WO2012059019A1 - 生物质气化成套装置及其系统 - Google Patents

生物质气化成套装置及其系统 Download PDF

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Publication number
WO2012059019A1
WO2012059019A1 PCT/CN2011/081415 CN2011081415W WO2012059019A1 WO 2012059019 A1 WO2012059019 A1 WO 2012059019A1 CN 2011081415 W CN2011081415 W CN 2011081415W WO 2012059019 A1 WO2012059019 A1 WO 2012059019A1
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Prior art keywords
biomass
gasification
fluidized bed
outlet
gas
Prior art date
Application number
PCT/CN2011/081415
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English (en)
French (fr)
Inventor
常厚春
马革
赵广健
陈平
覃勇付
陈燕芳
刘安庆
Original Assignee
广州迪森热能技术股份有限公司
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Priority claimed from CN2010105281060A external-priority patent/CN101967401A/zh
Priority claimed from CN2010105282307A external-priority patent/CN101967402A/zh
Priority claimed from CN2010105289240A external-priority patent/CN101967404B/zh
Priority claimed from CN2010105289058A external-priority patent/CN101967403A/zh
Priority claimed from CN2010105279145A external-priority patent/CN101967400A/zh
Priority claimed from CN201010528274XA external-priority patent/CN102041102B/zh
Application filed by 广州迪森热能技术股份有限公司 filed Critical 广州迪森热能技术股份有限公司
Publication of WO2012059019A1 publication Critical patent/WO2012059019A1/zh

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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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • 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
    • C10J3/503—Fuel charging devices for gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/158—Screws
    • 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
    • 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
    • C10J2300/0956—Air or oxygen enriched air
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1693—Integration of gasification processes with another plant or parts within the plant with storage facilities for intermediate, feed and/or product
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1869—Heat exchange between at least two process streams with one stream being air, oxygen or ozone
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/026—Dust removal by centrifugal forces
    • 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
    • Y02P20/133—Renewable energy sources, e.g. sunlight
    • 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 present invention relates to a biomass gasification plant and system thereof, and more particularly to a biomass gasification plant and system thereof using a fluidized bed gasifier.
  • Biomass energy raw materials are widely distributed, large in reserves, low in cost, and widely used. They are the only renewable energy that can be converted into clean fuel. The content of harmful substances (sulfur and nitrogen) is only medium-sized bituminous coal.
  • Biomass gasification refers to the processing of biomass raw materials, and then sent to a gasification furnace for gasification cracking under anoxic conditions to obtain a combustible gas. Sometimes, the produced gas is purified according to the application requirements. So get) J quality product gas.
  • biomass gasification is to pyrolysis, oxidation, reduction, reforming reaction, pyrolysis of biomass high polymer under the action of a certain thermodynamic condition by means of a gasification medium such as air, oxygen or water vapor.
  • a gasification medium such as air, oxygen or water vapor.
  • the associated tar is further thermally cracked or catalytically cracked into small molecular hydrocarbons, obtaining co,
  • Biomass gasification mainly includes gasification reaction, catalytic gas catalytic conversion and gas separation purification process (direct separation without purification). Taking air as the gasification medium as an example, the chemical reaction formula of biomass gasification can be expressed as:
  • biomass consists of cellulose and semi-fiber Composition of lignin, lignin, inert ash, etc., high oxygen content and volatile matter, and strong activation of coke. Therefore, biomass has higher gasification activity than coal, and is more suitable for gasification.
  • biomass gasification technology can be divided into two categories, one is fixed bed gasifier technology, and the other is fluidized bed gasifier technology.
  • the fixed bed gasification furnace can be further divided into a top suction fixed bed gasification furnace, a down suction fixed bed gasification furnace, a horizontal suction fixed bed gasification furnace, and a happy fixed bed gasification furnace;
  • the bed gasifier can be further divided into a fluidized bed gasifier and a double stream.
  • a biomass mixed gasification process and apparatus therefor are disclosed in Chinese Patent No. ZL 200410027427. 7 (CN 1232614C), which includes a pre-gasification stage and a post-gasification stage.
  • the biomass material in the pre-gasification stage, the biomass material is subjected to pyrolysis gasification by a circulating fluidized bed gasification process
  • the post gasification stage the biomass material is subjected to pyrolysis gasification by a downdraft gasification process.
  • the patented gasification unit is a composite gasification furnace consisting of a circulating fluidized bed gasifier and a downdraft fixed bed gasifier. It is characterized by the ability to simultaneously process different materials such as granular and massive biomass materials, but its disadvantage is that the gasifier has a complicated structure and is not suitable for large-scale gas production.
  • Cicle 1098911C discloses a biomass circulating fluidized bed gasification purification system using an air preheating circulating fluidized bed as a gas generation and air preheating system, by a cyclone separator, Wenqiu
  • the inner tube and the water washing tower constitute a gas purification system.
  • the circulating fluidized bed uses an inertial separator to separate the product from the incompletely reacted material, the carbon reflux is difficult to control; moreover, the cyclone used in the patent, The separated unreacted materials are directly discharged, which is wasteful, and brings about post-treatment or environmental problems.
  • the biomass gasification process used mainly has the following problems:
  • the gasification efficiency of the gasifier is low, and the gasifier has more ash and slagging;
  • the inlet structure of the silo of the storage device is easy to cause the gas generated during the production process to escape, and the gas leaks into the silo, which is easy to cause the material to be burned in the silo or even the silo.
  • the object of the present invention is to provide a biomass gasification complete device and a system thereof, which can improve gasification efficiency and gas heat generation, reduce generation of impurities such as tar and dust, reduce secondary pollution, and improve safety.
  • the present invention provides a biomass gasification apparatus comprising: a fluidized bed gasification reactor for preparing biomass gas; providing a reaction raw material for the fluidized bed gasification reactor Biomass feedstock supply system; two or more separation devices disposed outside the fluidized bed gasification reactor and separating the reaction products of the fluidized bed gasification reactor, the two or more separation devices At least a first separation device and a second separation device; and a gasification medium supply system for providing a gasification medium to the fluidized bed gasification reactor.
  • the fluidized bed gasification reactor comprises a first feed port and a second feed port disposed in a central portion thereof, a gasification medium inlet and a waste outlet disposed at a bottom portion thereof, and a upper portion disposed therein a material outlet; wherein, the first feed port of the fluidized bed gasification reactor is coupled to the biomass feedstock supply system, and the gasification medium inlet of the fluidized bed gasification reactor is coupled to the gasification medium supply system;
  • the first separating device comprises a material inlet disposed in an upper region thereof, a material outlet disposed in a central portion thereof, and a circulation outlet disposed at a bottom portion thereof; wherein the material inlet of the first separating device and the fluidized bed gasification reactor The material outlets are joined, and the circulation outlet of the first separating device is coupled to the second inlet of the fluidized bed gasification reactor through the first conveying device;
  • the second separating device includes a gas outlet disposed at a top portion thereof, a material inlet disposed at an upper portion thereof, and a circulation outlet disposed at a bottom portion thereof; wherein a material inlet of the second separation device is engaged with a material outlet of the first separation device
  • the circulation outlet of the second separation device is coupled to the second feed port of the fluidized bed gasification reactor through the second delivery device and the first delivery device.
  • biomass raw materials such as granular biomass raw materials are reacted with a gasification medium in a fluidized bed gasification reactor, and biomass polymers such as cellulose are pyrolyzed and oxidized.
  • the fluidized bed gasification reactor may be a gasification furnace, for example, a tower-like gasification tower; the gasification medium may be air, or may be a gasification medium to which other components are added in the air, or The gasification medium whose composition is adjusted, for example, according to different biomass materials, occasions and purposes, the oxygen, nitrogen, water vapor, and carbon dioxide content may be appropriately increased or decreased to Control conversion, yield, and composition of products such as gas.
  • the gasification medium supply system may include an air delivery device, such as a blower, and the air delivery device is connected to the gasification medium inlet at the bottom of the fluidized bed gasification reactor through a pipe, and the gasification medium is Blow in from the bottom of the fluidized bed gasification reactor.
  • an air delivery device such as a blower
  • the heat exchange apparatus may further be included, wherein the gas from the gas outlet of the second separation unit and the gasification medium from the gasification medium supply system flow through the heat exchange unit, and heat is generated Exchanging, the gasification medium is preheated, and the gas is cooled; after that, the preheated gasification medium is sent to the fluidized bed gasification reactor through the inlet of the gasification medium of the fluidized bed gasification reactor, and is cooled. The gas is sent to the downstream unit of the biomass gasification reaction system.
  • this design can cool the product leaving the reaction system, such as gas, so that it can be further utilized; on the other hand, the gasification medium can be preheated by the high-temperature gas to make the gasification medium entering the fluidized bed gasification reactor reach At a certain temperature, the reaction in the fluidized bed gasification reactor is facilitated, and the heat carried by the product is fully recovered.
  • the biomass feedstock supply system may include a pre-furnace storage device and a pre-furnace feed device; wherein, the pre-furnace storage device includes a buffer bin and a work bin, the buffer bin and the work bin respectively The feed port and the discharge port are included, and the feed port of the work bin is engaged with the discharge port of the buffer bin; the buffer bin and the work bin are connected by a gas lock device, and the gas lock device can be a narrow passage or
  • the valve is a kind of a drum valve, a ball valve or a drum valve, preferably a drum valve.
  • the sealing function of the drum valve is good, and when the valve is opened, the channel formed by the valve has a large size, which is more favorable for material transportation.
  • the pre-furnace feeding device feeds the raw material from the discharge port of the working chamber into the first feed port of the fluidized bed gasification reactor.
  • the buffer tank and the work compartment can be arranged up and down, and the top feed port of the work chamber is located below the bottom discharge port of the buffer tank; the feed end of the furnace feed device is located below the bottom discharge port of the work chamber. The discharge end is passed to the first feed port of the fluidized bed gasification reactor.
  • biomass materials such as biomass granular materials in the buffer warehouse.
  • biomass particles temporarily stored in the buffer chamber first enter the working chamber and fall into the furnace feeding device through the working chamber.
  • This design prevents the reaction gases, such as the hot reaction gases in the fluidized bed gasification reactor, from being leaked out of the working chamber.
  • Valves are provided at the bottom discharge port of the buffer tank and the working chamber, such as rotary valves, ball valves, drum valves, etc., and these rotary valves function as a gas lock device, for example, when the working chamber is turned to a fluidized bed
  • the rotary valve of the working chamber is opened, and the rotary valve of the buffer chamber is closed; and when the buffer chamber is fed to the working chamber, the rotary valve of the working chamber is closed, and The rotary valve of the buffer chamber is open.
  • the buffer bin may be plural.
  • the design of the buffer bins can also include both parallel connections and series connections.
  • the first conveying means, the second conveying means and/or the pre-furnace feeding means are screw conveying means.
  • the biomass gasification device of the present invention further comprises a silo and a feeding device, wherein the silo comprises a top feed port and a bottom discharge port, and the feeding device comprises a horizontal conveyor belt and a large dip angle conveyor belt;
  • the belt is located below the bottom discharge opening of the silo, the beginning of the large dip conveyor is engaged with the end of the horizontal conveyor belt, and the end of the large dip conveyor is located above the top feed opening of the buffer tank.
  • the biomass granular raw material enters the silo from the feed inlet at the top of the silo, falls from the discharge port at the bottom of the silo to the horizontal conveyor belt, and then passes from the horizontal conveyor belt to the large dip angle conveyor belt, which is finally transported by the large dip angle conveyor belt.
  • the biomass apparatus of the present invention may further comprise a biomass gasifier closed slag discharge device, comprising a rotating shaft and a cylinder, wherein the rotating shaft is installed in the cylinder body, and the spiral shaft is sleeved on the rotating shaft, and one end of the cylinder body There is a slag inlet, and the other end is provided with a slag outlet.
  • the cylinder is inclined, and the slag outlet is higher than the slag inlet, and the slag inlet of the cylinder is connected with the waste outlet at the bottom of the biomass gasifier.
  • the tilting design of the cylinder can well function as a gas lock.
  • the spiral blade on the rotating shaft is divided into two parts, and the spiral blades of the two parts are oppositely rotated and respectively disposed at both sides of the slag discharge port.
  • valves such as a rotary valve, a ball valve, a drum valve, and the like, are respectively provided at the slag inlet and the slag discharge port.
  • the valve of the slag outlet is in an open state, and the valve of the slag inlet is in a closed state; and when the biomass gasification furnace such as a fluidized bed gasification reactor is discharged to the slag discharge device
  • the valve of the slag discharge device of the slag discharge device is in a closed state, and the slag discharge port is in an open state, thereby further effectively controlling the leakage of gas in the furnace.
  • the gasifier closed slagging device may further include a water tank, and the slag outlet is connected to the water tank.
  • the formation of a water seal at the tap opening further effectively controls the leakage of gas in the furnace and simultaneously cools the hot ash to ensure the safety of the equipment and the human body.
  • the diameter of one of the rotating shafts is slightly larger than the diameter of the other portions, and in the rotating shaft inside the cylindrical body, the density of the ash is slightly changed at a slightly larger diameter, and the gas escape is prevented.
  • the portion of the shaft having a slightly larger diameter is located between the slag opening and the slag opening, on the side close to the slag opening.
  • the discharge end of the slag discharge device is provided with a water container filled with water to form a water seal at the discharge end of the slag discharge device.
  • the gas outlet of the second separating device is provided with a water sealing valve which is located before the heat exchange device.
  • the reaction system of the present invention further includes a discharge device including a vertically disposed discharge pipe and an ignition device disposed at the top end of the discharge pipe.
  • the outer cover of the water seal valve is provided with a discharge port, the discharge port is connected with the discharge pipe, and the outlet end of the discharge pipe is provided with an ignition device. In this way, the excess gas is burned off by the dispersing device, avoiding the explosion accident that may be caused by the gas return.
  • a plurality of ventilation ducts are arranged at the bottom of the fluidized bed gasification reactor, and the air inlet of the ventilation duct communicates with the gasification medium inlet of the fluidized bed gasification reactor.
  • the air outlet of the air duct is covered with a bucket-shaped hood, and the hood is provided with a plurality of small holes for spraying air while avoiding the air outlet of the ventilation duct being blocked by the biomass particles.
  • the biomass gasification device of the present invention may further comprise a gas curtain feeding device comprising: a motor and a deceleration device connected to the motor; and the motor and the deceleration device drive the rotation and fluidize a rotating shaft extending from the feed opening of the bed gasification reactor; a spiral blade fixedly attached to the rotating shaft; a feeding tube sleeved outside the spiral blade, the feeding pipe is provided with a feeding port and a discharging port, The feed port of the feed pipe is located below the discharge port of the pre-furnace storage device, and the discharge port of the feed pipe is connected to the feed port of the fluidized bed gasification reactor; the feed port and the discharge of the feed pipe There is a pore area between the mouths, and there are a plurality of air holes in the air hole area; a sealing cover which is sleeved outside the air hole area of the feeding pipe, and a joint portion of the sealing cover and the feeding tube is sealed; the sealing cover has an air inlet; the sealing is connected An air delivery device
  • the driving device including the motor and the speed reducing device
  • the rotating shaft constituting the spiral blade, and the feeding tube
  • the air delivery device may be a blower for conveying air into the sealing cover, and the air delivered by the air delivery device further enters the spiral conveying device through the air hole in the air hole of the feeding tube, and forms a gas curtain in the spiral conveying device to block the fluidized bed.
  • the gas produced by the gasification reactor leaks from the screw conveyor.
  • the air curtain In order for the air curtain to effectively block the gas, the air curtain should not be too close to the fluidized bed gasification reactor.
  • the preferred distance is that the air curtain, that is, the air hole area, is located between the feed port and the discharge port of the feed pipe.
  • the air holes for generating the air curtain are arranged along the circumferential direction of the feeding tube, that is, the trajectory of the air hole distribution is a circle on the feeding tube.
  • the pores in the pore zone may have one or more rows, that is, a circular track having a plurality of pores distributed in the pore region.
  • the number of vent holes is preferably eight.
  • the number of vent holes is preferably four per row, and the two vent holes are staggered.
  • a lock air feeding device may be further included, which includes a driving device that drives the rotating shaft, the spiral shaft is sleeved on the rotating shaft, and the outer sleeve of the spiral blade is sleeved.
  • a feed pipe the feed pipe has a feed port and a discharge port; wherein, the lock air feeding device further Included in the air lock structure at least one place between the feed port and the discharge port of the feed pipe; the lock structure can make the density of the biomass material in the feed pipe higher than the adjacent biomass material Density, thereby forming a relatively airtight structure.
  • the wind lock structure may be formed by a thicker one-stage rotating shaft which is thicker than the adjacent rotating shaft.
  • the air lock structure may have a pitch on the spiral blade between the feed port and the discharge port of the feed pipe which is smaller than the other portions.
  • the air lock structure may be such that the end of the rotating shaft is located in the feed pipe and at a certain distance from the discharge port of the feed pipe.
  • the pitch of the spiral blade be B
  • the cross-sectional area of the biomass material in the feed pipe is S
  • the rotation speed of the rotating shaft be N
  • the cross-sectional area of the biomass material of the thickened portion is S, that is, the volume of the biomass material conveyed per unit time of the pitch of the rotating portion of the bold portion is
  • V, B X S, x N.
  • the air lock structure may specifically be: a section on the rotating shaft between the feed port and the discharge port of the feed pipe is thicker than other portions.
  • the density of the biomass material in the thickened portion of the rotating shaft becomes larger, and the airtightness can be achieved.
  • the rotating shaft is too thick, the excessive biomass material will be compacted, and the motor may be stopped. Therefore, a section of the rotating shaft which is thicker than the other portions is not excessively long, and the length thereof is preferably a pitch of the spiral blade.
  • the air lock structure can be specifically: a spiral blade between the feed port and the discharge port of the feed pipe There is a section of pitch smaller than the other parts.
  • the pitch of the spiral blade is smaller than the length of the other portion, and the length of the spiral blade is preferably a pitch.
  • the air lock structure may specifically be: The end of the rotating shaft is located in the feeding pipe and has a certain distance from the discharging port of the feeding pipe.
  • the present invention also provides a biomass gasification parallel reaction system comprising:
  • Two or more fluidized bed gasification reactors for preparing biomass gas in parallel Two or more fluidized bed gasification reactors for preparing biomass gas in parallel;
  • each fluidized bed gasification reactor is provided with a separate separation device; two or more fluidized bed gasification reactors correspond to two or two sets.
  • the above separation device may share a set of biomass feedstock supply system and a set of gasification medium supply system, or each fluidized bed gasification reactor may be provided with a separate separation device for each fluidized bed gasification.
  • the reactor is provided with a separate biomass feedstock supply system and/or a gasification medium supply system.
  • this parallel system can save utility equipment.
  • this parallel system offers great flexibility, for example, depending on the specific situation, at the low load, the partially fluidized bed gasification reactor can be closed to the corresponding downstream.
  • the invention provides a multi-stage separation device, which can fully react the biomass particles, improve the gasification efficiency, save energy, generate more gas, and increase the calorific value of the gas; Due to the sufficient reaction of the biomass particles, the generation of tar and dust is reduced, the safety hazard of tar and dust in the fluidized bed gasification reactor is avoided, and the environmental pollution problem caused by the treatment of tar and dust is reduced.
  • FIG. 1 is a schematic structural view of a biomass gasification apparatus according to an embodiment of the present invention
  • FIG. 2 is a schematic longitudinal sectional view of a ventilation duct in a fluidized bed gasification reactor of the apparatus of FIG. 1
  • FIG. 4 is a schematic structural view of a specific embodiment of a gas curtain feeding device in the present invention
  • FIG. 5 is a schematic view of a biomass storage device in front of the biomass furnace of the present invention
  • Figure 6 is a schematic structural view of a specific embodiment of a gasifier closed slag discharge device according to the present invention
  • Figure 7 is a schematic view showing the structure of the first embodiment of the lock air feeding device of the present invention
  • Figure 8 is a schematic view showing the structure of the second embodiment of the lock air feeding device of the present invention
  • Figure 9 is a schematic view showing the structure of the third embodiment of the lock air feeding device of the present invention
  • Figure 10 is a parallel system according to an embodiment of the present invention. Front view (front view); Fig. 11 is a plan view of the parallel system shown in Fig. 10.
  • the biomass gasification apparatus of the present embodiment comprises: a fluidized bed gasification reactor such as a fluidized bed 1, a first separation device such as a cyclone separator 2, a second separation device such as a cyclone separator 3, Air delivery device such as blower 4, heat exchange device 5, buffer chamber 61, work chamber 62, pre-furnace feeding device such as screw Rotary conveyor 7, silo 8, horizontal conveyor belt 91, large angle conveyor belt 92, waste pipeline 101, slagging device such as screw conveyor 102, waste storage device 103, discharge pipe 1 11, ignition device 112, Water seal valve 12, gasification medium supply system.
  • a fluidized bed gasification reactor such as a fluidized bed 1
  • a first separation device such as a cyclone separator 2
  • a second separation device such as a cyclone separator 3
  • Air delivery device such as blower 4
  • heat exchange device such as blower 4
  • buffer chamber 61 such as a cyclone separator 2
  • work chamber 62 such as a cyclone separator 3
  • the top of the silo 8 has a feed port, and the bottom has a discharge port; the horizontal conveyor belt 91 is located below the bottom discharge port of the silo 8, and the start end of the large dip conveyor 92 is engaged with the end of the horizontal conveyor belt 91.
  • the end of the large angle conveyor belt 91 is located above the top feed port of the buffer tank 61.
  • the top of the buffer chamber 61 has a feed port, and the bottom has a discharge port; the top of the work chamber 62 has a feed port, and the bottom has a discharge port; the buffer chamber 61 and the work chamber 62 are arranged up and down, and the top of the work chamber 62 is fed.
  • the port is located below the bottom discharge opening of the buffer bin 61; a rotary valve is provided at the bottom discharge port of the buffer bin 61.
  • the feed end of the pre-furnace feeding device such as the screw conveyor 7, is located below the bottom discharge opening of the working chamber 62, and its terminal opens into the first feed port of the fluidized bed 1.
  • the fluidized bed 1 has a first feed port and a second feed port in the middle; a gasification medium inlet and a waste outlet at the bottom; and a material outlet at the upper portion thereof.
  • Waste outlet connection waste pipeline 101, waste pipeline 101 The outlet is equipped with a slagging device such as a screw conveyor 1 02.
  • the screw conveyor 102 is tilted upwards, i.e., its discharge end is higher than its feed end.
  • the discharge end of the screw conveyor 102 is provided with a waste storage device 103.
  • the first separating device such as the upper portion of the cyclone separator 2, has a material inlet, and the material inlet is connected to the material outlet of the fluidized bed 1 through a pipeline; the middle portion has a material outlet; the bottom portion has a circulation outlet; the circulation outlet is connected by a pipeline to be recycled.
  • the temporary storage device 21 has a first conveying device such as a screw conveyor leading to the second inlet of the fluidized bed 1 outside the bottom outlet of the retentate temporary storage device 21.
  • the second separating device such as the upper portion of the cyclone separator 3, has a material inlet; the top portion thereof has a gas outlet, the gas outlet is connected to the gas pipeline; the bottom portion has a circulation outlet; and the circulation outlet has a second conveying device leading to the recovery material temporary storage device 21 Such as a screw conveyor.
  • the heat exchange device 5 includes a gas inlet, a gas outlet and an air inlet, and an air outlet; the gas inlet and the gas outlet are respectively connected to the gas pipeline; and the air inlet and the air outlet are respectively connected to the air duct.
  • the second separating means such as the gas outlet of the cyclone 3, is provided with a water seal valve 12, which is located before the heat exchange means 5.
  • the water seal valve 12 is provided with a discharge port, the discharge port is connected to the discharge pipe 111, and the outlet end of the discharge pipe 111 is provided with an ignition device 112.
  • the air delivery device such as the air blower 4 is connected to the air inlet of the heat exchange device 5 through an air duct, and the air outlet of the heat exchange device 5 is connected to the gasification medium inlet at the bottom of the fluidized bed 1, and air is blown from the bottom of the fluidized bed 1 .
  • a plurality of ventilation ducts are disposed at the bottom of the fluidized bed 1.
  • the air inlet of the ventilation duct communicates with the air inlet of the fluidized bed 1, and the air outlet of the ventilation duct is covered with a bucket-shaped hood. There are a number of small holes in the hood.
  • the gasification medium supply system includes an air delivery device such as a blower, an air duct, an air inlet, and the like.
  • an air delivery device such as a blower, an air duct, an air inlet, and the like.
  • the biomass particles enter the buffer chamber 61 from the silo 8 via the horizontal conveyor belt 91 and the large dip conveyor belt 92, enter the working chamber 62 through the buffer tank 61, and then enter the fluidized bed 1 via the screw conveyor 7.
  • the blower 4 supplies air to the fluidized bed 1.
  • biomass particles react with air to form gas and solid waste such as C0, H2 and CH4.
  • the solid waste enters the waste storage device 103 via the waste pipe 101 and the screw conveyor 102.
  • the gas and the incompletely reacted biomass particles enter the cyclone 2, after which the gas and the lighter biomass particles enter the cyclone 3, and the heavier biomass particles are returned to the fluidized bed through the screw conveyor to continue to participate in the reaction. .
  • the gas and the lighter biomass particles are further separated, the gas enters the gas pipe, the air for the reaction is heated by the heat exchange device 5, and the gas is cooled, and the cooled gas is sent to the biomass gasification.
  • the specific embodiment of the air curtain feeding device used in the present invention comprises: a motor, a speed reducing device, a rotating shaft, a spiral blade, a feeding tube, a sealing cover 71, and an air blowing device such as a blower 72.
  • the motor is connected with the deceleration device, and the two drives the rotating shaft to rotate, the spiral shaft is fixedly sleeved on the rotating shaft, and the feeding tube is sleeved outside the spiral blade, and the feeding tube is provided with a feeding port and a discharging port.
  • the feed port of the feed pipe is located at the outlet of the feed pipe below the discharge port of the pre-furnace storage device and is connected to the feed port of the fluidized bed gasification reactor; the feed port and the discharge port of the feed pipe There is a vent area between the feed port and the discharge port of the feed pipe at a distance of 1 / 3, and away from the discharge port.
  • a biomass furnace front storage device includes a buffer chamber 61 and a work chamber 62.
  • the buffer chamber is provided with a feed port 63, and the bottom of the work chamber is provided with a discharge port 64 for buffering.
  • the cartridge 61 is disposed above the working chamber 62, the buffer chamber 61 is connected to the working chamber 62 through the drum valve 65, and the rotary valve 66 is disposed at the discharge port 64 at the bottom of the working chamber, and the rotary valve 66 is selected as the valve at the position. Better interface with the lower feeder.
  • the rotary valve of the working chamber discharge port is opened, and the drum valve between the buffer chamber and the working chamber is closed, and when the buffer chamber is working
  • the rotary valve of the working compartment discharge port is closed, and the drum valve between the buffer bin and the working bin is opened.
  • a specific embodiment of a biomass gasifier closed slagging device 102 of the present invention includes a rotating shaft 71 and a cylinder 72.
  • the rotating shaft 71 is installed in the cylinder 72, and the rotating shaft 71 is sleeved with a spiral blade 73 and a cylinder.
  • One end of the body 72 is provided with a slag opening 74, and the other end is provided with a slag opening 75.
  • the spiral blade 73 on the rotating shaft 71 is divided into two parts, and the spiral blades of the two parts are oppositely rotated and respectively disposed at the slag opening 75.
  • a rotary valve (not shown) is respectively disposed at the slag inlet 74 and the slag outlet 75.
  • the cylinder 72 is inclined, and the slag opening 75 is higher than the slag opening 74, and the cylinder 72 is advanced.
  • the slag port 74 is connected to a waste outlet at the bottom of a biomass gasifier (such as a fluidized bed), and the slag port 75 is connected to the water tank 103.
  • the diameter of one of the rotating shafts 71 is slightly larger than the diameter of the other portion, and the portion of the shaft having a slightly larger diameter is located between the slag opening 74 and the slag opening 75 on the side close to the slag opening 75. As shown in FIG.
  • the lock air feeding device of the present invention comprising: a motor, a speed reducing device, a rotating shaft, a spiral blade, and a feeding pipe.
  • the motor is connected to the deceleration device, and the two drives the rotating shaft to rotate, the spiral shaft is fixedly sleeved on the rotating shaft, and the feeding tube is sleeved outside the spiral blade, and the feeding tube is provided with a feeding port and a discharging port, and the rotating shaft is provided The discharge port of the terminal and the feed pipe are flush.
  • the feed port of the feed pipe is located at the outlet of the feed pipe below the discharge port of the pre-furnace storage device and is connected to the feed port of the fluidized bed gasification reactor; the feed port and the discharge port of the feed pipe There is a section on the axis of rotation that is thicker than the other part.
  • the length of the section of rotation that is thicker than the other part is a pitch of the spiral blade (see Figure ⁇ Shown in a).
  • Figure 8 shows a second embodiment of the lock air feeding device of the present invention, which differs from the first embodiment in that: the diameter of the rotating shaft is constant, but between the feed port and the discharge port of the feed pipe
  • the spiral blade has a section of pitch smaller than the other parts (as shown by b in Fig. 8).
  • Figure 9 shows a third embodiment of the lock air feeding device of the present invention, which differs from the first embodiment in that: the diameter of the rotating shaft is constant, but the end of the rotating shaft does not reach the discharge port of the feeding pipe, There is a certain distance between the end of the rotating shaft and the discharge port of the feed pipe (as shown by c in Figure 9).
  • 10 and 11 are schematic views of a parallel gasification system according to an embodiment of the present invention, the embodiment comprising two fluidized bed gasification reactors, each fluidized bed gasification reactor comprising a two-stage separation device, Each fluidized bed gasification reactor includes its separate gasification medium supply system.

Description

生物质气化成套装置及其系统
技术领域 本发明涉及一种生物质气化成套装置及其系统， 更具体地讲， 本发明涉 及一种采用流化床气化炉的生物质气化成套装置及其系统。
背景技术
生物质能源原料分布广、 储量大、 成本低、 应用范围广， 是唯一可以转 化为清洁燃料的可再生能源， 其有害物质（硫和氮等） 含量仅为中质烟煤的
1/10 , 同时其能源利用可实现温室气体 C02零排放。
生物质气化是指将生物质原料加工处理后， 送入气化炉中， 在缺氧的条 件下进行气化裂解， 得到可燃气体， 有时根据应用需要还要对产出气经行净 化处理从而得 )J优质的产品气。
生物质气化原理是在一定的热力学条件下， 借助于气化介质如空气、 氧 气或水蒸气等的作用， 使生物质的高聚物发生热解、 氧化、 还原、 重整反应， 热解伴生的焦油进一步热裂化或催化裂化成为小分子碳氢化合物， 获得 co、
H2和 CH4等可燃气体。 生物质气化主要包括气化反应、 合成气催化变换和气 体分离净化过程（直接燃用的不用分离净化）。 以空气为气化介质为例， 生物 质气化化学反应通式可以表示为：
CH1 40。 6+0. 402+1· 5Ν2=0· 7CO+0. 3CO2+0. 6Η2+0· 1H20+ (1. 5N2) 一般而言， 生物质由纤维素、 半纤维素、 木质素、 惰性灰等组成， 含氧 量和挥发份高， 焦炭的活化性强， 因此生物质与煤相比， 具有更高的气化活 性， 更适合气化。
从所采用的气化炉的角度来看， 生物质气化技术可以分为两大类， 一类 是固定床气化炉技术， 一类是流化床气化炉技术。 其中， 固定床气化炉又可 以分为上吸式固定床气化炉、 下吸式固定床气化炉、 横吸式固定床气化炉、 以及开心式固定床气化炉等； 流化床气化炉又可以分为流化床气化炉、 双流 化床气化炉、 以及循环流化床气化炉等。
中国专利 ZL 200410027427. 7 ( CN 1232614C ) 中公开了一种生物质混 合气化工艺及其装置， 其包括前气化阶段和后气化阶段。 其中， 在前气化阶 段， 生物质物料采用循环流化床气化工艺进行热解气化， 在后气化阶段， 生 物质物料采用下吸式气化工艺进行热解气化。 该专利的气化装置是一种由循 环流化床气化炉和下吸式固定床气化炉组成的复合式气化炉。 其特点是能够 同时处理不同形态如粒状和块状的生物质物料，但其缺点是气化炉结构复杂， 而且不适合大规模制气的场合。
中国专利 ZL 98122264. 1 (CN 1098911C)公开了一种生物质循环流化床 气化净化系统，其采用空气预热式循环流化床作为燃气生成和空气预热系统， 由旋风分离器、 文丘里管和水洗塔构成燃气净化系统。 但这种装置由于采用 循环流化床， 而循环流化床采用惯性分离器对产物和未完全反应的物料进行 分离， 因而其炭回流难以控制； 而且， 该专利中所采用的旋风分离器， 将分 离出的未反应完全的物料被直接排放， 既浪费， 又带来了后处理或环保问题。
目前， 采用的生物质气化工艺主要存在如下几个问题：
(1) 气化炉气化效率低， 气化炉积灰及结渣较多；
(2) 燃气发热量偏低， 限制了用户用气的积极性；
(3) 杂质含量高， 焦油和灰尘沉积严重， 影响生产的连续性；
(4) 二次污染问题： 部分生物质气化机组采用湿式净化技术， 冷却水中 含有多种有害物质， 如酚、 氨等， 从而造成二次污染；
(5) 储料装置的料仓进口结构处易导致生产过程中产生的气体外逸， 气 体泄露到料仓中容易引发生物质原料在料仓中燃烧甚至料仓爆炸。
发明内容
针对现有技术的缺点， 本发明的目的是提供一种生物质气化成套装置及 其系统， 以提高气化效率和燃气发热量， 减少焦油和灰尘等杂质的生成， 减 少二次污染， 提高安全性。 一方面， 为了实现上述目的， 本发明提供了一种生物质气化装置， 其包 括： 用于制备生物质燃气的流化床气化反应器； 为该流化床气化反应器提供 反应原料的生物质原料供给系统； 设置于该流化床气化反应器之外、 并对该 流化床气化反应器之反应产物进行分离的两级以上的分离装置， 该两级以上 的分离装置至少包括第一分离装置和第二分离装置； 以及为流化床气化反应 器提供气化介质的气化介质供给系统。
优选地， 上述流化床气化反应器包括设置于其中部区域的第一进料口和 第二进料口、 设置于其底部的气化介质入口和废弃物出口、 以及设置于其上 部区域的物料出口； 其中， 流化床气化反应器的第一进料口与生物质原料供 给系统相接合， 流化床气化反应器的气化介质入口与气化介质供给系统相接 合；
上述第一分离装置包括设置于其上部区域的物料入口、 设置于其中部区 域的物料出口以及设置于其底部的循环出口； 其中， 第一分离装置的物料入 口与流化床气化反应器的物料出口相接合， 第一分离装置的循环出口通过第 一输送装置与流化床气化反应器的第二进料口相接合； 以及
上述第二分离装置包括设置于其顶部的燃气出口、 设置于其上部区域的 物料入口、 设置于其底部的循环出口； 其中， 第二分离装置的物料入口与第 一分离装置的物料出口相接合， 第二分离装置的循环出口通过第二输送装置 和第一输送装置与流化床气化反应器的第二进料口相接合。 在本发明的生物质气化装置中， 生物质原料如颗粒状的生物质原料在流 化床气化反应器与气化介质发生反应，生物质的聚合物如纤维素等发生热解、 氧化、 还原、 重整等复杂的系列反应， 得到 C0、 H2和 CH4等燃气， 其中， 热 解伴生的焦油进一步热裂化或催化裂化成为小分子碳氢化合物。 流化床气化反应器可以是气化炉， 例如可以是塔状的气化塔； 气化介质 可以空气， 也可以是在空气中添加了其它成分的气化介质， 或者是对空气中 各成分进行了调节的气化介质， 例如， 根据不同的生物质原料、 场合以及目 的， 可以适当地增加或减少氧气、 氮气、 水蒸气、 以及二氧化碳的含量， 以 控制转化率、 产率以及产物如燃气的组成。 在本发明的生物质气化装置中， 气化介质供给系统可以包括风送装置， 如鼓风机，风送装置通过管道连接于流化床气化反应器底部的气化介质入口， 将气化介质从流化床气化反应器的底部吹入。 在本发明的生物质气化装置中， 可以进一步包括热交换装置， 其中， 来 自第二分离装置燃气出口的燃气和来自气化介质供给系统的气化介质流经该 热交换装置， 并发生热交换， 气化介质被预热， 燃气被冷却； 之后， 被预热 的气化介质则经由流化床气化反应器的气化介质入口， 送入流化床气化反应 器， 而被冷却的燃气则送至生物质气化反应系统的下游装置。 这种设计一方 面可以使离开反应系统的产物如燃气降温， 以便其进一步被利用； 另一方面， 可以利用高温燃气预热气化介质， 使得进入流化床气化反应器的气化介质达 到一定温度， 便于流化床气化反应器中的反应平稳进行， 充分回收产物所携 带的热量。 在本发明的生物质气化装置中， 其生物质原料供给系统可以包括炉前储 料装置和炉前送料装置； 其中， 炉前储料装置包括緩沖仓和工作仓， 緩沖仓 和工作仓分别包括进料口和出料口，工作仓的进料口与緩沖仓的出料口接合； 緩沖仓与工作仓之间通过一锁气装置连接相通，锁气装置可以为一狭窄通道， 也可以为阀门； 阀门为滚筒阀、 球阀或滚筒阀的一种， 优选为滚筒阀， 滚筒 阀的封闭性好， 并且阀门打开时， 其形成的通道尺寸大， 更有利于物料的输 送。 炉前送料装置将来自工作仓出料口的原料送入流化床气化反应器的第一 进料口。
例如， 上述的緩沖仓和工作仓可以上下排布， 工作仓的顶部进料口位于 緩沖仓的底部出料口的下方； 炉前送料装置的进料端位于工作仓的底部出料 口下方， 其出料端通入流化床气化反应器的第一进料口。
緩沖仓内存有生物质原料如生物质颗粒状原料， 工作时， 緩沖仓内暂存 的生物质颗粒先进入工作仓， 通过工作仓落入炉前送料装置。 这种设计可以 防止反应系统如流化床气化反应器中热的反应气体由工作仓外泄。 优选地， 在緩沖仓和工作仓的底部出料口处均设有阀门， 如旋转阀、 球阀、 滚筒阀等， 而且这些旋转阀起到一种锁气装置的作用， 例如， 当工作仓向流化床气化反 应器中供料时， 则工作仓的旋转阀处于打开状态， 而緩沖仓的旋转阀处于闭 合状态； 而当緩沖仓向工作仓加料时， 则工作仓的旋转阀处于关闭状态， 而 緩沖仓的旋转阀处于打开状态。 这样的设计可以 4艮好地解决向反应系统中加 料时防止反应气体外泄的问题。 进一步地， 緩沖仓可以是多个， 例如， 可以 有多个平行的緩沖仓， 每个都与工作仓直接相连， 但其旋转阀依次打开， 这 样的设计可以适应连续进料的反应系统； 或者， 多个緩沖仓是串联连接， 其 中， 只有一个靠近工作仓的緩沖仓与工作仓直接连接， 这样的设计是一种多 级锁气装置， 进一步降低反应气体外泄的可能性； 当然， 多个緩沖仓的设计 方案也可以是既包括平行连接， 也包括串联连接。 优选地， 在本发明的生物质气化装置中， 第一输送装置、 第二输送装置 和 /或炉前送料装置为螺旋输送装置。 进一步地， 在本发明的生物质气化装置中还包括料仓及送料装置， 其中， 料仓包括顶部进料口和底部出料口， 送料装置包括水平输送带和大倾角输送 带； 水平输送带位于料仓的底部出料口下方， 大倾角输送带的起始端与水平 输送带末端相接合， 大倾角输送带的末端位于緩沖仓的顶部进料口上方。 生 物质颗粒状原料从料仓顶部的进料口进入料仓， 从料仓底部的出料口落到水 平输送带上， 再由水平输送带转至大倾角输送带， 由大倾角输送带最终完成 向緩沖仓加料。 由于流化床气化反应器会产生一些固体废弃物， 若不及时排除会影响气 化反应的正常进行。 因而， 本发明的生物质装置还可以包括一种生物质气化 炉密闭排渣装置， 其包括转轴和筒体， 其中， 转轴安装在筒体内， 转轴上套 设有螺旋叶片， 筒体的一端设有进渣口， 另一端设有出渣口， 筒体倾斜设置， 其出渣口高于进渣口， 筒体的进渣口与生物质气化炉底部的废弃物出口连接 相通。 由于应用该密闭排渣装置的生物质气化炉通常为一微正压系统， 所以 筒体的这种倾斜设计可以很好地起到锁气作用。 在上述的密闭排渣装置中， 转轴上的螺旋叶片分为两部分， 该两部分的 螺旋叶片旋向相反并分别设置在出渣口的两侧。 当灰渣从进渣口进入筒体时， 转动的螺旋叶片将灰渣向前推到出渣口， 并联同出渣口另一侧的旋向相反的 螺旋叶片一起将灰渣挤入出渣口， 进行高效且彻底的出渣。
在上述的密闭排渣装置中， 在进渣口和出渣口处分别设有阀门， 如旋转 阀、 球阀、 滚筒阀等。 当排渣装置向外排渣时， 则出渣口的阀门处于打开状 态， 而进渣口的阀门处于闭合状态； 而当生物质气化炉如流化床气化反应器 向排渣装置排渣时， 则排渣装置进渣口的阀门处于关闭状态， 而出渣口处于 打开状态， 进一步有效控制炉内气体的外泄。
上述的气化炉密闭排渣装置还可以包括一水箱， 出渣口与该水箱连接相 通。 在出渣口形成水封进一步有效控制炉内气体的外泄， 并且同时对炽热的 灰渣进行冷却， 保证了设备和人身的安全。
在上述的密闭排渣装置中，转轴其中一段的直径略大于其他部分的直径， 在筒体内部的转轴中， 直径略大处会发生灰渣的密度改变， 对防止气体的外 逸起到一定作用， 优选地， 直径略大的转轴部分位于进渣口与出渣口之间、 靠近出渣口的一侧。 优选地， 排渣装置出料端设置有装有水的水容器， 以便 在排渣装置出料端形成水封。 为了控制燃气的通和关， 第二分离装置的燃气出口设有水封阀， 该水封 阀位于热交换装置之前。 若用户需要的燃气较少， 而反应系统产生的燃气较 多， 多余的燃气会通过燃气管道、 第二分离装置、 第一分离装置返回流化床 气化反应器， 这种情况会导致爆炸等危重事故。 为了避免这种情况的发生， 本发明的反应系统还包括放散装置， 该放散装置包括竖直设立的放散管道和 设置于该放散管道顶端的点火装置。 水封阀的外罩上设有一个放散口， 该放 散口连接放散管道， 放散管道的出口端设有点火装置。 这样， 多余的燃气通 过放散装置燃烧掉， 避免了燃气回流可能导致的爆炸事故。 为了增加生物质颗粒的流化效果， 在流化床气化反应器的底部置有多个 通风管道， 通风管道的进风口与流化床气化反应器的气化介质入口相通， 通 风管道的出风口上罩有斗笠形的风帽， 风帽上置有多个小孔， 用于喷出空气 同时避免通风管道的出风口被生物质颗粒堵塞。 在本发明的生物质气化装置中还可以包括一种气幕进料装置， 该气幕进 料装置包括： 电机及连接于电机的减速装置； 由电机及减速装置驱动旋转、 并向流化床气化反应器的进料口延伸的旋转轴； 固定套接在旋转轴上的螺旋 叶片； 套在螺旋叶片之外的进料管， 进料管上设有进料口和出料口， 进料管 的进料口位于炉前储料装置的出料口下方， 进料管的出料口连接于流化床气 化反应器的进料口； 进料管的进料口和出料口之间具有气孔区， 气孔区内具 有多个气孔； 套在进料管气孔区之外的密封罩， 密封罩与进料管的结合部密 封； 密封罩上具有一进风口； 连接于密封罩上进风口的风送装置。
其中， 在上述的气幕进料装置中， 驱动装置（包括电机和减速装置）、 旋 转轴、 螺旋叶片、 进料管组成了螺旋输送装置。 风送装置可为鼓风机， 用于 向密封罩内输送空气， 风送装置输送的空气进一步通过进料管气孔区的气孔 进入螺旋输送装置， 在螺旋输送装置内形成一道气幕， 阻止流化床气化反应 器产生的燃气从螺旋输送装置泄露。
在上述的气幕进料装置中， 越接近流化床气化反应器， 燃气产生的压强 越大。 为了使气幕能够有效地阻止燃气， 气幕不宜距离流化床气化反应器太 近。 其优选的距离为气幕即气孔区位于进料管的进料口与出料口之间距离的
1 / 3处， 且远离出料口。
为了使气幕产生的阻力不分散、 足够大， 产生气幕的气孔沿进料管周向 排布， 即气孔分布的轨迹为进料管上的一个圓。 气孔区内的气孔可以有一排 或多排， 即气孔区内内有多个气孔分布的圓轨迹。 当气孔区内有一排气孔时， 气孔的数目优选为 8个。 当气孔区内有两排气孔时， 气孔的数目优选为每排 4个， 且两排气孔交错排布。 在本发明的生物质气化装置中， 还可以包括一种锁风进料装置， 其包括 驱动装置， 该驱动装置驱动连接旋转轴， 旋转轴上套接有螺旋叶片， 螺旋叶 片的外围套设进料管， 进料管具有进料口和出料口； 其中， 锁风进料装置还 包括位于进料管的进料口和出料口之间的至少一处的锁风结构； 该锁风结构 能够使得进料管中的某处生物质原料的密度高于相邻的生物质原料密度， 从 而形成相对气密的结构。
作为本发明锁风进料装置的一种具体实施方式， 锁风结构可以由较粗的 一段旋转轴形成， 该较粗的一段旋转轴比与之相邻的旋转轴更粗。
作为本发明锁风进料装置的另一种具体实施方式， 锁风结构可以为所述 进料管的进料口和出料口之间的螺旋叶片上有一段螺距小于其它部分。
作为本发明锁风进料装置的再一种具体实施方式， 锁风结构可以为旋转 轴的终端位于进料管内， 且和所述进料管的出料口之间有一定距离。
以下通过计算可以更好地阐明本发明锁风进料装置的基本原理：
令螺旋叶片的螺距为 B , 进料管内的生物质原料截面积为 S , 旋转轴的转 速为 N , 则螺旋输送装置的一个螺距单位时间内输送的生物质原料体积为： V=B x S x N。
当旋转轴上的某一段加粗， 该加粗部分的生物质原料截面积为 S， ， 即 该加粗部分旋转轴的一个螺距单位时间内输送的生物质原料体积为
V， = B X S， x N。
由于 S， < S，因而 V， < V。
实际送料量 M=M， ， 即 V X P =V， χ ρ， 。
由于 V， < V , 因而 ρ， > ρ , 即旋转轴加粗部分的生物质原料密度变 大， 气密性变大。
因而锁风结构具体可为： 进料管的进料口和出料口之间的旋转轴上有一 段粗于其它部分。
旋转轴加粗部分的生物质原料密度变大， 能够实现气密， 但旋转轴加粗 部分过长的话， 会压实过多的生物质原料， 甚至导致电机停转。 因而旋转轴 上粗于其它部分的一段不宜过长， 其长度为螺旋叶片的一个螺距为宜。
另外， 当旋转轴上某一段螺旋叶片的螺距变小 （小于相邻螺旋叶片的螺 巨）， 即 < Β , 同样可以实现 V， < V , 进而实现 Ρ， > ρ。
因而锁风结构具体又可为： 进料管的进料口和出料口之间的螺旋叶片上 有一段螺距小于其它部分。
同样基于避免电机停转的考虑， 螺旋叶片上螺距小于其它部分的一段不 宜过长， 其长度为螺旋叶片的一个螺距为宜。
另外， 当旋转轴的终端未到达进料管的出料口， 即旋转轴的终端和进料 管的出料口之间有一段距离， 由于该段距离内不再有螺旋叶片的推动， 因而 部分生物质原料堆积于此， 同样可以实现气密锁风。
因而锁风结构具体又可为： 旋转轴的终端位于进料管内， 且和进料管的 出料口之间有一定距离。 另一方面， 为了实现本发明的发明目的， 本发明还提供了本发明提供了 一种生物质气化并联反应系统， 其包括：
两个或两个以上的、 并行设置的用于制备生物质燃气的流化床气化反应 器；
两套或两套以上的、 分别设置于每个流化床气化反应器之外并对该流化 床气化反应器之反应产物进行分离的两级以上的分离装置， 每套分离装置至 少包括第一分离装置和第二分离装置；
在本本发明的生物质气化并联反应系统中， 每个流化床气化反应器对应 设有单独的分离装置； 两个或两个以上的流化床气化反应器对应两套或两套 以上的分离装置， 其可以共用一套生物质原料供给系统和一套气化介质供给 系统， 也可以是每个流化床气化反应器对应设有单独的分离装置每个流化床 气化反应器对应设有单独的生物质原料供给系统和 /或气化介质供给系统。一 方面， 这种并联系统可以节省公用设备， 另一方面， 这种并联系统提供了巨 大的灵活性， 例如可以根据具体情况， 低负荷时可以关闭部分流化床气化反 应器极其对应的下游设备， 高负荷时可开启所有的流化床气化反应器。 与现有技术相比， 本发明设置了多级分离装置， 使生物质颗粒能够充分 反应， 提高了气化效率， 节约了能源， 产生了更多燃气， 提高了燃气发热量； 由于生物质颗粒反应充分， 减少了焦油和灰尘的产生， 避免了焦油和灰尘在 流化床气化反应器内形成的安全隐患， 同时减少了处理焦油和灰尘带来的环 境污染问题。
以下结合附图和实施例， 来进一步说明本发明， 但本发明不局限于这些 实施例， 任何在本发明基本精神上的改进或替代， 仍属于本发明权利要求书 中所要求保护的范围。
附图说明 图 1是本发明中一生物质气化装置具体实施方式的结构示意图； 图 2是图 1装置中流化床气化反应器内通风管道排布纵截面示意图； 图 3是图 1装置中流化床气化反应器内通风管道排布横截面示意图； 图 4是本发明中一气幕进料装置具体实施方式的结构示意图； 图 5是本发明中一生物质炉前储料装置具体实施方式的结构示意图； 图 6是本发明中一气化炉密闭排渣装置具体实施方式的结构示意图； 图 7是本发明中锁风进料装置第一实施例的结构示意图；
图 8是本发明中锁风进料装置第二实施例的结构示意图； 图 9是本发明中锁风进料装置第三实施例的结构示意图； 图 10是本发明一具体实施方式之并联系统的正面观察图 （前视图）； 图 11是图 10所示并联系统的俯视图。
具体实施方式
如图 1所示， 本实施例的生物质气化装置包括： 流化床气化反应器如流 化床 1、 第一分离装置如旋风分离器 2、 第二分离装置如旋风分离器 3、 风送 装置如鼓风机 4、 热交换装置 5、 緩沖仓 61、 工作仓 62、 炉前送料装置如螺 旋输送机 7、 料仓 8、 水平输送带 91、 大倾角输送带 92、 废弃物管道 101、 排渣装置如螺旋输送机 102、 废弃物存储装置 1 03、 放散管道 1 11、 点火装置 112、 水封阀 12、 气化介质供给系统。
其中， 料仓 8的顶部具有进料口， 底部具有出料口； 水平输送带 91位于 料仓 8的底部出料口下方， 大倾角输送带 92的起始端与水平输送带 91的末 端相接合， 大倾角输送带 91的末端位于緩沖仓 61的顶部进料口上方。
緩沖仓 61的顶部具有进料口， 底部具有出料口； 工作仓 62的顶部具有 进料口， 底部具有出料口； 緩沖仓 61和工作仓 62上下排布， 工作仓 62的顶 部进料口位于緩沖仓 61的底部出料口的下方； 緩沖仓 61的底部出料口处设 有旋转阀。炉前送料装置如螺旋输送机 7的起始端位于工作仓 62的底部出料 口下方， 其终端通入流化床 1的第一进料口。
流化床 1 中部具有第一进料口和第二进料口； 其底部具有气化介质入口 和废弃物出口； 其上部具有物料出口。 废弃物出口连接废弃物管道 101 , 废 弃物管道 101 出口处置有排渣装置如螺旋输送机 1 02。 螺旋输送机 102向上 倾斜， 即其出料端高于其进料端。 螺旋输送机 102的出料端置有废弃物存储 装置 1 03。
第一分离装置如旋风分离器 2的上部具有物料入口， 该物料入口与流化 床 1的物料出口通过管道相连； 其中部具有物料出口； 其底部具有循环出口； 该循环出口通过管道连接一回收物暂存装置 21 , 回收物暂存装置 21 的底部 出口外具有通向流化床 1第二进料口的第一输送装置如螺旋输送机。
第二分离装置如旋风分离器 3的上部具有物料入口； 其顶部具有燃气出 口， 燃气出口连接燃气管道； 其底部具有循环出口； 循环出口外具有通向回 收物暂存装置 21的第二输送装置如螺旋输送机。
热交换装置 5 包括燃气入口、 燃气出口及空气入口、 空气出口； 燃气入 口和燃气出口分别连接燃气管道； 空气入口和空气出口分别连接空气管道。
第二分离装置如旋风分离器 3的燃气出口设有水封阀 12 , 水封阀 12位 于热交换装置 5之前。 水封阀 12上设有一个放散口， 该放散口连接放散管道 111 , 放散管道 111的出口端设有点火装置 112。 风送装置如鼓风机 4通过空气管道连接于热交换装置 5的空气入口， 热 交换装置 5的空气出口连接于流化床 1底部的气化介质入口， 将空气从流化 床 1的底部吹入。 如图 2及图 3所示， 流化床 1的底部置有多个通风管道， 通风管道的进风口与流化床 1的空气入口相通， 通风管道的出风口上罩有斗 笠形的风帽， 风帽上置有多个小孔。
气化介质供给系统， 包括风送装置如鼓风机、 空气管道、 空气入口等。 本发明的工作过程如下：
生物质颗粒从料仓 8经水平输送带 91及大倾角输送带 92进入緩沖仓 61 , 经緩沖仓 61进入工作仓 62 , 然后经螺旋输送机 7进入流化床 1。 鼓风机 4向 流化床 1中送风。 在流化床 1中生物质颗粒与空气作用生成 C0、 H2和 CH4等 燃气和固体废弃物。 固体废弃物经废弃物管道 101及螺旋输送机 102进入废 弃物存储装置 103。
燃气和未完全反应的生物质颗粒进入旋风分离器 2 , 经分离后燃气和较 轻的生物质颗粒进入旋风分离器 3 , 较重的生物质颗粒通过螺旋输送机返回 流化床 1继续参加反应。
在旋风分离器 3 内， 燃气和较轻的生物质颗粒进一步分离， 燃气进入燃 气管道， 通过热交换装置 5加热用于反应的空气， 同时燃气被冷却， 被冷却 的燃气送至生物质气化反应系统的下游装置。 多余的燃气进入放散管道 111 , 在放散管道 11 1的端部点燃。 如图 4所示， 本发明所采用的气幕进料装置的具体实施方式包括： 电机、 减速装置、 旋转轴、 螺旋叶片、 进料管、 密封罩 71、 风送装置如鼓风机 72。
其中， 电机连接减速装置， 二者驱动旋转轴旋转， 旋转轴上固定套接有 螺旋叶片， 螺旋叶片之外套有进料管， 进料管上设有进料口和出料口。 进料 管的进料口位于炉前储料装置的出料口下方进料管的出料口连接于流化床气 化反应器的进料口； 进料管的进料口和出料口之间具有气孔区， 气孔区位于 进料管的进料口与出料口之间距离的 1 / 3处， 且远离出料口。 气孔区内具有 一排共 8个气孔 73 , 该 8个气孔 73沿进料管周向排布， 其分布轨迹为一个 圓。 进料管气孔区之外套有密封罩 71 , 密封罩 71 与进料管的结合部密封， 密封罩 71上具有一进风口。 进风口连接风送装置如鼓风机 72。 请参阅图 5 , 本发明的一生物质炉前储料装置具体实施方式包括緩沖仓 61和工作仓 62 , 其中， 緩沖仓设有进料口 63 , 工作仓的底部设有出料口 64 , 緩沖仓 61设置在工作仓 62上方， 緩沖仓 61与工作仓 62之间通过滚筒阀 65 连接相通， 并且在工作仓底部的出料口 64设置旋转阀 66 , 选择旋转阀 66作 为该处的阀门可以更好地与下方的送料装置实现衔接过度。 当工作仓向流化 床气化反应器中供料时， 则工作仓出料口的旋转阀处于打开状态， 而緩沖仓 与工作仓之间的滚筒阀处于闭合状态， 而当緩沖仓向工作仓加料时， 则工作 仓出料口的旋转阀处于关闭状态， 而緩沖仓与工作仓之间的滚筒阀处于打开 状态。
请参阅图 6 , 本发明的一生物质气化炉密闭排渣装置 102 的具体实施方 式包括转轴 71和筒体 72 , 转轴 71安装在筒体 72内， 转轴 71上套设有螺旋 叶片 73 , 筒体 72的一端设有进渣口 74 , 另一端设有出渣口 75 , 转轴 71上 的螺旋叶片 73分为两部分，该两部分的螺旋叶片旋向相反并分别设置在出渣 口 75的两侧， 在进渣口 74和出渣口 75处分别设有旋转阀 （图中未示出）， 筒体 72倾斜设置， 其出渣口 75高于进渣口 74 , 筒体 72的进渣口 74与生物 质气化炉（如流化床）底部的废弃物出口连接相通， 出渣口 75与水箱 103连 接相通。 转轴 71其中一段的直径略大于其他部分的直径， 该直径略大的转轴 部分位于进渣口 74与出渣口 75之间、 靠近出渣口 75的一侧。 如图 7所示， 其为本发明锁风进料装置的第一实施例， 包括： 电机、 减 速装置、 旋转轴、 螺旋叶片、 进料管。 其中， 电机连接减速装置， 二者驱动 旋转轴旋转， 旋转轴上固定套接有螺旋叶片， 螺旋叶片之外套有进料管， 进 料管上设有进料口和出料口， 旋转轴的终端和进料管的出料口平齐。 进料管 的进料口位于炉前储料装置的出料口下方进料管的出料口连接于流化床气化 反应器的进料口； 进料管的进料口和出料口之间的旋转轴上有一段粗于其它 部分， 该粗于其它部分的一段旋转轴其长度为螺旋叶片的一个螺距（如图 Ί 中 a所示）。 图 8所示为本发明锁风进料装置的第二实施例， 其与第一实施例的区别 在于： 旋转轴的直径不变， 但进料管的进料口和出料口之间的螺旋叶片上有 一段螺距小于其它部分（如图 8中 b所示；)。 图 9所示为本发明锁风进料装置的第三实施例， 其与第一实施例的区别 在于： 旋转轴的直径不变， 但旋转轴的终端未到达进料管的出料口， 旋转轴 的终端和进料管的出料口之间有一定距离 （如图 9中 c所示）。 图 10和图 11是本发明一实施方式的并联气化系统的示意图， 该实施方 式包括两个流化床气化反应器、 每个流化床气化反应器包括一套两级分离装 置、 每个流化床气化反应器包括其单独的气化介质供给系统。

Claims

权 利 要 求
1、 一种生物质气化装置， 其包括：
用于制备生物质燃气的流化床气化反应器； 设置于所述流化床气化反应器之外、 并对所述流化床气化反应器之反应 产物进行分离的两级以上的分离装置， 该两级以上的分离装置至少包括第一 分离装置和第二分离装置； 以及
2、 如权利要求 1所述的生物质气化装置， 其中：
所述的流化床气化反应器包括设置于其中部区域的第一进料口和第二进 料口、 设置于其底部的气化介质入口和废弃物出口、 以及设置于其上部区域 的物料出口； 其中， 所述流化床气化反应器的第一进料口与所述生物质原料 供给系统相接合， 所述流化床气化反应器的气化介质入口与所述的气化介质 供给系统相接合；
所述的第一分离装置包括设置于其上部区域的物料入口、 设置于其中部 区域的物料出口以及设置于其底部的循环出口； 其中， 所述第一分离装置的 物料入口与所述流化床气化反应器的物料出口相接合， 所述第一分离装置的 循环出口通过第一输送装置与所述流化床气化反应器的第二进料口相接合； 以及
所述的第二分离装置包括设置于其顶部的燃气出口、 设置于其上部区域 的物料入口、 设置于其底部的循环出口； 其中， 所述第二分离装置的物料入 口与所述第一分离装置的物料出口相接合， 所述第二分离装置的循环出口通 过第二输送装置和第一输送装置与所述流化床气化反应器的第二进料口相接 合。
3、 如权利要求 2所述的生物质气化装置， 其中， 所述的生物质气化装 置进一步包括热交换装置， 其中， 来自所述第二分离装置燃气出口的燃气和 来自所述气化介质供给系统的气化介质流经该热交换装置， 并发生热交换， 气化介质被预热， 燃气被冷却； 之后， 被预热的气化介质则经由所述流化床 气化反应器的气化介质入口， 送入所述流化床气化反应器， 被冷却的燃气则 送至所述生物质气化反应系统的下游装置。
4、 如权利要求 2所述的生物质气化装置， 其中， 所述的生物质原料供 给系统包括炉前储料装置和炉前送料装置； 其中， 所述炉前储料装置包括緩 沖仓和工作仓， 緩沖仓设有进料口， 工作仓的底部设有出料口， 緩沖仓设置 在工作仓上方， 緩沖仓与工作仓之间通过一锁气装置连接相通； 所述炉前送 料装置将来自所述工作仓出料口的原料送入所述流化床气化反应器的第一进 料口。
5、 如权利要求 1所述的生物质气化装置， 其中， 所述的生物质气化装 置进一步包括料仓及送料装置， 所述料仓包括顶部进料口和底部出料口； 所 述送料装置包括水平输送带和大倾角输送带， 所述水平输送带位于所述料仓 的底部出料口下方， 所述大倾角输送带的起始端与所述水平输送带末端相接 合， 所述大倾角输送带的末端位于所述緩沖仓的顶部进料口上方。
6、 如权利要求 1所述的生物质气化装置， 其中， 所述的生物质气化装 置进一步包括密闭排渣装置， 该密闭排渣装置其包括转轴和筒体， 其中， 转 轴安装在筒体内， 转轴上套设有螺旋叶片， 筒体的一端设有进渣口， 另一端 设有出渣口， 筒体倾斜设置， 其出渣口高于进渣口， 筒体的进渣口与生物质 气化炉底部的废弃物出口连接相通。
7、 如权利要求 6所述的生物质气化装置， 其中， 所述转轴上的螺旋叶片 分为两部分，该两部分的螺旋叶片旋向相反并分别设置在所述出渣口的两侧。
8、 如权利要求 6所述的生物质气化装置， 其中， 所述生物质气化炉密闭 排渣装置还包括一水箱， 所述出渣口与该水箱连接相通。
9、 如权利要求 6所述的生物质气化装置， 其中， 所述转轴其中一段的直 径略大于其他部分的直径； 所述直径略大的转轴部分位于所述进渣口与出渣 口之间、 靠近出渣口的一侧。
10、 如权利要求 1所述的生物质气化装置， 其中， 所述第二分离装置的 燃气出口设置有水封阀。
11、 如权利要求 1所述的生物质气化装置， 其中， 所述的生物质气化装 置进一步包括气幕进料装置， 该气幕进料装置包括驱动装置， 驱动装置驱动 连接旋转轴， 所述旋转轴上套接有螺旋叶片， 所述螺旋叶片的外围套设进料 管， 所述进料管具有进料口和出料口， 所述进料口与出料口之间设置具有多 个气孔的气孔区， 在所述进料管的气孔区之外套有密封罩， 所述密封罩具有 进风口， 所述进风口与风送装置的出风口连通。
12、 如权利要求 1所述的生物质气化装置， 其中， 所述的生物质气化装 置进一步包括锁风进料装置， 该锁风进料装置包括驱动装置， 该驱动装置驱 动连接旋转轴， 所述旋转轴上套接有螺旋叶片， 所述螺旋叶片的外围套设进 料管， 所述进料管具有进料口和出料口； 其中， 该锁风进料装置还包括位于 所述进料管的进料口和出料口之间的至少一处的锁风结构； 该锁风结构能够 使得所述进料管中的某处生物质原料的密度高于相邻的生物质原料密度， 从 而形成相对气密的结构。
1 3、 如权利要求 12所述的生物质气化装置， 其中， 所述的锁风结构是由 较粗的一段旋转轴形成的， 该较粗的一段旋转轴比与之相邻的旋转轴更粗。
14、 如权利要求 12所述的生物质气化装置， 其中， 所述锁风结构为所述 进料管的进料口和出料口之间的螺旋叶片上有一段螺距小于其它部分。
15、 一种生物质气化并联反应系统， 其包括：
两个或两个以上的、 并行设置的用于制备生物质燃气的流化床气化反应 哭'
两套或两套以上的、 分别设置于每个流化床气化反应器之外并对该流化 床气化反应器之反应产物进行分离的两级以上的分离装置， 每套分离装置至 少包括第一分离装置和第二分离装置；
16、 如权利要求 15所述的生物质气化并联反应系统， 其特征在于， 每个 所述的流化床气化反应器包括设置于其中部区域的第一进料口和第二进料 口、 设置于其底部的气化介质入口和废弃物出口、 以及设置于其上部区域的 物料出口； 其中， 所述流化床气化反应器的第一进料口与所述生物质原料供 给系统相接合， 所述流化床气化反应器的气化介质入口与所述的气化介质供 给系统相接合；
每个所述的第一分离装置包括设置于其上部区域的物料入口、 设置于其 中部区域的物料出口以及设置于其底部的循环出口； 其中， 所述第一分离装 置的物料入口与所述流化床气化反应器的物料出口相接合， 所述第一分离装 置的循环出口通过第一输送装置与所述流化床气化反应器的第二进料口相接 合； 以及
每个所述的第二分离装置包括设置于其顶部的燃气出口、 设置于其上部 区域的物料入口、 设置于其底部的循环出口； 其中， 所述第二分离装置的物 料入口与所述第一分离装置的物料出口相接合， 所述第二分离装置的循环出 口通过第二输送装置和第一输送装置与所述流化床气化反应器的第二进料口 相接合。
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