WO2013097532A1 - 一种微波等离子生物质气流床气化炉及工艺 - Google Patents

一种微波等离子生物质气流床气化炉及工艺 Download PDF

Info

Publication number
WO2013097532A1
WO2013097532A1 PCT/CN2012/083562 CN2012083562W WO2013097532A1 WO 2013097532 A1 WO2013097532 A1 WO 2013097532A1 CN 2012083562 W CN2012083562 W CN 2012083562W WO 2013097532 A1 WO2013097532 A1 WO 2013097532A1
Authority
WO
WIPO (PCT)
Prior art keywords
fuel
gasifier
microwave plasma
biomass
synthesis gas
Prior art date
Application number
PCT/CN2012/083562
Other languages
English (en)
French (fr)
Inventor
陈义龙
张岩丰
夏明贵
张亮
Original Assignee
武汉凯迪工程技术研究总院有限公司
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to JP2014549316A priority Critical patent/JP6207524B2/ja
Priority to PL12863948T priority patent/PL2799522T3/pl
Priority to CA2861691A priority patent/CA2861691A1/en
Priority to BR112014015929A priority patent/BR112014015929A2/pt
Priority to AP2014007828A priority patent/AP2014007828A0/xx
Priority to ES12863948.1T priority patent/ES2653255T3/es
Priority to LTEP12863948.1T priority patent/LT2799522T/lt
Priority to DK12863948.1T priority patent/DK2799522T3/en
Priority to SI201231160T priority patent/SI2799522T1/en
Priority to EP12863948.1A priority patent/EP2799522B1/en
Priority to IN1472MUN2014 priority patent/IN2014MN01472A/en
Priority to RU2014131271/05A priority patent/RU2573016C1/ru
Priority to AU2012362083A priority patent/AU2012362083B2/en
Priority to KR1020147020547A priority patent/KR101695974B1/ko
Application filed by 武汉凯迪工程技术研究总院有限公司 filed Critical 武汉凯迪工程技术研究总院有限公司
Priority to SG11201403659YA priority patent/SG11201403659YA/en
Priority to NO12863948A priority patent/NO2799522T3/no
Priority to MX2014007756A priority patent/MX359878B/es
Publication of WO2013097532A1 publication Critical patent/WO2013097532A1/zh
Priority to US14/314,023 priority patent/US9518235B2/en
Priority to ZA2014/05492A priority patent/ZA201405492B/en
Priority to US15/344,569 priority patent/US9873841B2/en
Priority to HRP20171932TT priority patent/HRP20171932T1/hr
Priority to CY20171101328T priority patent/CY1119830T1/el

Links

Images

Classifications

    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/18—Continuous processes using electricity
    • 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
    • C10J3/466—Entrained flow processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C10J3/506—Fuel charging devices for entrained flow gasifiers
    • 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
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • 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
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • 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
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/123—Heating the gasifier by electromagnetic waves, e.g. microwaves
    • C10J2300/1238—Heating the gasifier by electromagnetic waves, e.g. microwaves by plasma
    • 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
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the invention is mainly directed to the field of gasification process using biomass fuel as raw material, in particular to a microwave plasma flow bed process to achieve a gasification furnace and a gasification process for efficiently utilizing biomass fuel to obtain high quality synthesis gas.
  • Biomass gasification process generally has three processes: fixed bed, fluidized bed and entrained flow bed.
  • the biomass fixed bed process mainly has problems of low gasification temperature, large tar content and low synthesis gas quality; fluidized bed gasification process Although the bed temperature is uniform, feeding and slagging are easy, but because of the need to ensure stable fluidization, the temperature inside the furnace is not too high, resulting in a high tar content. Syngas contains tar, the purification process needs to be costly to deal with, and the tar is not easy to remove.
  • the tar enrichment can block valves, pipes and equipment, and cause corrosion, which is extremely harmful.
  • the gasification reaction temperature is high, the furnace temperature is uniform, the gasification efficiency is high, the tar can be completely cracked in the furnace, the subsequent process is simple, and the entrained flow bed has good amplification, which is suitable for industrial scale utilization, but the current
  • the entrained flow process requires higher particle size of the raw material feedstock, and generally requires less than 0.1mm
  • the coal gasification process is even lower, and the biomass containing more biomass such as cellulose cannot be broken to the smaller particle size required for the entrained flow bed, and the smaller the crushed particle size, the more the crusher wears.
  • the object of the present invention is to propose an efficient microwave plasma biomass entrained flow gasifier and a process for solving a series of problems in the above-mentioned biomass production syngas, and preparing syngas for biomass fuel, especially CO and H 2 synthesis gas provides an economical, efficient, and viable industrial equipment and utilization process.
  • Microwave plasma biomass entrained flow gasifier comprising a vertically arranged furnace body, a fuel inlet formed by a burner disposed at a lower portion of the furnace body, a synthesis gas outlet at the top of the furnace body, a slag discharge port at the bottom of the furnace body, and a furnace body outside the furnace body
  • a fuel pretreatment system is further provided, including a fuel crushing device, a screening device located downstream of the fuel crushing device, a particle size qualified fuel bin and a particle size unqualified fuel tank arranged side by side downstream of the screening device, and a downstream setting of the particle size qualified fuel tank
  • the front of the furnace, the bottom of the furnace front is connected to the furnace through the burner; the synthesis gas outlet is arranged at the top of the gasification furnace; the burner is arranged along the radial direction of the furnace, the number is 2 ⁇ 4;
  • the first and second layers of microwave plasma generators are arranged above and below the gasification reaction zone of the furnace body, and each layer of the microwave plasma generator is arranged with 2 to
  • the microwave plasma generator uses a horizontal/tangential arrangement to increase the travel and residence time of the carbonaceous biomass molten particles in the plasma atmosphere.
  • the microwave plasma generator uses a plasma generator with a large electrode spacing, a strong plasma activity, and a wide volume range.
  • the microwave plasma generator microwave power source has a frequency of 2.45 GHz and a single power of less than 200 kW.
  • the process for gasification of biomass gas flow bed by using the above gasification furnace mainly comprises the following steps:
  • Biomass fuel is firstly crushed and sieved by a fuel pretreatment system to obtain biomass fuel particles with acceptable particle size, and sent to the furnace for storage;
  • the microwave plasma working gas enters the plasma generator from the inlet, is excited into a high temperature, high ionization, high activity plasma and is injected into the gasifier;
  • Biomass fuel particles are sprayed into the gasifier through the burner, and the oxidant is sent from the oxygen/steam inlet to the system, and simultaneously injected into the gasifier with the biomass fuel, and the biomass fuel particles are high in the furnace.
  • step 1) the fuel that meets the set particle size is separated into the qualified fuel bin according to the set particle size, and if the particle size is too large, the fuel enters the unqualified fuel tank, and the fuel in the unqualified fuel tank is to be Return to the fuel crushing device and continue to crush to a smaller particle size until qualified; after the crushing and sieving, the biomass fuel particles satisfying the set particle size are transported from the qualified fuel tank to the front of the gasifier furnace for standby;
  • the particle size of the material fuel particles is 0 to 5 mm.
  • step 2) the microwave plasma generator is turned on 2 to 3 seconds before the gasifier burner is put into operation, and the microwave plasma working gas in the form of some oxidants enters the microwave plasma generator through the microwave plasma working gas inlet, and is then excited to a high temperature.
  • a highly ionized, highly reactive plasma gas is injected into the gasifier.
  • step 3 the biomass fuel particles are injected into the gasification furnace from the gasifier nozzle through the carrier gas; the oxidant enters the system through the oxygen/steam inlet, and is simultaneously injected into the gasifier with the biomass fuel, due to the use of high temperature gas.
  • the fuel is instantaneously ignited in the furnace for intense partial oxidation-reduction reaction, biomass fuel in the high temperature and anoxic environment, the formation of a large amount of CO, H 2 and a small part of CO 2 , CH 4 , H 2 S, COS components Syngas
  • Syngas is pumped up to the plasma reaction zone, ie, the gasification reaction zone, mixed with high-temperature, high-ionization, high-activity plasma gas injected horizontally/tangentially, and subjected to high-efficiency gas phase reaction, high temperature thermochemical gasification reaction zone temperature
  • the temperature is 1200 ° C ⁇ 1800 ° C
  • the central zone temperature is 1800 ° C ⁇ 2000 ° C
  • the residence time of the synthesis gas in the gasification reaction zone is set to 1 ⁇ 10 seconds, while controlling the microwave plasma power, to promote the reaction fully.
  • step 4 the volume of the active components CO and H 2 in the synthesis gas product is as high as 85% or more, and there is no tar or phenolic substance in the synthesis gas; the biomass liquid slag is discharged from the bottom of the gasifier by the slag discharge port, It can achieve pollution-free treatment after cold, and it is also a good insulation building material.
  • the microwave plasma working gas and carrier gas are air and/or oxygen and/or steam; the steam is derived from the recovery of sensible heat from its own high temperature synthesis gas.
  • a microwave plasma generator is arranged in the gasification reaction zone of the process, and the microwave plasma generator is a device for generating a stable open plasma by exciting the working gas by microwave, and the excited oxidant-rich microwave plasma has high temperature and high ionization degree. It has the characteristics of large dispersion and strong activity.
  • the temperature of the reaction zone can be increased and the chemical reaction can be promoted;
  • the chemical reaction between the gas phase synthesis gas and the solid phase/liquid phase biomass particles can be greatly improved, the rate of heat and mass transfer is accelerated, and the fuel chemical reaction time is shortened. Based on the residence time, the fuel conversion rate is improved.
  • the biomass fuel since the biomass fuel has the characteristics of large pores, high activity and low melting point with respect to coal, the biomass fuel particle size in the plasma reaction atmosphere with high temperature and high ionization. It can be used with significantly higher fuel particle sizes than conventional gas flow beds, and ultimately achieves the desired results.
  • the microwave plasma generator can not only provide a part of the oxidant for the reaction, but also improve the balance and uniformity of the reactant supply. Moreover, the microwave plasma also inputs a certain amount of heat power, which provides a part of the external heat source and increases the operation of the gasifier. a means of adjustment.
  • silane-free and phenol-free materials in the synthesis gas are processed by microwave plasma high-temperature entrained flow process, and the subsequent utilization process is simple.
  • Feeding and slagging are easy, gasification intensity is large, and large-scale is easy.
  • FIG. 1 is a schematic diagram of a microwave plasma biomass entrained flow gasifier and a process flow thereof according to a preferred embodiment of the present invention
  • Figure 2 is a view taken along line A-A of Figure 1.
  • fuel crushing device 1 screening device 2; particle size qualified fuel bin 3; particle size unqualified fuel bin 4; furnace front bin 5; burner 6; microwave plasma generator 7; gasifier 8, syngas outlet 9; slag discharge port 10; microwave plasma working gas inlet 11; monitoring unit 12; oxygen/steam inlet 13.
  • the microwave plasma biomass entrained flow gasifier 8 shown in Figures 1 and 2 comprises a vertically arranged cylindrical furnace body, a fuel inlet formed by a burner 6 disposed at a lower portion of the furnace body, and a syngas at the top of the furnace body.
  • the outlet 9 and the slag discharge port 10 at the bottom of the furnace body are provided with a fuel pretreatment system, including a fuel crushing device 1, a screening device 2 located downstream of the fuel crushing device 1, and a particle size qualified in parallel downstream of the screening device 2.
  • the gasifier furnace body may be cylindrical or a combination of a cone and a cylinder.
  • the microwave plasma generator 7 adopts two horizontal/tangential arrangements, so that the reaction airflow is sufficiently turbulent to increase the carbonaceous biomass.
  • the synthesis gas monitoring unit 12 is arranged at the synthesis gas outlet 9 of the gasifier, which can realize the online monitoring of the temperature and composition of the syngas to adjust the oxygen flow rate, the steam flow rate and the microwave power in real time, and maintain the gasification process parameters within the control range.
  • the gasifier burner 6 can be arranged in a radial manner along the furnace body, and the number of the burners can be 2 to 4. In actual operation, the number of burners can be selected according to the load condition.
  • the microwave plasma generator uses a plasma generator with a large electrode spacing, a strong plasma activity, and a wide volume range.
  • the microwave plasma generator microwave power source has a frequency of 2.45 GHz and a single power of less than 200 kW.
  • the process for gasification of biomass gas flow bed by using the above gasification furnace 8 mainly includes the following steps:
  • the biomass fuel first passes through the fuel crushing device 1 of the fuel pretreatment system, and is crushed to an appropriate size.
  • the crushed particle size is the key to the economics of the process. If the crushed particle size is too large, the gasification process is inefficient, and the carbon conversion is low. The rate is low; if the crushing particle size is too small, the crusher is seriously worn, the power consumption is high, and the economy is poor.
  • the fuel enters the fuel screening device 2, and the fuel that meets the set particle size is separated into the qualified fuel tank 3 according to the set particle size.
  • the fuel in the qualified fuel tank 4 will be returned to the fuel crushing unit 1 and continue to be crushed to a smaller particle size until it is qualified.
  • the original size of the rice husk is about 7-10 mm long and 2 mm wide.
  • the shape is like a boat shape, and it can be used simply by crushing the fuel to a particle size of 1 to 5 mm.
  • the diameter of the branches and straws is large, and the disc type or drum crusher can be selected to be about 50 to 100 mm, and then the hammer mill is used to crush the mixture to 1 according to the feeding pretreatment scheme as described above. ⁇ 5mm particle size fuel can be used.
  • the microwave plasma working gas enters the plasma generator 7 from the inlet 11 and is excited into a high temperature, high ionization, high activity plasma and injected into the gasifier 8;
  • the microwave plasma generator 7 is turned on 2 to 3 seconds before the gasifier burner 6 is put into operation, and the microwave plasma working gas in the form of a part of the oxidant enters the microwave plasma generator 7 through the microwave plasma working gas inlet 11 and is then excited to a high temperature and a high temperature.
  • the ionization, high activity plasma gas is injected into the gasification furnace 8.
  • the carrier gas sprays the biomass fuel into the gasification furnace 8 through the burner 6, while the oxidant is sent from the oxygen/steam inlet 13 through the nozzle 6 to the system, and simultaneously injected into the gasifier with the biomass fuel.
  • the biomass fuel particles undergo high-temperature rapid thermochemical reaction in a highly active plasma atmosphere in the furnace to produce a synthesis gas containing a large amount of CO, H 2 and a small portion of CO 2 , CH 4 , H 2 S, and COS components.
  • the biomass fuel particles satisfying the set particle size after being crushed and sieved are transported from the qualified fuel tank 3 to the front chamber 5 of the gasifier furnace, and are pneumatically conveyed to the gasifier nozzle 6 by the gasifying agent at the lower portion of the furnace front 5
  • the fuel is injected into the gasifier;
  • the oxidant enters the system through the oxygen/steam inlet 13 and is injected into the gasifier simultaneously with the biomass fuel.
  • the fuel instantaneously ignites in the furnace. Partial redox reaction, biomass fuel in the high temperature anoxic environment, the formation of a large amount of CO, H 2 and a small part of the CO 2 , CH 4 , H 2 S, COS components of the synthesis gas;
  • Syngas is pumped up to the plasma reaction zone, ie, the gasification reaction zone, mixed with high-temperature, high-ionization, high-activity plasma gas injected horizontally/tangentially, and subjected to high-efficiency gas phase reaction, high temperature thermochemical gasification reaction zone temperature 1200 ° C ⁇ 1800 ° C, the central zone temperature can be as high as 1800 ° C ⁇ 2000 ° C, the process design to ensure the residence time of the gasification reaction zone 1 ⁇ 10 seconds, while controlling the microwave plasma power, to promote the reaction fully, the final synthesis gas by The synthesis gas outlet 9 at the top of the gasifier is taken out, and the content of the active components CO and H 2 in the synthesis gas product is as high as 85% or more, and there is no tar or phenolic substance in the synthesis gas.
  • the biomass liquid slag is discharged from the slag discharge port 9 of the gasifier, and can be treated with pollution-free treatment after chilling, and is also a good insulating building material.
  • the steam used in the process is derived from the recovery of high temperature syngas.
  • the synthesis gas temperature and composition are monitored to adjust the oxygen flow rate, steam flow rate and microwave power in real time to maintain the gasification process parameters within the control range;
  • the synthesis gas outlet temperature is 900 ° C ⁇ 1200 ° C;
  • the high temperature synthesis gas from the top synthesis gas outlet 9 It is taken out while the liquid slag is discharged from the bottom slag discharge port 10.
  • the biomass fuel powder particles have a particle diameter of 0 to 5 mm, and a preferred example is about 2 mm.
  • the microwave plasma working gas and carrier gas are air and/or oxygen and/or steam; the steam is derived from the recovery of sensible heat from its own high temperature synthesis gas.
  • the key in the design is to control the bed temperature and adjust the microwave plasma power and the supply of oxygen and steam.
  • the control of the above-mentioned key factors can be achieved by the syngas outlet monitoring device, and the interlock control can be realized, and the fully automated operation can be performed to improve the operational stability.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)

Abstract

一种微波等离子生物质气流床气化炉，包括炉体（8）、设置在炉体（8）下部的燃料进口、炉体顶部的合成气出口（9）、炉体（8）底部的排渣口（10），炉体（8）外还设置燃料预处理系统，包括燃料破碎装置（1）、位于燃料破碎装置（1）下游的筛分装置（2）、筛分装置（2）下游并列设置的粒径合格燃料仓（3）和粒径不合格燃料仓（4）、以及粒径合格燃料仓（3）下游设置的炉前仓（5），炉前仓（5）的底部通过烧嘴与炉体（8）相连；气化炉顶部合成气出口（9）布置有合成气监测单元（12）。还提供一种利用上述气化炉进行生物质气流床气化的工艺，所述工艺包括：1）生物质燃料预处理；2）微波等离子工作气体从入口进入等离子发生器中，激励成等离子体而喷入气化炉中；3）生物质燃料粉粒通过烧嘴喷入气化炉中，同时将氧化剂从氧气/蒸汽入口送入系统，与生物质燃料同时喷入气化炉内，生物质燃料在炉内进行热化学反应；4）对合成气温度、成份进行监测来实时调整氧气流量、蒸汽流量及微波功率；合成气出口温度900°C〜1200°C；最终合成气从顶部合成气出口引出，同时液态渣由排渣口排出。

Description

一种微波等离子生物质气流床气化炉及工艺 技术领域
本发明主要针对采用生物质燃料为原料的气化工艺领域，具体来说是一种微波等离子气流床工艺来达到高效利用生物质燃料制取高品质合成气的气化炉及气化工艺过程。
背景技术
目前，在生物质能源利用工艺中，生物质气化技术因对生物质种类的适应性更宽，且产品扩展性更强，因而发展潜力巨大。生物质气化工艺大致存在固定床、流化床、气流床这三种工艺，生物质固定床工艺主要存在气化温度低，焦油含量大，合成气品质低等问题；流化床气化工艺中虽床温均匀，给料及排渣容易，但是由于需要确保稳定流化，炉内温度不易过高，导致焦油含量较高。合成气中含有焦油，则净化工艺需要花费较大代价来处理，且焦油不易去除，焦油富集能堵塞阀门、管道及设备，并对其产生腐蚀，因而危害性极大。而气流床中气化反应温度高，炉温均匀，气化效率高，焦油在炉内能完全裂解，后续工艺处理简单，且气流床具有较好的放大性，适合工业化规模利用，但是现行的气流床工艺对原料给料粒径要求较高，一般均要求小于 0.1mm ，特别是燃煤气化工艺甚至要求更低，而生物质这类纤维素含量较多的原料无法破碎到气流床所需要的较小粒径，且破碎粒径越小，破碎机磨损越厉害，电耗也越高；而较大粒径则会导致气流床工艺中碳转化率降低，冷煤气效率降低，这样限制了常规气流床工艺在生物质燃料方面的利用与发展。
 技术问题
本发明的目的是提出一种高效的微波等离子生物质气流床气化炉及工艺，解决上述生物质制取合成气中存在的一系列问题，为生物质燃料制取合成气，特别是CO和H 2 的合成气提供一种经济、高效、可行的工业化设备及利用工艺。
技术解决方案
本发明为解决上述技术问题，采取的技术方案如下：
微波等离子生物质气流床气化炉，包括竖直设置的炉体、由烧嘴构成的设置在炉体下部的燃料进口、炉体顶部的合成气出口、炉体底部的排渣口，炉体外还设置燃料预处理系统，包括燃料破碎装置、位于燃料破碎装置下游的筛分装置、筛分装置下游并列设置的粒径合格燃料仓和粒径不合格燃料仓、以及粒径合格燃料仓下游设置的炉前仓，炉前仓的底部通过烧嘴与炉体相连；气化炉顶部合成气出口布置有合成气监测单元；烧嘴沿炉体径向布置，数量为2～4个；其特征在于，在炉体的气化反应区上下布置1～2层微波等离子发生器，每层微波等离子发生器布置2～4个工作气体接入口。
微波等离子发生器采用水平/切向布置方式，以增加含碳生物质熔融颗粒在等离子体氛围内的行程及停留时间。
微波等离子发生器采用电极间距大、等离子体活性强、体积范围广的等离子发生器。
微波等离子发生器微波功率源主频2.45GHz,单台功率约200kW以内。
采用上述气化炉进行生物质气流床气化的工艺主要包括如下步骤：
1 ）生物质燃料先经过燃料预处理系统破碎、筛分后得到粒径合格的生物质燃料粉粒，并送入炉前仓备用；
2 ）微波等离子工作气体从入口进入等离子发生器中，激励成高温、高电离度、高活性的等离子体而喷入气化炉中；
3 ）生物质燃料粉粒通过烧嘴喷入气化炉中，同时将氧化剂从氧气/蒸汽入口送入系统，与生物质燃料同时喷入气化炉内，生物质燃料粉粒在炉内高活性的等离子体氛围中进行高温快速热化学反应，生成含大量CO、H 2 的合成气；
4 ）对合成气温度、成份进行监测来实时调整氧气流量、蒸汽流量及微波功率，维持气化工艺参数在控制范围内；合成气出口温度900℃～1200℃；最终高温合成气从顶部合成气出口引出，同时液态渣由排渣口排出。
步骤1）中，按设定粒径分离出满足设定粒径尺寸的燃料进入合格燃料仓，粒径过大燃料则进入粒径不合格燃料仓，而粒径不合格燃料仓中燃料将被返回送入燃料破碎装置中继续破碎至较小粒径，直至合格；经破碎、筛分后满足设定粒径尺寸的生物质燃料颗粒由合格燃料仓输送至气化炉炉前仓备用；生物质燃料粉粒的粒径为0～5mm。
步骤2）中，气化炉烧嘴投运前2～3秒即开启微波等离子发生器，部分氧化剂形式的微波等离子工作气体通过微波等离子工作气体入口进入微波等离子发生器，随后被激励成高温、高电离度、高活性的等离子气体喷入气化炉。
步骤3）中，生物质燃料粉粒通过载气由气化炉喷嘴喷入气化炉内；氧化剂通过氧气/蒸汽入口进入系统，与生物质燃料同时喷入气化炉内，由于采用高温气化工艺，燃料瞬间着火在炉内进行剧烈的部分氧化还原反应，生物质燃料在高温缺氧环境下，生成含大量CO、H 2 和少部分CO 2 、CH 4 、H 2 S 、COS成分的合成气；
合成气上行至等离子体反应区也即气化反应区，与水平/切向喷入的高温、高电离度、高活性的等离子气体混合，并进行高效气相反应，高温热化学气化反应区温度为1200℃～1800℃，中心区温度为1800℃～2000℃，合成气在气化反应区的停留时间设定为1～10秒，同时控制微波等离子功率，促进反应充分进行。
步骤4）中，合成气产物中有效成分CO和H 2 体积含量高达85%以上，且合成气中无焦油、酚类物质；生物质液态渣由气化炉底部排渣口排出炉外，激冷后能够实现无公害处理，同时也是良好的保温建筑材料。
步骤2）和3）中，微波等离子工作气体和载气为空气和/或氧气和/或蒸汽；蒸汽来源于对自身高温合成气显热的回收。
在本工艺气化反应区布置有微波等离子发生器，微波等离子发生器是通过微波激发工作气体产生稳定开放的等离子体的设备，激发的富含氧化剂的微波等离子体具有温度高、电离度高、分散度大，活性强的特点，当在气流床氧化还原区中喷入适量微波等离子体工作气体时，在高温高活性的等离子体的作用下，一方面能提高反应区温度，促进化学反应；另一方面由于等离子活性高、反应强，能极大提高气相合成气与固相/液相生物质颗粒间的化学反应，加快了传热传质的速率，使得燃料化学反应时间缩短，在相同停留时间基础上，提高了燃料转化率，同时由于生物质燃料相对煤而言具有孔隙大、活性高、熔点低的特点，因而在高温高电离度的等离子体反应气氛中，生物质燃料粒径能采用明显高于常规气流床所需燃料粒径，且最终能达到理想效果。
再次，微波等离子发生器不仅能为反应提供一部分氧化剂，提高反应物供给的平衡性与均匀性，而且微波等离子也同时输入了一定量的热功率，提供了一部分外热源，增加了气化炉运行的一种调节手段。
 有益效果
本工艺的有益效果是：
1. 采用微波等离子气流床高温工艺，结合生物质燃料自身具有的高活性的特点，在炉内实现生物质燃料化学能高效转化，碳转化率高达约99%，冷煤气效率85%以上，CO和H 2 有效成分含量高。
2. 采用微波等离子高温气流床工艺合成气中无焦油、无酚类物质，后续利用工艺简单。
3. 对生物质燃料粒径适应范围广，无需过分破碎，经济性好；且通过微波等离子气流床能实现将生物质颗粒在气流床中气化，解决了常规气流床气化工艺中需采用粒径小的生物质燃料带来的难度大、经济性差的难题。
4. 给料、排渣容易，气化强度大，大型化容易。
 附图说明
下面结合附图和实施例来说明本发明。
图1为本发明优选实施例的微波等离子生物质气流床气化炉及工艺流程示意图；
图2为图1的A-A视图。
其中：燃料破碎装置1；筛分装置2；粒径合格燃料仓3；粒径不合格燃料仓4；炉前仓5；烧嘴6；微波等离子发生器7；气化炉8，合成气出口9；排渣口10；微波等离子工作气体入口11；监测单元12；氧气/蒸汽入口13。
 本发明的最佳实施方式
如图1和2所示的微波等离子生物质气流床气化炉8，包括竖直设置的圆柱状炉体、由烧嘴6构成的设置在炉体下部的燃料进口、炉体顶部的合成气出口9、炉体底部的排渣口10，炉体外还设置燃料预处理系统，包括燃料破碎装置1、位于燃料破碎装置1下游的筛分装置2、筛分装置2下游并列设置的粒径合格燃料仓3和粒径不合格燃料仓4、以及粒径合格燃料仓3下游设置的炉前仓5，炉前仓5的底部通烧嘴6与炉体相连；其特征在于，在炉体的气化反应区上下布置1～2层微波等离子发生器7，以增大等离子反应区范围，每层微波等离子发生器布置2～4个工作气体接入口11（如图2所示为3个）。气化炉炉体可以是圆柱状，也可以是圆锥和圆柱的组合形式。
微波等离子布置点的位置及布置方式也对工艺存在较大影响，本发明中，微波等离子发生器7采用水平/切向两种布置方式，这样使得反应气流扰流充分，以增加含碳生物质熔融颗粒在等离子体氛围内的行程及停留时间。
气化炉顶部合成气出口9布置有合成气监测单元12，可实现在线对合成气温度、成份的监测来实时调整氧气流量、蒸汽流量及微波功率，维持气化工艺参数在控制范围内。
气化炉烧嘴6可采用常规沿炉体径向布置方式，布置数量可为2～4个，实际运行中可依据负荷情况，选择运行烧嘴数目。
微波等离子发生器采用电极间距大、等离子体活性强、体积范围广的等离子发生器。
微波等离子发生器微波功率源主频2.45GHz,单台功率约200kW以内。
采用上述气化炉8进行生物质气流床气化的工艺主要包括如下步骤：
1 ）生物质燃料经过燃料破碎装置1、筛分装置2后得到粒径合格的生物质燃料粉粒；
首先，生物质燃料先经过燃料预处理系统的燃料破碎装置1，被破碎至合适尺寸，破碎粒径大小是本工艺经济性的关键，破碎粒径过大，则气化工艺效率低，碳转化率低；破碎粒径过小，则破碎机磨损严重，电耗高，经济性差。破碎后燃料进入燃料筛分装置2，按设定粒径分离出满足设定粒径尺寸的燃料进入合格燃料仓3，粒径过大燃料则进入粒径不合格燃料仓4，而粒径不合格燃料仓4中燃料将被返回送入燃料破碎装置1中继续破碎至较小粒径，直至合格。以稻壳为例，稻壳原样粒径为长约7～10mm，宽2mm，外形如船形，只需简单破碎至1～5mm粒径燃料即可利用。以树枝、秸秆类为例，树枝、秸秆原样粒径较大，可选盘式或鼓式破碎机至50～100mm左右，再采用锤式粉碎机按如上所述给料预处理方案破碎至1～5mm粒径燃料即可利用。
2 ）微波等离子工作气体从入口11进入等离子发生器7中，激励成高温、高电离度、高活性的等离子体而喷入气化炉8中；
气化炉烧嘴6投运前2～3秒即开启微波等离子发生器7，部分氧化剂形式的微波等离子工作气体通过微波等离子工作气体入口11进入微波等离子发生器7，随后被激励成高温、高电离度、高活性的等离子气体喷入气化炉8。
3 ）载气将生物质燃料通过烧嘴6喷入气化炉8中，同时将氧化剂从氧气/蒸汽入口13再通过喷嘴6送入系统，与生物质燃料同时喷入气化炉内，生物质燃料粉粒在炉内高活性的等离子体氛围中进行高温快速热化学反应，生成含大量CO、H 2 和少部分CO 2 、CH 4 、H 2 S 、COS成分的合成气。
经破碎、筛分后满足设定粒径尺寸的生物质燃料颗粒由合格燃料仓3输送至气化炉炉前仓5，在炉前仓5下部通过气化剂气力输送至气化炉喷嘴6处，由喷嘴6处喷入气化炉内；氧化剂通过氧气/蒸汽入口13进入系统，与生物质燃料同时喷入气化炉内，由于采用高温气化工艺，燃料瞬间着火在炉内进行剧烈的部分氧化还原反应，生物质燃料在高温缺氧环境下，生成含大量CO、H 2 和少部分CO 2 、CH 4 、H 2 S 、COS成分的合成气；
合成气上行至等离子体反应区也即气化反应区，与水平/切向喷入的高温、高电离度、高活性的等离子气体混合，并进行高效气相反应，高温热化学气化反应区温度为1200℃～1800℃，中心区温度可高达1800℃～2000℃，工艺设计中保证该气化反应区的停留时间1～10秒，同时控制微波等离子功率，促进反应充分进行，最终合成气由气化炉顶部合成气出口9引出，合成气产物中有效成分CO和H 2 体积含量高达85%以上，且合成气中无焦油、酚类物质。生物质液态渣由气化炉排渣口9排出炉外，激冷后可实现无公害处理，同时也是良好的保温建筑材料。工艺中采用的蒸汽来源于对高温合成气的回收。
4 ）对合成气温度、成份进行监测来实时调整氧气流量、蒸汽流量及微波功率，维持气化工艺参数在控制范围内；合成气出口温度900℃～1200℃；高温合成气从顶部合成气出口9引出，同时液态渣由底部排渣口10排出。
步骤1）中，生物质燃料粉粒的粒径为0～5mm，较佳实例为2mm左右。
步骤2）和3）中，微波等离子工作气体和载气为空气和/或氧气和/或蒸汽；蒸汽来源于对自身高温合成气显热的回收。
为了使本工艺达到最佳工作效果，满足工艺整体性能要求，设计中关键是控制床层温度，调节好微波等离子功率及氧气、蒸汽的供给量。通过对合成气出口监测装置来达到对上述关键因素的控制，也能实现连锁控制，进行全自动化操作，提高运行稳定性。
以上所揭露的仅为本发明的较佳实施例而已，当然不能以此来限定本发明之权利范围，因此依本发明申请专利范围所作的等效变化，仍属本发明的保护范围。

Claims (10)

1 、一种微波等离子生物质气流床气化炉，包括竖直设置的炉体、由烧嘴构成的设置在炉体下部的燃料进口、炉体顶部的合成气出口、炉体底部的排渣口，炉体外还设置燃料预处理系统，包括燃料破碎装置、位于燃料破碎装置下游的筛分装置、筛分装置下游并列设置的粒径合格燃料仓和粒径不合格燃料仓、以及粒径合格燃料仓下游设置的炉前仓，炉前仓的底部通过烧嘴与炉体相连；气化炉顶部合成气出口布置有合成气监测单元；烧嘴沿炉体径向布置，数量为2～4个；其特征在于，在炉体的气化反应区上下布置1～2层微波等离子发生器，每层微波等离子发生器布置2～4个工作气体接入口。
2 、根据权利要求1所述的气化炉，其特征在于微波等离子发生器采用水平/切向布置方式。
3 、根据权利要求1或2所述的气化炉，其特征在于微波等离子发生器采用电极间距大、等离子体活性强、体积范围广的等离子发生器。
4 、根据权利要求3所述的气化炉，其特征在于微波等离子发生器微波功率源主频2.45GHz,单台功率约200kW以内。
5 、采用上述权利要求之一所述气化炉进行生物质气流床气化的工艺，其特征在于主要包括如下步骤：
1 ）生物质燃料先经过燃料预处理系统破碎、筛分后得到粒径合格的生物质燃料粉粒，并送入炉前仓备用；
2 ）微波等离子工作气体从入口进入等离子发生器中，激励成高温、高电离度、高活性的等离子体而喷入气化炉中；
3）生物质燃料粉粒通过烧嘴喷入气化炉中，同时将氧化剂从氧气/蒸汽入口送入系统，与生物质燃料同时喷入气化炉内，生物质燃料粉粒在炉内高活性的等离子体氛围中进行高温快速热化学反应，生成含大量CO、H 2 的合成气；
4 ）对合成气温度、成份进行监测来实时调整氧气流量、蒸汽流量及微波功率，维持气化工艺参数在控制范围内；合成气出口温度900℃～1200℃；最终高温合成气从顶部合成气出口引出，同时液态渣由排渣口排出。
6 、根据权利要求5所述的工艺，其特征在于步骤1）中，按设定粒径分离出满足设定粒径尺寸的燃料进入合格燃料仓，粒径过大燃料则进入粒径不合格燃料仓，而粒径不合格燃料仓中燃料将被返回送入燃料破碎装置中继续破碎至较小粒径，直至合格；经破碎、筛分后满足设定粒径尺寸的生物质燃料颗粒由合格燃料仓输送至气化炉炉前仓备用；生物质燃料粉粒的粒径为0～5mm。
7 、根据权利要求5或6所述的工艺，其特征在于步骤2）中，气化炉烧嘴投运前2～3秒即开启微波等离子发生器，部分氧化剂形式的微波等离子工作气体通过微波等离子工作气体入口进入微波等离子发生器，随后被激励成高温、高电离度、高活性的等离子气体喷入气化炉。
8 、根据权利要求7所述的工艺，其特征在于步骤3）中，生物质燃料粉粒通过载气由气化炉喷嘴喷入气化炉内；氧化剂通过氧气/蒸汽入口进入系统，与生物质燃料同时喷入气化炉内，由于采用高温气化工艺，燃料瞬间着火在炉内进行剧烈的部分氧化还原反应，生物质燃料在高温缺氧环境下，生成含大量CO、H 2 和少部分CO 2 、CH 4 、H 2 S 、COS成分的合成气；合成气上行至等离子体反应区也即气化反应区，与水平/切向喷入的高温、高电离度、高活性的等离子气体混合，并进行高效气相反应，高温热化学气化反应区温度为1200℃～1800℃，中心区温度为1800℃～2000℃，合成气在气化反应区的停留时间设定为1～10秒，同时控制微波等离子功率，促进反应充分进行。
9 、根据权利要求5或6或8所述的工艺，其特征在于步骤4）中，合成气产物中有效成分CO和H 2 体积含量高达85%以上，且合成气中无焦油、酚类物质；生物质液态渣由气化炉底部排渣口排出炉外，激冷后能够实现无公害处理，同时也是良好的保温建筑材料。
10 、根据权利要求9所述的工艺，其特征在于步骤2）和3）中，微波等离子工作气体和载气为空气和/或氧气和/或蒸汽；蒸汽来源于对自身高温合成气显热的回收。
PCT/CN2012/083562 2011-12-29 2012-10-26 一种微波等离子生物质气流床气化炉及工艺 WO2013097532A1 (zh)

Priority Applications (22)

Application Number Priority Date Filing Date Title
NO12863948A NO2799522T3 (zh) 2011-12-29 2012-10-26
CA2861691A CA2861691A1 (en) 2011-12-29 2012-10-26 Microwave plasma biomass entrained flow gasifier and process
BR112014015929A BR112014015929A2 (pt) 2011-12-29 2012-10-26 gaseificador de leito arrastado de biomassa de plasma de microondas e seu processo correspondente
AP2014007828A AP2014007828A0 (en) 2011-12-29 2012-10-26 Microwave plasma biomass entrained flow gasifier and process
ES12863948.1T ES2653255T3 (es) 2011-12-29 2012-10-26 Gasificador de biomasa de flujo arrastrado con plasma por microondas y su proceso
LTEP12863948.1T LT2799522T (lt) 2011-12-29 2012-10-26 Biomasės dujinimo sraute mikrobangų plazmos dujų generatorius ir būdas
DK12863948.1T DK2799522T3 (en) 2011-12-29 2012-10-26 REACTOR FOR GASATION OF MICROWAVE PLASMA BIOMASS WITH ENTRAINED FLOW AND SIMILAR PROCEDURE
SI201231160T SI2799522T1 (en) 2011-12-29 2012-10-26 A microwave flow biomass blower driven by a microwave plasma and a process
EP12863948.1A EP2799522B1 (en) 2011-12-29 2012-10-26 Microwave plasma biomass entrained flow gasifier and process
IN1472MUN2014 IN2014MN01472A (zh) 2011-12-29 2012-10-26
RU2014131271/05A RU2573016C1 (ru) 2011-12-29 2012-10-26 Микроволновой плазменный газификатор биомассы с перемещающимся потоком и способ газификации
JP2014549316A JP6207524B2 (ja) 2011-12-29 2012-10-26 マイクロ波プラズマバイオマス噴流床ガス化炉およびその方法
KR1020147020547A KR101695974B1 (ko) 2011-12-29 2012-10-26 극초단파 플라즈마 바이오매스 분류층 가스화기 및 공정
AU2012362083A AU2012362083B2 (en) 2011-12-29 2012-10-26 Microwave plasma biomass entrained flow gasifier and process
SG11201403659YA SG11201403659YA (en) 2011-12-29 2012-10-26 Microwave plasma biomass entrained flow gasifier and process
PL12863948T PL2799522T3 (pl) 2011-12-29 2012-10-26 Mikrofalowy gazyfikator plazmowy z przepływem pyłowym biomasy i sposób
MX2014007756A MX359878B (es) 2011-12-29 2012-10-26 Gasificador de flujo retenido de biomasa de plasma de microondas y proceso.
US14/314,023 US9518235B2 (en) 2011-12-29 2014-06-24 Entrained-flow gasifier and gasification method using the same for synthesizing syngas from biomass fuel
ZA2014/05492A ZA201405492B (en) 2011-12-29 2014-07-25 Microwave plasma biomass entrained flow gasifier and process
US15/344,569 US9873841B2 (en) 2011-12-29 2016-11-06 Entrained-flow gasifier and gasification method using the same for synthesizing syngas from biomass fuel
HRP20171932TT HRP20171932T1 (hr) 2011-12-29 2017-12-13 Mikrovalni uređaj za rasplinjavanje biomase putem plazme sa zajedničkim tokom i postupak
CY20171101328T CY1119830T1 (el) 2011-12-29 2017-12-19 Αεριοποιητης παρασυρομενης ροης βιομαζας μικροκυματικου πλασματος και διεργασια

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN201110449413.4 2011-12-29
CN201110449413.4A CN102559272B (zh) 2011-12-29 2011-12-29 一种微波等离子生物质气流床气化炉及工艺

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US14/314,023 Continuation-In-Part US9518235B2 (en) 2011-12-29 2014-06-24 Entrained-flow gasifier and gasification method using the same for synthesizing syngas from biomass fuel

Publications (1)

Publication Number Publication Date
WO2013097532A1 true WO2013097532A1 (zh) 2013-07-04

Family

ID=46405898

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2012/083562 WO2013097532A1 (zh) 2011-12-29 2012-10-26 一种微波等离子生物质气流床气化炉及工艺

Country Status (26)

Country Link
US (2) US9518235B2 (zh)
EP (1) EP2799522B1 (zh)
JP (1) JP6207524B2 (zh)
KR (1) KR101695974B1 (zh)
CN (1) CN102559272B (zh)
AP (1) AP2014007828A0 (zh)
AU (1) AU2012362083B2 (zh)
BR (1) BR112014015929A2 (zh)
CA (1) CA2861691A1 (zh)
CY (1) CY1119830T1 (zh)
DK (1) DK2799522T3 (zh)
ES (1) ES2653255T3 (zh)
HR (1) HRP20171932T1 (zh)
HU (1) HUE034963T2 (zh)
IN (1) IN2014MN01472A (zh)
LT (1) LT2799522T (zh)
MX (1) MX359878B (zh)
MY (1) MY170642A (zh)
NO (1) NO2799522T3 (zh)
PL (1) PL2799522T3 (zh)
PT (1) PT2799522T (zh)
RU (1) RU2573016C1 (zh)
SG (1) SG11201403659YA (zh)
SI (1) SI2799522T1 (zh)
WO (1) WO2013097532A1 (zh)
ZA (1) ZA201405492B (zh)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110055111A (zh) * 2018-03-16 2019-07-26 新能能源有限公司 流化床气化炉稳态排渣装置

Families Citing this family (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102559272B (zh) * 2011-12-29 2014-05-14 武汉凯迪工程技术研究总院有限公司 一种微波等离子生物质气流床气化炉及工艺
CN103589459B (zh) * 2013-11-20 2015-01-21 北京环宇冠川等离子技术有限公司 采用等离子体炬加热技术的煤气化方法及装置
DE102014204027A1 (de) * 2014-03-05 2015-09-10 Siemens Aktiengesellschaft Flugstromvergaser mit integriertem Mitteltemperaturplasma
CN104449846A (zh) * 2014-12-09 2015-03-25 贵州开阳化工有限公司 煤粉的制备及输送方法及装置
KR101669004B1 (ko) * 2015-04-30 2016-10-25 (주)그린사이언스 폐기물로부터 합성가스를 생성하는 가스화 방법, 폐기물로부터 합성가스를 생성하기 위한 가스화 장치 및 이를 포함하는 발전 시스템
CN104946281A (zh) * 2015-06-29 2015-09-30 山东大学 一种生物质气化热解过程中强化焦油裂解的装置与方法
ITUB20153783A1 (it) * 2015-09-22 2017-03-22 Endeavour S R L Reattore, impianto e processo di gassificazione per la gassificazione di combustibili fossili o non fossili, in particolare biomasse.
CN105419869A (zh) * 2015-11-16 2016-03-23 昆明理工大学 一种利用微波等离子体火炬处理紫茎泽兰的方法
CN105861006B (zh) * 2016-06-17 2019-12-03 东阳市琰安建筑工程有限公司 一种基于高电压电解式生物质加压热解工艺
US10059894B2 (en) * 2017-02-02 2018-08-28 Southern University And A&M College Gasifier
CN107118805A (zh) * 2017-06-15 2017-09-01 航天长征化学工程股份有限公司 一种粉煤掺烧可燃物的气化系统和方法
EP3498665B1 (en) * 2017-12-18 2020-09-02 Clariant International Ltd Method for the production of synthesis gas
CN110010436B (zh) * 2019-04-24 2024-05-14 南京奥依菲光电科技有限公司 等离子体流化床粉体处理装置
CN111595744B (zh) * 2020-06-09 2023-03-31 南京航空航天大学 一种气相射流中添加固体颗粒的装置及方法
CN111909730B (zh) * 2020-07-20 2021-03-26 来安县华阳玻璃制品有限公司 一种环保的玻璃生产用二段式煤气发生炉
CN113401869B (zh) * 2021-08-03 2023-07-25 辽宁科技大学 一种处理污泥生物质固废的双塔板化学链制氢装置及方法

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN201218507Y (zh) * 2008-05-29 2009-04-08 周开根 等离子体、氧化钙协同气化的垃圾生物质气化设备
CN101671578A (zh) * 2009-09-22 2010-03-17 武汉凯迪控股投资有限公司 可燃物料等离子体高温气化工艺及其设备
EP2163597A1 (en) * 2007-07-06 2010-03-17 Aba Research, S. A. De C. V. Method and apparatus for plasma gasificatiion of carbonic material by means of microwave radiation
CN102559272A (zh) * 2011-12-29 2012-07-11 武汉凯迪工程技术研究总院有限公司 一种微波等离子生物质气流床气化炉及工艺

Family Cites Families (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3948640A (en) * 1973-04-30 1976-04-06 Boliden Aktiebolag Method of carrying out heat-requiring chemical and/or physical processes
FR2555392B1 (fr) * 1983-11-17 1986-08-22 Air Liquide Procede de traitement thermique, notamment de coupage, par un jet de plasma
JPS63146400A (ja) * 1986-12-08 1988-06-18 バブコツク日立株式会社 プラズマト−チ
JPH08236293A (ja) * 1994-10-26 1996-09-13 Matsushita Electric Ind Co Ltd マイクロ波プラズマトーチおよびプラズマ発生方法
US9481584B2 (en) * 2001-07-16 2016-11-01 Foret Plasma Labs, Llc System, method and apparatus for treating liquids with wave energy from plasma
US6987792B2 (en) * 2001-08-22 2006-01-17 Solena Group, Inc. Plasma pyrolysis, gasification and vitrification of organic material
JP2003147373A (ja) * 2001-11-13 2003-05-21 Eco Technos:Kk プラズマによる有機物のガス化方法
CN100413564C (zh) * 2002-05-08 2008-08-27 刘健安 有害废物的处理方法及装备
CN1219857C (zh) * 2002-09-27 2005-09-21 中国科学院山西煤炭化学研究所 一种固态排渣干粉气流床气化方法及装置
US7279655B2 (en) * 2003-06-11 2007-10-09 Plasmet Corporation Inductively coupled plasma/partial oxidation reformation of carbonaceous compounds to produce fuel for energy production
CN1274791C (zh) * 2005-01-05 2006-09-13 太原理工大学 一种等离子煤气化工艺及装置
WO2006081661A1 (en) * 2005-02-04 2006-08-10 Plasco Energy Group Inc. Coal gasification process and apparatus
RU2007146271A (ru) * 2005-06-03 2009-06-20 Пласко Энерджи Групп Инк., (CA) Система для переработки углеродсодержащего сырья в газ определенного состава
CA2610808A1 (en) * 2005-06-03 2006-12-07 Plasco Energy Group Inc. A system for the conversion of coal to a gas of a specified composition
RU2318722C2 (ru) * 2006-04-10 2008-03-10 Федеральное государственное учреждение Российский научный центр "Курчатовский институт" Плазменный конвертор газообразного и жидкого углеводородного сырья и топлив в синтез-газ на основе микроволнового разряда
CN103995503A (zh) * 2006-05-05 2014-08-20 普拉斯科能源Ip控股集团毕尔巴鄂沙夫豪森分公司 用于将含碳原料转化成气体的控制系统
NZ573217A (en) * 2006-05-05 2011-11-25 Plascoenergy Ip Holdings S L Bilbao Schaffhausen Branch A facility for conversion of carbonaceous feedstock into a reformulated syngas containing CO and H2
US8475551B2 (en) * 2006-05-05 2013-07-02 Plasco Energy Group Inc. Gas reformulating system using plasma torch heat
US20080277265A1 (en) * 2007-05-11 2008-11-13 Plasco Energy Group, Inc. Gas reformulation system comprising means to optimize the effectiveness of gas conversion
JP5214314B2 (ja) * 2008-04-17 2013-06-19 新日鉄住金エンジニアリング株式会社 ガス化方法及びガス化装置
CN201530809U (zh) * 2009-09-22 2010-07-21 武汉凯迪控股投资有限公司 双级等离子体高温气化设备
CN101781584B (zh) * 2010-02-06 2012-09-26 周开根 等离子体煤气化的方法及设备
CN101906325B (zh) * 2010-07-20 2013-09-04 阳光凯迪新能源集团有限公司 生物质低温裂解高温气化工艺及其设备
CN102061196A (zh) * 2011-01-27 2011-05-18 中国科学院力学研究所 一种等离子体气化生活垃圾与生物质发电的方法和装置
CN202390392U (zh) * 2011-12-29 2012-08-22 武汉凯迪工程技术研究总院有限公司 一种微波等离子生物质气流床气化炉

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2163597A1 (en) * 2007-07-06 2010-03-17 Aba Research, S. A. De C. V. Method and apparatus for plasma gasificatiion of carbonic material by means of microwave radiation
CN201218507Y (zh) * 2008-05-29 2009-04-08 周开根 等离子体、氧化钙协同气化的垃圾生物质气化设备
CN101671578A (zh) * 2009-09-22 2010-03-17 武汉凯迪控股投资有限公司 可燃物料等离子体高温气化工艺及其设备
CN102559272A (zh) * 2011-12-29 2012-07-11 武汉凯迪工程技术研究总院有限公司 一种微波等离子生物质气流床气化炉及工艺

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP2799522A4 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110055111A (zh) * 2018-03-16 2019-07-26 新能能源有限公司 流化床气化炉稳态排渣装置
CN110055111B (zh) * 2018-03-16 2024-04-05 新能能源有限公司 流化床气化炉稳态排渣装置

Also Published As

Publication number Publication date
ES2653255T3 (es) 2018-02-06
EP2799522A4 (en) 2016-04-27
SG11201403659YA (en) 2014-10-30
US20170051216A1 (en) 2017-02-23
CY1119830T1 (el) 2018-06-27
JP2015503641A (ja) 2015-02-02
EP2799522A1 (en) 2014-11-05
KR20140120310A (ko) 2014-10-13
HUE034963T2 (en) 2018-05-02
ZA201405492B (en) 2015-10-28
CN102559272A (zh) 2012-07-11
LT2799522T (lt) 2018-01-25
PT2799522T (pt) 2017-12-26
AU2012362083A1 (en) 2014-08-21
MY170642A (en) 2019-08-21
RU2573016C1 (ru) 2016-01-20
MX359878B (es) 2018-10-15
JP6207524B2 (ja) 2017-10-04
US9873841B2 (en) 2018-01-23
PL2799522T3 (pl) 2018-03-30
US20140306160A1 (en) 2014-10-16
AP2014007828A0 (en) 2014-07-31
EP2799522B1 (en) 2017-09-20
DK2799522T3 (en) 2018-01-08
HRP20171932T1 (hr) 2018-02-09
MX2014007756A (es) 2015-05-15
CN102559272B (zh) 2014-05-14
US9518235B2 (en) 2016-12-13
AU2012362083B2 (en) 2016-06-09
BR112014015929A2 (pt) 2017-07-04
KR101695974B1 (ko) 2017-01-12
SI2799522T1 (en) 2018-04-30
CA2861691A1 (en) 2013-07-04
IN2014MN01472A (zh) 2015-04-24
NO2799522T3 (zh) 2018-02-17

Similar Documents

Publication Publication Date Title
WO2013097532A1 (zh) 一种微波等离子生物质气流床气化炉及工艺
KR101625152B1 (ko) 극초단파 플라즈마 바이오매스 가스화 고정층 가스화기 및 방법
JP6238907B2 (ja) 外部加熱型マイクロ波プラズマガス化炉及び合成ガス製造方法
CN103666580B (zh) 一种耦合式生物质加压热解工艺及系统
KR101471995B1 (ko) 탄화에 의해 바이오매스로부터 합성 가스를 제조하는 시스템 및 방법
JP2015507673A5 (zh)
US20200087589A1 (en) Pulverized coal gasification device and process for producing high heating value coal gas with low carbon residue content
CN106430206A (zh) 一种热解炉和电石炉联用生产电石的系统及方法
CN206720749U (zh) 利用废旧轮胎制备活性炭的系统
CN203582820U (zh) 一种耦合式生物质加压热解系统
CN108358204B (zh) 一种双床活性炭活化系统及活化方法
CN105861006B (zh) 一种基于高电压电解式生物质加压热解工艺
CN206266232U (zh) 一种热解炉和电石炉联用生产电石的系统
CN202390392U (zh) 一种微波等离子生物质气流床气化炉
CN107474881A (zh) 带活化段、两次气化的生物质颗粒下吸式气炭炉
CN208136180U (zh) 一种煤与石灰共同裂解制备乙炔的系统
CN205527774U (zh) 制备电石的系统
CN111019708A (zh) 一种高效生物质气化与能源利用系统及生物质气化与能源利用方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 12863948

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: MX/A/2014/007756

Country of ref document: MX

ENP Entry into the national phase

Ref document number: 2861691

Country of ref document: CA

Ref document number: 2014549316

Country of ref document: JP

Kind code of ref document: A

NENP Non-entry into the national phase

Ref country code: DE

WWE Wipo information: entry into national phase

Ref document number: IDP00201404241

Country of ref document: ID

ENP Entry into the national phase

Ref document number: 20147020547

Country of ref document: KR

Kind code of ref document: A

REEP Request for entry into the european phase

Ref document number: 2012863948

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2012863948

Country of ref document: EP

ENP Entry into the national phase

Ref document number: 2014131271

Country of ref document: RU

Kind code of ref document: A

ENP Entry into the national phase

Ref document number: 2012362083

Country of ref document: AU

Date of ref document: 20121026

Kind code of ref document: A

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: 112014015929

Country of ref document: BR

ENP Entry into the national phase

Ref document number: 112014015929

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20140626