated by the primary cyclone separator in the step (2) into an air preheater for heat exchange, preheating air or oxygen-enriched air required in the gasification process, and feeding preheated hot air into a circulating fluidized bed gasification furnace for gasification. The crude gas after heat exchange of the air preheater is divided into two parts, and one part of the crude gas is used as hot carrier gas to enter the carbonization furnace to provide heat for normal operation of the carbonization furnace for processing biomass; then, the crude gas mixed with the pyrolysis gas passes through a primary cooler and a secondary cooler which are connected in sequence, so that condensable gas is condensed and removed, and finally, dust removal treatment is carried out on the crude gas in a bag-type dust remover to obtain mixed gas. The other part of the crude gas enters the waste water evaporator as a heat source of the waste water evaporator so as to ensure the supply of the water vapor gasifying agent to the circulating fluidized bed gasification furnace; then, the crude gas flowing out of the waste water evaporator sequentially passes through a secondary cyclone separator and a gas cooler, and finally enters a bag-type dust remover for dust removal treatment to obtain clean gas.
(4) The secondary cyclone separator and the bag-type dust collector further separate high-carbon fly ash with small particle size from the main gas, and convey the high-carbon fly ash into the stirrer. Meanwhile, the raw gas as the hot carrier gas in the step (3) is inevitably mixed with a part of pyrolysis gas generated by biomass pyrolysis after flowing through the carbonization furnace. And condensing the mixed gas consisting of the pyrolysis gas and the crude gas by a primary cooler to obtain acidic organic waste liquid, and enabling the acidic organic waste liquid to enter a stirrer to be used as an activating agent of the high-carbon fly ash. And condensing the mixed gas consisting of the pyrolysis gas and the crude gas by a secondary cooler to obtain wastewater, and allowing the obtained wastewater to enter a wastewater evaporator to be used as a gasifying agent for gasification reaction, so that the wastewater generated by the system can be recycled.
(5) The biochar generated by the carbonization furnace in the step (3) enters a circulating fluidized bed gasification furnace through a conveying device to be co-gasified with the pulverized coal, so that the reactivity of the pulverized coal is improved; or as an activated carbon raw material for subsequent utilization.
(6) And (4) uniformly mixing the high-carbon fly ash obtained by the secondary cyclone separator and the bag-type dust collector in the step (4) with the acidic organic waste liquid condensed by the primary cooler in a stirrer. And then, the mixed material is conveyed to a cold press molding machine to be pressed into particles with the diameter of less than 8mm, and then the particles are returned to the circulating fluidized bed gasification furnace through a conveying device to be circularly gasified.
As a further technical scheme, the mass ratio of the high-carbon fly ash to the acidic organic waste liquid is preferably 3: 1.
As a further technical scheme, in the step (2), the gasification temperature in the circulating fluidized bed gasification furnace is 900-1100 ℃.
As a further means, in the step (3), the carbonization furnace is not particularly limited as long as it is a device capable of converting a biomass raw material into a biomass char. The operating temperature of the carbonization furnace is 300-500 ℃, and the volatile content of the generated biochar is less than 40%.
As a further technical scheme, in the step (4), the water content in the acidic organic waste liquid obtained by condensation of the primary cooler is lower than 60%.
As a further technical solution, in the step (6), calcium-based minerals such as limestone need to be dissolved in the acidic organic waste liquid for fly ash with low calcium content.
Compared with the prior art, the invention has the following beneficial effects:
(1) the invention utilizes the high-temperature raw gas generated by the circulating fluidized bed gasification furnace to provide heat for the air preheater and the waste water evaporator, and simultaneously utilizes the raw gas as hot carrier gas to provide energy for the low-temperature pyrolysis of biomass in the carbonization furnace, thereby realizing the cascade utilization of the energy.
(2) Compared with the traditional coal gasification process only using coal powder as a raw material, the addition of the biomass charcoal can improve the gasification reactivity, further improve the gasification efficiency of the whole system, and simultaneously realize the further reduction of carbon dioxide emission.
(3) The coupling with the coal gasification of the circulating fluidized bed and the use of the raw gas as the hot carrier gas avoid the addition of biomass low-temperature carbonization external heat source in the traditional process, and improve the operability and economic benefit of the low-temperature carbonization process.
(4) The acidic organic waste liquid separated by the primary cooler and the waste water separated by the secondary cooler do not need to be further treated, but are respectively and directly used as an activating agent of high-carbon fly ash and a gasifying agent of gasification reaction to enter the gasification furnace for reaction, so that equipment and cost for treating the acidic organic waste liquid and the waste water are reduced.
(5) In the treatment of the high-carbon fly ash, the method adopts the acidic organic waste liquid separated from the primary cooler to activate, so that the reactivity of carbon particles in the fly ash is enhanced, the high-carbon fly ash can be returned to the circulating fluidized bed gasification furnace for continuous reaction, and the utilization efficiency of coal is improved.
Drawings
FIG. 1 is a flow chart of a coupled system for fluidized bed coal gasification and biomass low temperature carbonization.
In the figure: 1 circulating fluidized bed gasification furnace; 2, a first-stage cyclone separator; 3, an air preheater; 4, carbonizing furnace; 5, a first-stage cooler; 6 a secondary cooler; 7, a waste water evaporator; 8, a secondary cyclone separator; 9 gas cooler; 10 a stirrer; 11 cold press forming machine; 12 bag dust collector.
Fig. 2 is a graph showing the gasification conversion ratio when the acidic organic waste liquid is mixed in the high-carbon fly ash.
Fig. 3 is a graph showing the gasification reaction rate when the acidic organic waste liquid is mixed in the high-carbon fly ash.
Detailed Description
Examples of the present invention will be described below, but the present invention is not limited to these examples.
Example 1
The coal powder with the particle size of less than 8mm and the gasifying agent enter the circulating fluidized bed gasification furnace 1 together for gasification reaction, the generated crude coal gas is treated by the primary cyclone separator 2, the entrained carbon particles with larger particle size are separated, and the separated carbon particles directly return to the hearth from the lower input port of the circulating fluidized bed gasification furnace 1 to continue to participate in the gasification reaction. The raw gas treated by the primary cyclone separator 2 continuously enters an air preheater 3 to preheat air or oxygen-enriched air required in the gasification process. The crude gas after heat exchange of the air preheater 3 is divided into two parts by a three-way pipe, and one part of the crude gas enters the carbonization furnace as hot carrier gas to provide heat for normal operation of the carbonization furnace 4 for processing biomass; then, the raw gas mixed with the pyrolysis gas passes through a primary cooler 5 and a secondary cooler 6 which are connected in sequence, so that the condensable gas is condensed and removed, and finally, the dust is removed in a bag-type dust remover 12 to obtain the mixed gas. The biomass charcoal produced by the carbonization furnace 4 enters the circulating fluidized bed gasification furnace 1 through the conveying device to be co-gasified with the coal powder, or is used as an active carbon raw material to be subsequently utilized. The other part of the crude gas enters a waste water evaporator 7 to be used as a heat source of the waste water evaporator so as to ensure the supply of a water vapor gasifying agent; then, the raw gas flowing out of the waste water evaporator 7 sequentially passes through a secondary cyclone separator 8 and a gas cooler 9, and finally enters a bag-type dust remover 12 for dust removal treatment to obtain clean gas.
The secondary cyclone 8 and bag-type dust collector 12 further separate the high carbon fly ash with smaller particle size entrained in the raw gas from the main stream gas and transport these fine particles into the mixer 10. Meanwhile, the raw gas as the hot carrier gas inevitably mixes with a part of pyrolysis gas generated by pyrolysis of biomass after flowing through the carbonization furnace 4. After the mixed gas is condensed by the primary cooler 5, the obtained acidic organic waste liquid also enters the stirrer 10 to be used as an activating agent of the high-carbon fly ash, and the high-carbon fly ash obtained by the secondary cyclone separator 8 and the bag-type dust collector 12 and the limestone powder additionally added are uniformly mixed in the stirrer 10. And then, the mixed material is conveyed to the cold press molding machine 11 for press molding, and then returns to the circulating fluidized bed gasification furnace 1 through a conveying device for circulating gasification. The mixed gas is condensed by a secondary cooler 6, and the obtained waste water enters a waste water evaporator 7 to be used as a gasifying agent for gasification reaction.
Example 2 reactivity test of high carbon fly ash with acidic organic waste liquid
The high carbon fly ash and the acidic organic waste liquid were mixed and stirred in the proportions (mass ratio) shown in the figure and dried, and the conversion rate and the gasification reaction rate were measured. In addition, the reaction is carried out in a thermogravimetric analyzer, the measuring temperature is 900 ℃, and the gasifying agent is pure CO2. In addition, the fixed carbon content of the high-carbon fly ash is 66.4 percent, the volatile component content is 10.4 percent, and the ash content is 23.2 percent; the acidic organic waste liquid is condensate obtained by low-temperature pyrolysis of pine wood at 320 ℃, and the pH value of the condensate is 2.1.
Fig. 2 and 3 show the results of measurement of the gasification conversion rate and the reaction rate, respectively. From these results, it was found that the gasification reactivity of the high-carbon fly ash was significantly improved by mixing the acidic organic waste liquid, and the gasification reaction rate was increased by more than 2 times only by mixing the acidic organic waste liquid with the high-carbon fly ash and drying the mixture. Next, the relationship between the mixing ratio of the high-carbon fly ash and the acidic organic waste liquid and the reactivity was investigated. As is clear from fig. 2 and 3, the reactivity of the mixture increases as the amount of the acidic organic waste liquid added increases, but the influence of the amount added is not significant. Considering that the yield of the waste liquid is about 30-50% of the biomass carbonization treatment amount and the high carbon fly ash and the acidic organic waste liquid can show a sufficiently significant gasification reactivity promoting effect at a mass ratio of 3:1, a mass ratio of 3:1 is set as a preferable embodiment.
Claims (10)
1. A fluidized bed coal gasification and biomass low-temperature carbonization coupling system is characterized by comprising a circulating fluidized bed gasification furnace, a carbonization furnace, a primary cyclone separator, a secondary cyclone separator, a primary cooler, a secondary cooler, an air preheater, a wastewater evaporator, a coal gas cooler, a bag-type dust remover, a stirrer, a cold-pressing forming machine and a corresponding conveying device; an upper output port and a lower input port of the circulating fluidized bed gasification furnace are respectively communicated with a primary cyclone separator, and an output port of the primary cyclone separator is communicated with an input port of an air preheater through a pipeline; a first output port of the air preheater is communicated with a hot carrier gas input port of the carbonization furnace through a pipeline, a second output port of the air preheater is communicated with a heat source input port of the waste water evaporator through a pipeline, and a third output port of the air preheater is communicated with a hot air input port of the circulating fluidized bed gasification furnace through a pipeline; the gas production output port of the carbonization furnace is communicated with a downstream primary cooler, a downstream secondary cooler and a bag-type dust remover in sequence, and the gas production output port of the carbonization furnace is communicated with the feed port of the circulating fluidized bed gasification furnace through a pipeline; the waste water outlet of the secondary cooler is communicated with the waste water inlet of the waste water evaporator through a pipeline; the heat source output port of the waste water evaporator is sequentially communicated with a downstream secondary cyclone separator, a gas cooler and a bag-type dust collector on one hand, and is connected with a water vapor inlet of the circulating fluidized bed gasification furnace on the other hand; the input port of the stirrer is respectively communicated with the output ports of the secondary cyclone separator, the bag-type dust collector and the primary cooler, and the output port of the stirrer is communicated with the input port of the cold-pressing forming machine; and the output port of the cold-pressing forming machine is communicated with the conveying device, and the pressed raw materials are conveyed back to the gasification furnace for recycling.
2. The working method of the coupling system for coal gasification in the fluidized bed and low-temperature carbonization of biomass according to claim 1 is characterized by comprising the following steps:
(1) screening raw coal and biomass to obtain coal powder with the particle size of less than 8mm and biomass particles with the particle size of less than 8 mm;
(2) the coal powder treated in the step (1) and a gasifying agent enter a circulating fluidized bed gasification furnace together for gasification reaction to obtain crude gas carrying carbon particles; after the crude gas carrying the carbon particles is treated by a primary cyclone separator, separating the carbon particles with larger particle size, and directly returning the separated carbon particles to a hearth from a lower input port of the circulating fluidized bed to continuously participate in gasification reaction;
(3) the raw gas treated by the primary cyclone separator in the step (2) continuously enters an air preheater for heat exchange, air or oxygen-enriched air required in the gasification process is preheated, and preheated hot air enters a circulating fluidized bed gasification furnace to participate in gasification; the crude gas after heat exchange of the air preheater is divided into two parts, and one part of the crude gas is used as hot carrier gas to enter the carbonization furnace to provide heat for normal operation of the carbonization furnace for processing biomass; then, the crude gas mixed with the pyrolysis gas passes through a primary cooler and a secondary cooler which are connected in sequence, so that condensable gas is condensed and removed, and finally, dust removal treatment is carried out on the crude gas in a bag-type dust remover to obtain mixed gas; the other part of the crude gas enters the waste water evaporator as a heat source of the waste water evaporator so as to ensure the supply of the water vapor gasifying agent to the circulating fluidized bed gasification furnace; then, the crude gas flowing out of the waste water evaporator sequentially passes through a secondary cyclone separator and a gas cooler, and finally enters a bag-type dust remover for dust removal treatment to obtain clean gas;
(4) the secondary cyclone separator and the bag-type dust collector further separate high-carbon fly ash with small particle size from the main gas, and convey the high-carbon fly ash into the stirrer; meanwhile, the raw gas serving as the hot carrier gas in the step (3) is inevitably mixed with a part of pyrolysis gas generated by biomass pyrolysis after flowing through the carbonization furnace; condensing the mixed gas composed of the pyrolysis gas and the crude gas by a primary cooler, and allowing the obtained acidic organic waste liquid to enter a stirrer to be used as an activating agent of the high-carbon fly ash; condensing the mixed gas consisting of the pyrolysis gas and the crude gas by a secondary cooler, and allowing the obtained wastewater to enter a wastewater evaporator to be used as a gasifying agent for gasification reaction, so that the wastewater generated by the system can be recycled;
(5) the biochar generated by the carbonization furnace in the step (3) enters a circulating fluidized bed gasification furnace through a conveying device to be co-gasified with the pulverized coal, so that the reactivity of the pulverized coal is improved; or as an active carbon raw material for subsequent utilization;
(6) uniformly mixing the high-carbon fly ash obtained by the secondary cyclone separator and the bag-type dust collector in the step (4) and the acidic organic waste liquid condensed by the primary cooler in a stirrer; and then, the mixed material is conveyed to a cold press molding machine to be pressed into particles with the diameter of less than 8mm, and then the particles are returned to the circulating fluidized bed gasification furnace through a conveying device to be circularly gasified.
3. The working method according to claim 2, characterized in that the mass ratio of the high carbon fly ash to the acidic organic waste liquid is preferably 3: 1.
4. The operating method as claimed in claim 2 or 3, wherein in step (2), the gasification temperature in the circulating fluidized bed gasification furnace is 900-1100 ℃.
5. The operation method according to claim 2 or 3, wherein in the step (3), the carbonization furnace is not particularly limited as long as it is a device capable of converting a biomass raw material into biomass char; the operating temperature of the carbonization furnace is 300-500 ℃, and the volatile content of the generated biochar is less than 40%.
6. The operation method according to claim 4, wherein in the step (3), the carbonization furnace is not particularly limited as long as it is a device capable of converting a biomass raw material into biomass char; the operating temperature of the carbonization furnace is 300-500 ℃, and the volatile content of the generated biochar is less than 40%.
7. The working method as claimed in claim 2, 3 or 6, wherein in step (3), the water content in the acidic organic waste liquid obtained by condensation in the primary cooler in step (4) is less than 60%.
8. The working method as claimed in claim 4, wherein in step (3), the water content in the acidic organic waste liquid obtained by condensation in the primary cooler in step (4) is less than 60%.
9. The working method as claimed in claim 5, wherein in step (3), the water content in the acidic organic waste liquid obtained by condensation in the primary cooler in step (4) is less than 60%.
10. Working method according to claim 2, 3, 6, 8 or 9, characterized in that in step (6) it is necessary to dissolve limestone calcium-based minerals in acidic organic waste liquid for fly ash with low calcium content.
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| CN1230498C (en) * | 2004-01-18 | 2005-12-07 | 江苏大学 | Gasification method and device for biomass and coal mixed fluidized-bed |
| JP5432554B2 (en) * | 2009-03-25 | 2014-03-05 | 一般財団法人電力中央研究所 | Gasification system |
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