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WO2012059016A1 - Procédé de gazéification de biomasse - Google Patents

Procédé de gazéification de biomasse Download PDF

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Publication number
WO2012059016A1
WO2012059016A1 PCT/CN2011/081378 CN2011081378W WO2012059016A1 WO 2012059016 A1 WO2012059016 A1 WO 2012059016A1 CN 2011081378 W CN2011081378 W CN 2011081378W WO 2012059016 A1 WO2012059016 A1 WO 2012059016A1
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WO
WIPO (PCT)
Prior art keywords
gas
gasification
temporary storage
fluidized bed
biomass
Prior art date
Legal status (The legal status 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 status listed.)
Ceased
Application number
PCT/CN2011/081378
Other languages
English (en)
Chinese (zh)
Inventor
常厚春
马革
赵广健
陈平
覃勇付
陈燕芳
刘安庆
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Guangzhou Devotion Thermal Technology Co Ltd
Original Assignee
Guangzhou Devotion Thermal Technology Co Ltd
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 claimed from CN2010105281342A external-priority patent/CN101967397A/zh
Priority claimed from CN2010105282167A external-priority patent/CN101967399A/zh
Application filed by Guangzhou Devotion Thermal Technology Co Ltd filed Critical Guangzhou Devotion Thermal Technology Co Ltd
Publication of WO2012059016A1 publication Critical patent/WO2012059016A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • 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
    • 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
    • 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

Definitions

  • the present invention relates to a process for utilizing biomass energy, and more particularly to a biomass gasification process. Background technique
  • 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 1 / 10 of medium-sized bituminous coal. At the same time, its energy utilization can achieve zero emission of greenhouse gas C02.
  • 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. Thereby obtaining a high quality product gas.
  • biomass gasification mainly includes gasification reaction, synthesis gas catalytic conversion and gas separation purification process (direct separation without purification). Taking air as the gasification medium, the general formula of biomass gasification chemical reaction can be expressed as:
  • biomass is composed of cellulose, hemicellulose, The composition of lignin, inert ash, etc., high oxygen content and volatile matter, and strong activation of coke, so 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.
  • fixed bed gasifier It can also be divided into a top suction fixed bed gasifier, a down suction fixed bed gasifier, a horizontal suction fixed bed gasifier, and a happy fixed bed gasifier;
  • the fluidized bed gasifier can be divided into It is a fluidized bed gasifier, a dual fluidized bed gasifier, and a circulating fluidized bed gasifier.
  • 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. Among them, in the pre-gasification stage, the biomass material is subjected to pyrolysis gasification by a circulating fluidized bed gasification process, and in 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 forms of biomass materials such as granules and blocks, but its disadvantages are also obvious: The gasifier has a complex structure and is not suitable for large-scale gas production.
  • Cicle 1098911C discloses a biomass circulating fluidized bed gasification purification system which uses 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 process for improving gasification efficiency and gas heat generation, reducing generation of impurities such as tar and dust, reducing secondary pollution, and improving the silo. safety.
  • the present invention provides a multi-stage circulating gasification process for preparing gas using biomass feedstock, which comprises the following steps:
  • the second light stream when the third separating device is not used, the second light stream directly enters the gas pipeline; when the third separating device is included or adopted, the second light stream enters the third separating device and is separated in the third separating device, Separating into a lighter third light stream and a heavier third stream, the resulting third stream is returned to the fluidized bed reactor for further reaction, and the resulting third light stream enters the fourth separation unit or directly enters the gas.
  • Pipeline if more stages of separation are used, and so on.
  • the first, second, and third heavy streams are mainly raw Material feedstock and incompletely reacted biomass feedstock, such as solid biomass feedstock and incompletely reacted biomass feedstock;
  • the first light stream includes gas, incompletely reacted biomass feedstock, and biomass feedstock.
  • the second light stream should be primarily gas, otherwise it will enter the third separation unit for separation.
  • the third light logistics should be mainly gas, otherwise it will enter the fourth separation device for separation. And so on.
  • the first, second and third separating devices are all cyclonic separating devices.
  • 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 A gasification medium that regulates various components in the air.
  • the contents of oxygen, nitrogen, water vapor, and carbon dioxide can be appropriately increased or decreased to control conversion rate and production.
  • the rate and composition of the product such as gas.
  • the gas produced by the biomass gasification reaction is usually wrapped with biomass raw materials such as biomass fine particles or powder.
  • biomass raw materials such as biomass fine particles or powder.
  • the multi-stage circulating gasification process of the present invention will be from a fluidized bed gas.
  • the material obtained from the material outlet of the reactor is subjected to multiple separations to reduce the biomass feedstock component in the gas.
  • the separation is two times, that is, the material including the gas and the biomass raw material is sequentially introduced into two separation devices for two separations, and the separated biomass raw materials in each separation are returned to the fluidized bed gasification reactor to continue to participate in the reaction.
  • the apparatus used for the above multiple separations may be a cyclone or other separation apparatus.
  • the multistage cycle gasification process of the present invention further includes the step of heating the gasification medium, that is, the gasification medium participating in the reaction is heated before entering the fluidized bed gasification reactor for reaction.
  • heating the gasification medium requires a certain amount of heat; on the other hand, the gas generated after the gasification reaction is extremely high in temperature, and it is easy to destroy the related combustion equipment and the conveying pipeline by directly using it for combustion. Therefore, the step of heating the gasification medium may specifically be heat exchange between the gasification medium and the gas generated by the reaction. In this way, the gasification medium participating in the reaction is heated, the reaction speed is increased, the gas temperature is lowered, and the related combustion equipment and the conveying pipeline are protected.
  • the above step of heating the gasification medium can be specifically carried out by a heat exchange device.
  • the gas and gasification medium generated by the gasification reaction flows through the heat exchange device, and heat exchange occurs, the gasification medium is preheated, and the gas is cooled; then, the preheated gasification medium is passed through the fluidized bed gasification reactor
  • the gasification medium inlet is sent to the fluidized bed gasification reactor, and the cooled 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 multistage cycle gasification process of the present invention also includes the step of releasing excess gas.
  • the step of dissipating excess gas is specifically to burn excess gas. It specifically includes the following steps:
  • the ignition device ignites and ignites the gas in the discharge pipe.
  • the above-mentioned discharge pipe and ignition device constitute a dispersing device, and the excess gas is burned by the dispersing device, thereby avoiding an explosion accident that may be caused by gas recirculation.
  • a valve is arranged on the gas pipeline, and the valve is located in the heat exchange Before the device.
  • the above valve may specifically be a water seal valve.
  • the water seal valve includes a water storage container, a cover, an inner cover, and a pull rod.
  • the bottom of the water storage container is provided with a through hole through which the gas pipe passes, the shape and size of the through hole are matched with the gas pipe passing through the through hole, and the contact portions of the two are welded.
  • the outer cover is placed on the upper part of the water container, and the contact portions of the two are welded.
  • the outer cover is provided with a gas outlet, and the top of the outer cover is provided with a through hole.
  • the free end of the gas conduit is located in the space enclosed by the water container and the outer casing and above the water surface in the water container.
  • the inner cover is placed on the free end of the gas pipe, and the inner cover is provided with a pull rod which protrudes from a through hole at the top of the outer cover.
  • the present invention provides a multi-stage interlocking furnace advancement process, that is, a temporary storage compartment of at least one layer arranged in the upper and lower rows before the fluidized bed gasification reactor (preferably Two or three layers), each of the temporary storage bins is provided with a feeding port at the top and a discharging port at the bottom, and the discharging port of each temporary storage bin and the feeding port of the next temporary storage bin A valve is arranged between the bottom of the discharge port of the bottom storage compartment, and a pre-furnace feeding device is arranged, wherein the first-stage temporary storage bin is located at the top; the process comprises the following steps:
  • the process of the present invention provides a multi-layer temporary storage compartment, a plurality of valves.
  • An extreme case of blocking the entry of reactive gases into the temporary storage compartment is to close all valves.
  • the biomass material in the temporary storage compartment cannot enter the pre-furnace feeding device.
  • the above steps are used, and when the valve of a certain temporary storage compartment is opened, the valve located in the upper storage compartment of the first layer is closed. This prevents all the temporary storage valves from opening at the same time, and allows the reaction gas to enter the temporary storage bins unimpeded, without reducing the reaction speed due to safety factors.
  • the valves of the remaining layers of the temporary storage compartment are closed. In this way, the opportunity for the reaction gas to enter the temporary storage bin is greatly reduced.
  • a working chamber can be set on the bottom layer, and multiple buffer chambers are arranged on the upper layer of the working chamber, and multiple buffer chambers of the layer are directly connected to the working chamber.
  • a multi-layer buffer tank can be arranged on the buffer tank of the layer, and the multi-layer buffer tank can be provided with a plurality of buffer bins per layer.
  • a preferred method is that the temporary storage bin has two layers, the upper layer is a buffer bin and the next layer is a work bin. There are multiple buffer bins and one working chamber. Each buffer bin is directly connected to the working chamber and has a valve. The valves are opened in sequence, and when one of the valves is opened, the remaining valves are closed.
  • the temporary storage bin has two layers, and each floor has a temporary storage bin; the upper layer is a buffer bin, and the lower layer is a work bin.
  • Valves suitable for implementing the present invention may be drum valves, ball valves, drum valves or other valves.
  • the pre-furnace feeding device can smoothly input the biomass raw material into the gasification furnace, and the pre-furnace feeding device is a spiral conveying device.
  • the invention separates the biomass raw materials in the gas, enables the biomass raw materials to fully react, improves the gasification efficiency, saves energy, generates more gas, and improves the calorific value of the gas. Because the biomass raw material reacts sufficiently, the generation of tar and dust is reduced, the safety hazard of tar and dust formed in the reaction device is avoided, and the environmental pollution problem caused by the treatment of tar and dust is reduced; meanwhile, the invention is set by Multi-layer temporary storage bins arranged up and down and valves are arranged between adjacent two-stage temporary storage bins, so that the valves of the respective layers are opened at different times, thereby realizing the prevention of the external feeding and preventing the reaction system such as the fluidized bed.
  • FIG. 1 is a flow chart of a multistage cycle gasification process of the present invention
  • FIG. 2 is a flow chart of an embodiment of a multi-stage interlocking furnace forward feed process of the present invention
  • FIG. 3 is a schematic view showing the structure of a biomass gasification reaction system to which the process of the present invention is applied. detailed description
  • the multi-stage circulation gasification process of the present invention comprises the following steps:
  • the gas and the gasification medium are heat exchanged by a heat exchange device
  • biomass feedstock enters from the feedstock inlet in the central portion of the fluidized bed gasification reactor, and the gasification medium enters from the air inlet at the bottom of the fluidized bed gasification reactor;
  • the gas pipeline is provided with a water seal valve
  • the water seal valve is located in front of the heat exchange device
  • the water seal valve is provided with a discharge port
  • the discharge port is connected to the discharge pipe
  • the outlet end of the discharge pipe is provided with an ignition Device.
  • the temporary storage bin has a plurality of layers, for example, three layers, and the first and the last are connected to the upper and lower rows. There is only one temporary storage bin per floor. Among them, the temporary storage warehouse at the bottom layer is the work warehouse, and the remaining temporary storage warehouses are buffer warehouses. Each of the temporary storage bins has a feed port at the top thereof and a discharge port at the bottom thereof, and a valve is provided at the bottom discharge port of each of the temporary storage bins. Below the discharge opening of the work compartment, there is a furnace feed device such as a screw conveyor. The valve is a drum valve, ball valve, drum valve or other valve. When one of the valves is open, the other valves are closed to achieve multi-stage shutoff of the gasification reaction gas. Specifically, the feeding steps are as follows:
  • the second embodiment differs from the first embodiment in that: the temporary storage bin has two layers, the upper layer is a buffer bin, and the lower layer is a work bin. The rest are the same and will not be described here.
  • the third embodiment is suitable for a continuous feed reaction system.
  • the temporary storage bin has two floors, the upper one is the buffer bin, and the lower one is the work bin. There is one working compartment on the bottom floor, and there are multiple buffer bins on the upper layer. Each buffer bin is directly connected to the work bin, and each buffer bin has a valve at the discharge port. When feeding, multiple valves are opened in sequence, and when one of the valves is opened, the remaining valves are closed.
  • Figure 3 shows a biomass gasification reaction system using the method of the present invention, comprising: 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
  • the air separator 3 the air delivery device such as the air blower 4, the heat exchange device 5, the buffer chamber 61, the work chamber 62, the pre-furnace feeding device such as the screw conveyor 7, the silo 8, the horizontal conveyor belt 91, the large dip belt 92,
  • the waste pipe 101, the slagging device such as the screw conveyor 102, the waste storage device 103, the discharge pipe 111, the ignition device 12, and the water seal valve 12.
  • 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 belt 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 front 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.
  • the waste outlet is connected to the waste pipeline 101, and the waste pipeline 101 is disposed at the outlet with a slagging device such as a screw conveyor 102.
  • 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 through 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 inlet and the gas outlet are respectively connected to the gas pipeline;
  • 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 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 arranged 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.
  • the air outlet of the ventilation duct is covered with a bucket-shaped hood, and the air cap is provided with a plurality of small holes.
  • 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 through 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 return 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.
  • a downstream device of the reaction system Excess gas enters the discharge pipe 1 11 and ignites at the end of the discharge pipe 1 11 .

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  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention porte sur un procédé de gazéification en plusieurs étapes pour le recyclage de biomasse, qui comprend : (1) l'introduction respectivement d'une matière première de type biomasse et d'un milieu de gazéification dans un réacteur de gazéification à lit fluidisé ; (2) la réaction de la matière première de type biomasse avec le milieu de gazéification dans le réacteur de gazéification à lit fluidisé pour produire du gaz combustible ; (3) l'introduction des produits réactionnels comprenant le gaz combustible et de la matière première de type biomasse provenant du réacteur de gazéification à lit fluidisé dans un premier appareil de séparation pour leur séparation en un premier flux de matière légère relativement léger et un premier flux de matière lourde relativement lourd ; (4) le recyclage du premier flux de matière lourde obtenu à partir du premier appareil de séparation vers le réacteur à lit fluidisé pour qu'il réagisse encore et l'introduction du premier flux de matière légère obtenu à partir du premier appareil de séparation dans un deuxième appareil de séparation ; (5) la séparation du premier flux de matière légère dans le deuxième appareil de séparation en un second flux de matière légère relativement léger et un second flux de matière lourde relativement lourd ; (6) le recyclage du second flux de matière lourde obtenu à partir du deuxième appareil de séparation vers le réacteur à lit fluidisé pour qu'il réagisse encore et l'introduction du second flux de matière légère obtenu à partir du deuxième appareil de séparation dans un troisième appareil de séparation ou directement dans une canalisation de gaz combustible. L'invention porte également sur un procédé d'alimentation de four par l'avant à emboitement en plusieurs étapes permettant d'améliorer la sécurité. La présente invention améliore le rendement de gazéification par la mise en œuvre d'une séparation en plusieurs étapes de matière première de type biomasse solide dans le gaz combustible afin que la matière première de type biomasse puisse réagir totalement et en même temps réduit la production de goudron et de poussière, en raison de la réaction totale de la matière de type biomasse.
PCT/CN2011/081378 2010-11-01 2011-10-27 Procédé de gazéification de biomasse Ceased WO2012059016A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
CN2010105281342A CN101967397A (zh) 2010-11-01 2010-11-01 采用多级密闭隔断的生物质气化反应炉前送料工艺
CN201010528216.7 2010-11-01
CN201010528134.2 2010-11-01
CN2010105282167A CN101967399A (zh) 2010-11-01 2010-11-01 生物质多级循环气化工艺

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WO2012059016A1 true WO2012059016A1 (fr) 2012-05-10

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Publication number Priority date Publication date Assignee Title
EP0223619A1 (fr) * 1985-09-09 1987-05-27 Framatome Dispositif de traitement de matières solides sous forme de particules, en lit fluidisé circuit circulant en particulier dispositif de gazéification
US4929255A (en) * 1987-08-28 1990-05-29 A. Ahlstrom Corporation Method for gasifying or combusting solid carbonaceous material
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WO2003029389A1 (fr) * 2001-10-02 2003-04-10 Valtion Teknillinen Tutkimuskeskus Procede et appareil pour la gazeification de combustible dans un reacteur a lit fluidise
CN201254554Y (zh) * 2008-07-18 2009-06-10 段先胜 具有自动进料装置的气化炉
CN101967399A (zh) * 2010-11-01 2011-02-09 广州迪森热能技术股份有限公司 生物质多级循环气化工艺

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EP0223619A1 (fr) * 1985-09-09 1987-05-27 Framatome Dispositif de traitement de matières solides sous forme de particules, en lit fluidisé circuit circulant en particulier dispositif de gazéification
US4929255A (en) * 1987-08-28 1990-05-29 A. Ahlstrom Corporation Method for gasifying or combusting solid carbonaceous material
CN1221777A (zh) * 1997-12-31 1999-07-07 中国科学院广州能源研究所 生物质氧气气化产生中热值可燃气体的方法及装置
WO2003029389A1 (fr) * 2001-10-02 2003-04-10 Valtion Teknillinen Tutkimuskeskus Procede et appareil pour la gazeification de combustible dans un reacteur a lit fluidise
CN201254554Y (zh) * 2008-07-18 2009-06-10 段先胜 具有自动进料装置的气化炉
CN101967399A (zh) * 2010-11-01 2011-02-09 广州迪森热能技术股份有限公司 生物质多级循环气化工艺

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