WO2011063579A1 - 带余热利用的生物质三段式气流床及其气化方法 - Google Patents

带余热利用的生物质三段式气流床及其气化方法 Download PDF

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WO2011063579A1
WO2011063579A1 PCT/CN2010/000021 CN2010000021W WO2011063579A1 WO 2011063579 A1 WO2011063579 A1 WO 2011063579A1 CN 2010000021 W CN2010000021 W CN 2010000021W WO 2011063579 A1 WO2011063579 A1 WO 2011063579A1
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heat exchanger
temperature
high temperature
bed
wall
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PCT/CN2010/000021
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English (en)
French (fr)
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韩剑锋
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中节环(北京)能源技术有限公司
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Publication of WO2011063579A1 publication Critical patent/WO2011063579A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/86—Other features combined with waste-heat boilers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/62—Processes with separate withdrawal of the distillation products
    • 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
    • C10J3/74—Construction of shells or jackets
    • C10J3/76—Water jackets; Steam boiler-jackets
    • 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/094—Char
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the three-stage gas flow bed gasification technology with waste heat utilization of the invention relates to the technical field of energy chemical industry; in particular to the field of thermochemical technology of biomass; in particular, the technical field of biomass gasification technology; The field of biomass gas flow bed gasification technology utilized. Background technique '
  • Plants in biomass are organic substances produced by the absorption of carbon dioxide in the air through photosynthesis. They are widely distributed, widely available, and are the only renewable natural raw materials that contain hydrocarbon components and heat. Substances for energy use and chemical production have the characteristics of zero CO 2 emissions. With the decreasing of traditional fossil energy reserves and the environmental pollution caused by the use of fossil energy, it has become the consensus of governments of all countries to attach importance to and develop renewable and environmentally friendly energy. Through thermochemical, biochemical and other methods, it can transform biomass into clean gas or liquid fuel, produce diesel/gasoline, chemical products and meet power demand, etc., with the potential to fully replace fossil energy, will become the world Priority for the development of new energy sources.
  • biomass gasification technology can adapt to all biomass species and has the capacity to industrialize large-scale production compared to other technologies.
  • the gasification process of biomass is a thermochemical process in which a biomass material reacts with a gasifying agent (air, oxygen, water vapor, carbon dioxide, etc.) at a high temperature.
  • a gasifying agent air, oxygen, water vapor, carbon dioxide, etc.
  • the composition of the syngas produced by the gasification process differs depending on the nature of the bioshield feedstock used in the gasification, the type of gasification agent, the conditions of the gasification process, and the structure of the gasifier.
  • the goal of gasification for the production of synthetic diesel/gasoline, chemical synthesis gas, ie refined synthesis gas, is to minimize the consumption of raw materials and oxidants (such as oxygen) and the methane content in the synthesis gas, and there is no tar production. At the same time, maximize the gasification efficiency, carbon conversion rate and the content of active ingredients (0) and ⁇ 1 2 in the synthesis gas.
  • the refined synthesis gas refers to: the composition of the synthesis gas obtained by vaporization of the gasification unit, CO and H 2 as the main component, no tar, CH 4 content ⁇ 0.5%.
  • Refined syngas is mainly used in the production of synthetic diesel/gasoline, olefins, alkanes, naphtha, lubricating oil, and as a fuel cell raw material, etc. It is suitable for the production of various chemical products and new energy utilization of various ultra-clean oil products.
  • biomass refining gasification technology is a key gasification technology with biomass chemical industry, biomass synthetic oil new energy industry and industrialized large-scale production capacity.
  • the synthesis gas produced by fixed bed gasification has a low calorific value and contains a large amount of tar; fluidized bed gasification is sensitive to the nature of the raw materials, the operating temperature is low, and the tar content in the outlet synthesis gas is relatively high. Since the fixed bed and the fluidized bed generally use air as the oxidant, and the gasification pressure is generally normal pressure, the synthesis gas contains a large amount of tar, and the tar cracking and purification device has to be installed in the subsequent equipment, so that the gasification process becomes Very complicated.
  • the core problem of the gasification method is that the average gasification temperature is lower than 1100 °C due to the lower average gasification temperature, which results in high tar content in the tar production and synthesis gas, which cannot meet the high-efficiency gasification of biomass. And the requirements for the production of refined syngas.
  • biomass gas flow bed gasification has strict limits on the particle size of raw materials, and the raw materials entering the gas flow bed need to be ground into ultrafine particles. Some crushing or milling techniques cannot grind the biomass containing more fiber into the particle size required for the operation of the entrained flow bed, which results in the inability to directly use the biomass feedstock for gasification of the entrained flow bed.
  • the temperature of the synthesis bed of the entrained gas bed is very high, generally above 1300 °C, and the application of syngas needs to be purified or changed. This requires the temperature of the syngas to be reduced to about 250, the residual heat of the syngas. If not fully utilized, it will result in inefficiency of the entire gasification system.
  • alkali metals U and Na in biomass feedstocks due to the high content of alkali metals U and Na in biomass feedstocks, they exist in gaseous form at high temperatures. During the cooling process of syngas, they will condense into solids at 800 X: ⁇ 600 C. On the wall surface of the heat exchanger tube, causing alkali metal corrosion and slagging of the tube on the heated surface and blocking the syngas passage.
  • biomass gas flow bed gasification technology in order to solve the problem, generally firstly pyrolyze biomass to obtain pyrolysis gas and solid carbon, and then send the pyrolysis gas and solid carbon powder into the gas stream bed.
  • Chemical. Biomass entrained bed technology has a liquid slagging method like pulverized coal gasification.
  • the syngas outlet temperature is generally controlled between 1300-1C and 1500, such as Chinese patents with application numbers 2006101245707 and 2006101245711, and Colin Company of Germany.
  • Carbon-V gasification technology, as well as the high-efficiency entrained gasification technology of biomass solid-state slagging for Chinese patent application No. 200910210433.
  • the present invention is based on the characteristics of biomass raw materials and the above-mentioned four major problems to be solved, and based on earnest and sufficient investigation, understanding, analysis, and summarization of the above-mentioned well-known technologies and current conditions, the gasification of the biomass gas flow bed is refined.
  • biomass with waste heat utilization requirements for waste heat utilization, control of carbon evolution reaction of synthetic gas, prevention of metal ash corrosion, control of alkali metal corrosion of biomass, prevention of alkali metal slagging and slag blocking of syngas channels, etc.
  • the three-stage entrained flow gasification technology is especially suitable for the purification of biomass and the utilization of waste heat of biomass synthesis gas. It not only solves the above four problems comprehensively, but also satisfies the biomass safely, efficiently, stably and with low investment. The requirements for refined gasification and syngas are of great importance. Summary of the invention
  • the present invention provides a "three-stage entrained flow gasification technology for biomass with waste heat" for the gas shielded gas bed and the main chemical reaction characteristics of the synthesis gas in different temperature ranges.
  • biomass is pyrolyzed to obtain solid carbon and pyrolysis gas, and the solid carbon is ground to obtain carbon powder.
  • the carbon powder is transported by pyrolysis gas/nitrogen/carbon dioxide gas, and oxygen is used as oxidant, carbon powder and heat.
  • the degassing and oxygen enter the gas flow bed through the burner for gasification reaction, and the high temperature synthesis gas is obtained.
  • the physical heat of the high temperature synthesis gas transfers heat to the water through the heat exchanger in the gasification furnace to generate superheated steam, and the high temperature synthesis gas is cooled. Flow out of the gasifier.
  • the invention has the following points: 1.
  • the airflow bed gasifier device with residual heat utilization is divided into three sections, namely a high temperature air flow bed, a high temperature heat exchanger and a low temperature heat exchanger; 2.
  • the high temperature air flow bed In the airflow bed gasification technology using solid waste slag, the inner wall of the high temperature gas flow bed is composed of a membrane type water wall coated with refractory material, and the synthesis gas outlet temperature of the high temperature air flow bed is 1280 ° C ⁇ 1320 ° Between C; 3, in the high temperature heat exchanger, the inlet temperature of the syngas is between 1280 ° C ⁇ 1320 ° C, the outlet temperature is between 580 ° C ⁇ 600 ° C; the high temperature heat exchanger
  • the inner wall of the furnace is composed of a light pipe membrane type water wall, and a chilling chamber and a high temperature superheater are arranged in the high temperature heat exchanger, and the temperature of the syngas entering the chilling chamber is between 1000 ° C and 1
  • the temperature of the syngas after chilling leaving the chilling chamber is between 700 ° C and 800 ° C. 4.
  • the inlet temperature of the syngas is between 580 ° C and 600 ° C.
  • the outlet temperature is between 220 ° C and 230 ° C;
  • the inner wall of the furnace of the low temperature heat exchanger is a light pipe film
  • Water wall constituting the cryogenic heat exchanger is arranged in the low temperature superheater And the economizer.
  • the gas flow bed gasification apparatus used in the three-stage entrained flow gasification technology with waste heat utilization of the present invention may be in any of the following three forms:
  • Device Form 1 The top of the high-temperature airflow bed of the three-stage airflow bed gasifier device with waste heat utilization is arranged with a down burner, the carbon powder, pyrolysis gas and oxygen passing through The down-type burner enters the high-temperature airflow bed for gasification reaction, and the synthesis gas descends in the high-temperature airflow bed, passes through the connecting channel formed by the inner wall of the optical tube membrane water-cooling wall, enters the high-temperature heat exchanger and is rectified by the rectification and shrinkage The connecting passage formed by the upward cooling and passing through the inner wall by the diaphragm film water-cooling wall enters the low-temperature heat exchanger and is rectified by the rectifier and then cooled downward.
  • Device Form 3 The lower part of the high-temperature airflow bed of the three-stage airflow bed gasifier device with waste heat utilization is arranged with a horizontal burner, the carbon powder, pyrolysis gas and oxygen gas passing through The horizontal burner enters the high-temperature airflow bed for gasification reaction, and the synthesis gas rises in the high-temperature airflow bed, passes through the rectification and shrinkage into the high-temperature heat exchanger, and is cooled upward, and then the inner wall is connected by the membrane-type water-cooling wall.
  • the channel 3 ⁇ 4 enters the low temperature heat exchanger and is rectified by the rectifier and then cooled down.
  • the inner wall of the three-stage air flow bed gasifier of the present invention has a cross section of a circular, square, octagonal, circular/square/octagonal combination.
  • the chilling chamber uses water as a chilling agent, and the residence time of the syngas in the chilling chamber is within 0.3 seconds, and the chilling water spraying method of the chilling chamber adopts a top-down fog.
  • One type of water spray, or atomized spray water from the bottom up, or a horizontal annular atomized spray water, and the high temperature superheater heating surface tube bundle is subjected to high pressure steam blowing or mechanical vibration to remove ash.
  • a rectification method is adopted at the syngas turn position, so that the syngas is uniformly distributed when the syngas enters the next step.
  • the whole gasification unit is divided into three sections of organic connection of "high temperature gas flow bed, high temperature heat exchanger and low temperature heat exchanger” to solve various technical problems in the process of biomass gasification and waste heat utilization, which constitutes "with waste heat”
  • the use of an entrained flow gasifier device "new equipment, providing an efficient carrier for biomass gasification and synthesis gas waste heat utilization;
  • the temperature of the synthesis gas outlet of the high-temperature airflow bed is controlled between "1280 °C ⁇ 1320; the synthesis gas outlet temperature of the high temperature heat exchanger is controlled between 580 °C ⁇ 600 °C, wherein the synthesis gas chilling temperature range is from 1000 ° C ⁇ 1100 ° C chilling to 700 ° C ⁇ 800 ° C ;
  • the synthesis gas outlet temperature of the low temperature heat exchanger is controlled between 220 ° C ⁇ 230 ° C, It constitutes a technical problem that can solve the technical problems in the temperature range of each stage of biomass high-temperature gas flow bed gasification and waste heat utilization, and provides high-temperature gas flow bed gasification and control carbon deposition reaction, metal ash corrosion, alkali metal corrosion Technical conditions;
  • the synthesis gas temperature is between 580 ° C and 600 ° C, and the high temperature heat exchanger and the low temperature heat exchanger are separated in different syngas passages, in order to solve the problem that the alkali metal slag slag blocks the syngas passage
  • the problem provides the conditions for implementation;
  • a biomass three-stage entrained flow gasification technology with waste heat utilization using biomass as raw material, raw materials obtained by pyrolysis to obtain solid carbon and pyrolysis gas, solid carbon is ground to obtain carbon powder, and carbon powder is pyrolyzed / Nitrogen / carbon dioxide gas transport, while using oxygen as oxidant, carbon powder, pyrolysis gas and oxygen through the burner into the gas flow bed for gasification
  • the high temperature synthesis gas is obtained by the reaction, and the physical heat of the high temperature synthesis gas is transferred to the water through the heat exchanger in the gasification furnace to generate superheated steam, and the high temperature synthesis gas is cooled and then flows out of the gasification furnace;
  • the invention points and implementation points are mainly embodied in :
  • the airflow bed gasifier device with residual heat utilization is divided into three sections, which are a high temperature gas flow bed, a high temperature heat exchanger, and a low temperature heat exchanger;
  • an entrained-flow gasification technique using solid-state slagging wherein the inner wall of the high-temperature entrained bed is composed of a membrane-type water-cooled wall coated with a refractory material, and the syngas outlet of the high-temperature entrained bed
  • the temperature is between 1280 ° C ⁇ 1320 ° C;
  • the inlet temperature of the syngas is between 1280 ° C and 1320 ° C, and the outlet temperature is between 580 ° C and 600 ° C;
  • the inner wall of the furnace of the high temperature heat exchanger is a light pipe membrane type water wall, wherein the high temperature heat exchanger is arranged with a chilling chamber and a high temperature superheater, and the temperature of the syngas entering the chilling chamber is between 1000 ° C and 1100 ° C, leaving the stimuli
  • the temperature of the syngas after chilling in the cold room is between 700 ° C and 800 ° C;
  • the inlet temperature of the syngas is between 580 ° C ⁇ 600 ° C, the outlet temperature is between 220 ° C ⁇ 230 ° C;
  • the inner wall of the furnace of the low temperature heat exchanger is adopted A light pipe membrane type water wall is disposed, and a low temperature superheater and an economizer are disposed in the low temperature heat exchanger.
  • the three-stage entrained flow gasifier apparatus with waste heat utilization of the present invention can be in any of the following three forms:
  • Device form 1 the biomass three-stage entrained flow gasification technology with waste heat utilization, the top cloth of the high temperature air flow bed of the three-stage air flow bed gasification device Provided with a down burner, the carbon powder, pyrolysis gas and oxygen enter the high temperature gas flow bed through the down burner for gasification reaction, the synthesis gas descends in the high temperature gas flow bed, passes through the inner wall by the light pipe membrane type
  • the connecting passage formed by the water-cooling wall enters the high-temperature heat exchanger and is rectified by the rectifying and shrinking, and then cooled upward, and then connected to the low-temperature heat exchanger through the connecting passage formed by the optical tube membrane water-cooling wall on the inner wall, and is cooled by the rectifier and then cooled downward.
  • Device form 2 the biomass three-stage entrained flow gasification technology with waste heat utilization, the top of the high temperature gas flow bed of the three-stage air flow bed gasification device is arranged with a down burner,
  • the carbon powder, pyrolysis gas and oxygen enter the high-temperature gas flow bed through the down burner for gasification reaction, and the synthesis gas descends in the high-temperature gas flow bed, passes through the rectification and shrinkage into the high-temperature heat exchanger, descends and then passes through the inner wall.
  • the connecting channel formed by the light pipe membrane type water-cooling wall enters the low-temperature heat exchanger and is rectified by the rectifying and shrinking, and then cooled upward.
  • Device form 3 the biomass three-stage flow-bed gasification technology with waste heat utilization, the lower part of the high-temperature air flow bed of the three-stage air flow bed gasification device is arranged with a horizontal burner, The carbon powder, the pyrolysis gas and the oxygen enter the high-temperature airflow bed through the horizontal burner for gasification reaction, and the synthesis gas rises in the high-temperature airflow bed, passes through the rectification and shrinkage into the high-temperature heat exchanger, and is cooled upward, and then passes through the inner wall.
  • the connecting channel formed by the light pipe membrane water wall enters the low temperature heat exchanger and is rectified by the rectifier and then cooled downward.
  • the biomass three-stage entrained flow gasification technology with waste heat utilization wherein the inner wall of the three-stage entrained flow gasifier device has a circular, square, octagonal cross section.
  • the inner wall of the three-stage entrained flow gasifier device has a circular, square, octagonal cross section.
  • the biomass three-stage flow-bed gasification technology with waste heat utilization in the high-temperature heat exchanger, the chilling water spray mode of the chilling chamber adopts a top-down atomized water spray, or from the bottom
  • One of the upward atomization spray water or the horizontal annular atomization spray water, and the high temperature superheater heating surface tube bundle is subjected to high pressure steam blowing or mechanical vibration to remove the ash.
  • the biomass three-stage entrained flow gasification technology with waste heat utilization wherein the three-stage entrained flow gasification furnace device adopts a rectification method at the syngas turn position, so that the syngas is maintained when entering the next step.
  • the airflow is evenly distributed.
  • the technical solution provided by the present invention is adopted. Since the invention adopts the "solid-state slagging flow-bed gasification technology" and the “synthesis gas-separated temperature interval waste heat utilization technology", the "three-stage gas flow bed gasification technology with waste heat utilization” is constructed.
  • the raw material is pyrolyzed to obtain solid carbon and pyrolysis gas, and the solid carbon is ground to obtain carbon powder, which is transported by pyrolysis gas/nitrogen/carbon dioxide gas, and oxygen is used as an oxidant, carbon.
  • the powder, pyrolysis gas and oxygen enter the gas flow bed through the burner for gasification reaction to obtain high temperature synthesis gas.
  • the physical heat of the high temperature synthesis gas transfers heat to the water through the heat exchanger in the gasification furnace to generate superheated steam, high temperature synthesis gas.
  • the invention adopts an entrained flow gasifier device with waste heat utilization, it is divided into three sections, namely a high temperature gas flow bed, a high temperature heat exchanger, and a low temperature exchange.
  • the high-temperature entrained bed the entrained-flow gasification technology of solid-state slagging is adopted, and the inner wall of the high-temperature entrained bed is composed of a membrane-type water-cooled wall coated with refractory material, and the syngas outlet temperature of the high-temperature entrained bed is 1280 °C.
  • the inlet temperature of the syngas is between 1280 ° C ⁇ 1320 ° C, the outlet temperature is between 580 ° C ⁇ 600 ° C;
  • the inner wall of the high temperature heat exchanger The utility model comprises a light pipe membrane type water wall, wherein a chilling chamber and a high temperature superheater are arranged in the high temperature heat exchanger, and a syngas temperature entering the chilling chamber is between 1000 ° C and 1100 ° C, leaving the chilling
  • the temperature of the syngas after chilling is between 700 °C and 800 °C.
  • the inlet temperature of the syngas is between 580 °C and 600 °C, and the outlet temperature is between 220 °C and 230.
  • the inner wall of the low-temperature heat exchanger is composed of a light pipe membrane type water-cooled wall, and a low-temperature superheater and an economizer are arranged in the low-temperature heat exchanger.
  • the invention divides the whole entrained flow gasifier device into three-stage organic connection of "high temperature gas flow bed, high temperature heat exchanger and low temperature heat exchanger", which is various technical problems in the process of biomass gasification and waste heat utilization.
  • Solution provides the basis and direction of the composition
  • the new equipment of the "Entrained Flow Gasifier with Waste Heat” provides the beneficial effects of the implementation of the biomass efficient gasification and synthesis gas waste heat utilization.
  • the inner wall of the high temperature gas flow bed furnace is coated with refractory material.
  • the composition of the membrane-type water-cooled wall is obtained, the gasification efficiency of the gas flow bed is more than 80%, the carbon conversion rate of the gas flow bed is more than 99.8%, the gasification product is tar-free, (3 ⁇ 4 content is less than 0.4%, synthesis) Gas CO And the dry-based component of 3 ⁇ 4 achieves the beneficial effect of more than 87% of refined syngas.
  • the synthesis gas exiting the high temperature gas flow bed of the present invention enters the high temperature heat exchanger, the synthesis gas outlet temperature of the high temperature heat exchanger is controlled between 580 ° C and 600 ° C, and then enters the low temperature heat exchanger, and the synthesis gas is at 220.
  • the gas flow bed gasifier device is discharged between °C and 230 °C, and the high temperature gas flow bed, the high temperature heat exchanger and the low temperature heat exchanger are all arranged with working fluid.
  • the syngas is chilled from 1000 ° C to 1100 ° C to 700 ° C to 800 ° C, and the synthesis gas stays in the chill chamber.
  • the time is within 0.3 seconds, which is the most intense interval of the synthesis gas carbonization reaction.
  • the synthesis gas passes through the temperature range by rapid chilling, which greatly reduces the carbon evolution reaction of the synthesis gas and controls the precipitation of carbon black.
  • the carbon conversion efficiency of the entrained flow gasifier device is improved, and the occurrence of metal ashing corrosion caused by the reaction of the carbon black with the heated surface pipe is controlled.
  • the syngas is chilled and then enters the high temperature superheater, the temperature of the syngas is between 800 ° C and 600 ° C, and the gaseous alkali metal in the syngas is solidified, and It is easy to adhere to the heating surface tube and slag.
  • the heated surface tube bundle is deashed by high pressure steam purging or mechanical rapping in the high temperature superheater, and at the same time, the invention adopts Three-stage airflow bed gasifier, high temperature heat exchanger and low temperature heat exchanger in two different In the channel, the slag generated by the soot blowing in the high temperature heat exchanger is directly discharged from the discharge port, and does not fall into the heating surface tube of the low temperature heat exchanger to block the synthesis gas passage.
  • the three-stage entrained flow gasifier apparatus of the present invention can be used in three different types of devices, respectively: 1.
  • a three-stage flow-bed gasification furnace device is arranged with a down burner at the top of the high-temperature gas flow bed.
  • the carbon powder, pyrolysis gas and oxygen enter the high-temperature gas flow bed through the down burner for gasification reaction, and the synthesis gas descends in the high-temperature gas flow bed, and enters the high-temperature heat exchange through the connecting channel formed by the inner wall of the membrane-type water-cooling wall.
  • the connecting channel which is rectified by the rectifying and shrinking, is cooled upward, and then passes through the inner wall by the diaphragm film water-cooling wall, enters the low-temperature heat exchanger and is rectified by the rectifier and then cooled downward.
  • the three-stage flow-bed gasification furnace device is arranged with a down burner at the top of the high-temperature gas flow bed, through which the carbon powder, pyrolysis gas and oxygen enter the high-temperature gas flow bed for gasification reaction, syngas Downstream in the high-temperature airflow bed, through the rectification and shrinkage into the high-temperature heat exchanger, down-cooling, and then through the inner wall, the connecting channel formed by the optical tube membrane water-cooling wall enters the low-temperature heat exchanger and is rectified by the rectifying and shrinking, and then cooled upward.
  • the lower part of the high-temperature gas flow bed of the three-stage flow-bed gasification furnace device is arranged with a horizontal burner, and the carbon powder, pyrolysis gas and oxygen enter the high-temperature gas flow bed through the horizontal burner for gasification reaction, syngas
  • the cooling channel is cooled by the rectification and shrinkage into the high-temperature heat exchanger, and then the connecting channel formed by the optical tube membrane water-cooling wall of the inner wall enters the low-temperature heat exchanger and is rectified by the rectifier and then cooled downward.
  • the inner wall of the furnace of the three-stage air flow bed gasification device of the present invention has a circular, square, octagonal, circular/square/octagonal cross-section, thereby obtaining a high-temperature airflow.
  • the different layout requirements of the three sections of the bed, the high temperature heat exchanger and the low temperature heat exchanger, and the requirements for the gasification combustion in the high temperature gas flow bed, the arrangement form of the heat surface tube bundle of the high temperature/low temperature heat exchanger, the circular section, The square section, the octagonal section, and the combination of circular, octagonal and square sections between the sections realize the simple structure of the heating surface tube bundle of the gasifier, easy to arrange, compact space, convenient material selection and simple installation. , to maximize the benefits of materials and other benefits.
  • the present invention is arranged with a down burner at the top of the high temperature gas flow bed in the three-stage flow-bed gasification furnace unit form one/two, in the third three-stage air flow bed gasification furnace device form
  • the lower part of the high-temperature airflow bed is arranged with a horizontal burner, and the carbon powder, pyrolysis gas and oxygen enter the high-temperature airflow bed through the burner for gasification reaction, and can respectively provide the gasification combustion required for the biomass solid waste slag flow bed.
  • the implementation conditions of the method realize the efficiency of the high efficiency entrained flow gasification reaction of biomass.
  • the chilling water spraying method of the chilling chamber according to the present invention adopts one of a top-down atomized water spray, or a bottom-up atomized water spray, or a horizontal annular atomized spray water, thereby obtaining According to the specific flow direction (upstream or downward) of the syngas and the specific structural arrangement requirements of the entrained flow gasifier device, one of the above three spray water atomization chilling methods can be selected, and the chilling chamber can be realized.
  • the synthesis gas can be chilled from 1000 ° C to 1100 ° C to between 700 ° C and 800 ° C in 0.3 seconds, which greatly reduces the carbon evolution reaction of the synthesis gas, and controls the metal ash corrosion and Improve carbon conversion efficiency The beneficial effect of the rate.
  • the rectifying method is adopted in the three-stage airflow bed gasification device of the present invention, the rectifying method is adopted at the turn of the syngas, so that the uniformity of the airflow is maintained when the syngas enters the next step, and the heat exchanger is heated.
  • the utilization of the surface avoids the beneficial effects of material life reduction and heat exchange efficiency reduction caused by temperature deviation of the heated surface.
  • the invention combines the scientific and organic combination of "biomass solid waste slag flow bed technology” and "syngas separation temperature interval waste heat utilization technology", which can solve the various stages of biomass gas flow bed gasification and waste heat utilization.
  • the implementation conditions of the technical problems of the temperature interval provide the beneficial effects of implementing the biomass high-efficiency entrained flow gasification, controlling the carbon deposition reaction to prevent metal ashing corrosion, and preventing the alkali metal corrosion of the socks conditions, thereby obtaining a complete technology.
  • the solution has a substantial technological leap and progress, and has the beneficial effects of operability.
  • the organic fusion of the device and the technology set by the above various articles and the invention is scientific and reasonable, and the effect is stable and reliable.
  • the biomass cold gasification efficiency can reach 80% or more, and gasification is obtained.
  • the system energy utilization rate is above 94%, and the carbon conversion rate of the high-temperature gas flow bed in the entrained flow gasifier unit is more than 99.8%, the carbon conversion rate in the whole device is over 97%, and the gasification product is tar-free, CH 4 % content is less than 0.4%, the dry component of CO and H 2 in the syngas reaches 87% or more.
  • Syngas is produced, and the three-stage entrained flow gasifier device of the invention greatly reduces the occurrence of carbon precipitation reaction, effectively prevents the occurrence of metal ash corrosion and alkali metal corrosion, and avoids the prevention of alkali metal slagging and The slag blocks the syngas passage, which ensures the safe, stable and efficient operation of the entire gasification unit, and facilitates the implementation of the project, the low investment cost of the equipment, the wide application and the comprehensive economic benefits.
  • Figure 1 is a schematic illustration of one of the embodiments of the present invention. That is, the top of the high-temperature gas flow bed of the three-stage flow-bed gasification furnace device is arranged with a down burner, carbon powder, pyrolysis gas and oxygen enter the high-temperature gas flow bed through the down burner for gasification reaction, and the synthesis gas is at a high temperature.
  • the connecting passage formed in the airflow bed and passing through the inner wall by the optical tube membrane water-cooling wall enters the high-temperature heat exchanger and is rectified by the rectifying and shrinking, then cooled upward, and then passes through the connecting passage formed by the optical tube membrane water-cooling wall on the inner wall to enter the low temperature.
  • FIG. 1 Schematic diagram of down-cooling in a heat exchanger and rectifying by a rectifier.
  • the high temperature gas flow bed, the high temperature heat exchanger and the low temperature heat exchanger are arranged separately from each other;
  • the partial enlargement of the high temperature gas flow bed means that the inner wall of the high temperature gas flow bed is composed of a membrane type water wall coated with refractory material;
  • the rectification and shrinkage is provided to rectify and synthesize the syngas, and the partial enlargement of the high temperature heat exchanger means that the inner wall of the high temperature heat exchanger is composed of a light pipe membrane type water wall;
  • the high temperature air flow bed and the high temperature heat exchanger The lower end is provided with a slag discharge port;
  • the low temperature heat exchanger is provided with a rectifier for rectifying and synthesizing the syngas, and
  • the partial enlargement of the low temperature heat exchanger means that the inner wall of the low temperature heat exchanger adopts a light pipe membrane type water wall
  • FIG. 2 is a schematic view of a second embodiment of the present invention.
  • Three-stage airflow bed The top of the high-temperature gas flow bed of the gasifier device is arranged with a down burner, carbon powder, pyrolysis gas and oxygen enter the high-temperature gas flow bed through the down burner for gasification reaction, and the synthesis gas goes down in the high-temperature gas flow bed.
  • the rectification shrinkage enters the high-temperature heat exchanger and descends through the cooling passage through the inner wall, and the connecting passage formed by the diaphragm-type water-cooling wall enters the low-temperature heat exchanger and is rectified by the rectifying and shrinking, and then is cooled upward.
  • the high temperature gas flow bed and the high temperature heat exchanger are arranged in the upper and lower phase and are arranged separately from the low temperature heat exchanger;
  • the partial enlargement of the high temperature gas flow bed means that the inner wall of the high temperature gas flow bed is formed by the membrane water wall coated with the refractory material;
  • a high-pressure airflow bed and a high-temperature heat exchanger are provided with a rectifying and shrinking mouth to rectify the syngas to be evenly distributed;
  • a partial enlargement of the high-temperature heat exchanger means that the inner wall of the high-temperature heat exchanger adopts a light pipe film type water-cooled wall
  • the low temperature heat exchanger is provided with a slag discharge port;
  • the low temperature heat exchanger is provided with a rectifying and shrinking port to rectify and synthesize the syngas, and the partial enlargement of the low temperature heat exchanger indicates the furnace of the low temperature heat exchanger
  • the inner wall is composed of a light pipe membrane type water wall, and a lower
  • FIG. 3 is a schematic view of a third embodiment of the present invention. That is, the lower part of the high-temperature gas flow bed of the three-stage flow-bed gasification furnace device is arranged with a horizontal burner, and the carbon powder, pyrolysis gas and oxygen enter the high-temperature gas flow bed through the horizontal burner for gasification reaction, and the synthesis gas is at a high temperature.
  • the schematic diagram of the upstream of the entrained flow chamber, the rectification and shrinkage into the high-temperature heat exchanger, the upward cooling, and the connection passage formed by the optical tube membrane water-cooling wall on the inner wall enters the low-temperature heat exchanger and is rectified by the rectifier and then cooled downward.
  • the high temperature gas flow bed is arranged in parallel with the high temperature heat exchanger and is arranged separately from the low temperature heat exchanger; the partial enlargement of the high temperature gas flow bed indicates that the inner wall of the high temperature gas flow bed is coated with refractory material.
  • the membrane type water wall comprises a slag discharge port at a lower end of the high temperature air flow bed; a rectifying and shrinking port is arranged between the high temperature air flow bed and the high temperature heat exchanger to rectify and uniformly distribute the syngas; and the partial amplification of the high temperature heat exchanger
  • the inner wall of the furnace of the high-temperature heat exchanger is composed of a light pipe membrane type water-cooled wall; a rectifier is arranged in the low-temperature heat exchanger to rectify and uniformly distribute the synthesis gas, and the partial amplification of the low-temperature heat exchanger indicates the low-temperature heat exchange
  • the inner wall of the furnace is composed of a light pipe membrane type water wall, and a lower end of the low temperature heat exchanger is provided with a syngas outlet.
  • Fig. 4 is a schematic view showing the inner wall of the "high temperature air flow bed” furnace having a circular cross section in a specific embodiment of the present invention.
  • the partial enlargement in the figure indicates that the inner wall of the furnace of the high-temperature air flow bed is constituted by a membrane type water-cooled wall coated with a refractory material.
  • Fig. 5 is a schematic view showing the inner wall of the "high temperature air flow bed” furnace having a square cross section in a specific embodiment of the present invention.
  • the partial enlargement in the figure indicates that the inner wall of the furnace of the high-temperature air flow bed is constituted by a membrane type water-cooled wall coated with a refractory material.
  • Fig. 6 is a schematic view showing the inner wall of the "high temperature air flow bed” furnace having an octagonal cross section in a specific embodiment of the present invention.
  • the partial enlargement in the figure indicates that the inner wall of the furnace of the high-temperature air flow bed is constituted by a membrane type water-cooled wall coated with a refractory material.
  • the inner wall cross section of the "high temperature air flow bed” can be implemented in any manner of a circular shape or a square shape or an octagon shape as needed.
  • Fig. 7 is a schematic view showing the cross section of the inner wall of the "high temperature heat exchanger and low temperature heat exchanger” in a circular shape in a specific embodiment of the present invention.
  • the partial enlargement in the figure shows the high temperature heat exchanger and the low temperature heat exchanger "the inner wall of the furnace, which is composed of a light pipe membrane type water wall.
  • Figure 8 is a "high temperature heat exchanger and a low temperature heat exchanger" in an embodiment of the present invention
  • the cross section of the inner wall of the furnace is a square schematic view.
  • the partial enlargement in the figure shows that the high temperature heat exchanger and the "furnace inner wall" of the low temperature heat exchanger are both formed by a light pipe membrane type water wall.
  • Fig. 9 is a schematic view showing the cross section of the inner wall of the "high temperature heat exchanger and the low temperature heat exchanger" in an octagonal shape in the embodiment of the present invention.
  • the partial enlargement in the figure indicates that the high temperature heat exchanger and the low temperature heat exchanger "furnace inner wall” are both formed by a light pipe membrane type water wall.
  • the inner wall cross section of the "high temperature heat exchanger and low temperature heat exchanger" can be implemented in any combination of a circular shape or a square shape or an octagonal shape as needed.
  • Figure 10 is a schematic diagram of a "chilled water atomizing nozzle" of a quenching chamber in a high temperature heat exchanger in which the inner wall of the high temperature heat exchanger is constructed by a light pipe membrane type water wall, and the cross section is circular. Schematic diagram of the arrangement of the horizontal annular atomizing water spray.
  • Figure 11 is a schematic diagram of a "chilled water atomizing nozzle" of a quenching chamber in a high temperature heat exchanger in which the inner wall of the high temperature heat exchanger is constructed of a light pipe membrane type water wall, and the cross section is square. Schematic diagram of the arrangement of the annular atomized water spray.
  • Figure 12 is a schematic diagram of a "chilled water atomizing nozzle" of a chilling chamber in a high temperature heat exchanger when the inner wall of the high temperature heat exchanger is constructed of a light pipe membrane type water wall and has an octagonal cross section. Schematic diagram of the mode arrangement of horizontal annular atomizing water spray.
  • Figure 13 is a schematic diagram of a "chilled water atomizing nozzle" of a quenching chamber in a high temperature heat exchanger in which the inner wall of the high temperature heat exchanger is constructed by a light pipe membrane type water wall, and the cross section is circular.
  • Figure 14 is a schematic diagram of a "chilled water atomizing nozzle" of a quenching chamber in a high temperature heat exchanger in which the inner wall of the high temperature heat exchanger is constructed by a light pipe membrane type water wall, and the cross section is square. Schematic diagram of the arrangement of the upper and lower atomized water sprays/or the bottom sprayed water sprays. That is: when the syngas is ascending, it is arranged in the manner of "spinning water spray from top to bottom”; when the syngas is descending, it is arranged in the manner of "atomization spray from bottom to top”.
  • Figure 15 is a schematic diagram of a "chilled water atomizing nozzle" of a quenching chamber in a high temperature heat exchanger when the inner wall of the high temperature heat exchanger is constructed of a light pipe membrane type water wall and the cross section is octagonal in the embodiment of the present invention.
  • a biomass three-stage entrained flow gasification technology with waste heat utilization using biomass as raw material, raw materials obtained by pyrolysis to obtain solid carbon and pyrolysis gas, solid carbon is ground to obtain carbon powder, and carbon powder is pyrolyzed / Nitrogen / carbon dioxide gas transport, while using oxygen as oxidant, carbon powder, pyrolysis gas and oxygen through the burner into the gas flow bed for gasification reaction, to obtain high temperature synthesis gas, the physical heat of high temperature synthesis gas through the gasification furnace
  • the heat exchanger transfers heat to the water to generate superheated steam, and the high temperature syngas cools and then flows out of the gasifier;
  • the airflow bed gasifier device with residual heat utilization is divided into three sections, which are a high temperature gas flow bed, a high temperature heat exchanger, and a low temperature heat exchanger;
  • an entrained-flow gasification technique using solid-state slagging wherein the inner wall of the high-temperature entrained bed is composed of a membrane-type water-cooled wall coated with a refractory material, and the syngas outlet of the high-temperature entrained bed
  • the temperature is between 1280 ° C ⁇ 1320 ° C;
  • the inlet temperature of the syngas is between 1280 ° C and 1320 C, and the outlet temperature is between 580 ° C and 600 ° C;
  • the inner wall of the furnace of the high temperature heat exchanger is light.
  • a tubular membrane water wall in which a chill chamber and a high temperature superheater are arranged, and a temperature of the syngas entering the chill chamber is between 1000 ° C and 1100 ° C, leaving the chill
  • the temperature of the syngas after chilling is between 700 ° C and 800 ° C;
  • the inlet temperature of the syngas is between 580 ° C and 600 ° C, and the outlet temperature is between 220 ° C and 230 ° C;
  • the inner wall of the furnace of the low temperature heat exchanger is a light pipe membrane type water wall, in which a low temperature is arranged Superheater and economizer.
  • the biomass three-stage entrained flow gasification technology with waste heat utilization as shown in FIG. 1 , the top of the high temperature air flow bed of the three-stage air flow bed gasification device is arranged with a down burner,
  • the carbon powder, pyrolysis gas and oxygen enter the high-temperature gas flow bed through the down burner for gasification reaction, and the synthesis gas descends in the high-temperature gas flow bed, and enters through the connecting channel formed by the inner wall of the light pipe membrane water-cooling wall
  • the cooling is carried out, and then the connecting passage formed by the optical tube membrane water-cooling wall on the inner wall enters the low-temperature heat exchanger and is rectified by the rectifier and then cooled downward.
  • the biomass three-stage entrained flow gasification technology with waste heat utilization as shown in FIG. 2, a descending burner is arranged on the top of the high temperature entrained flow bed of the three-stage entrained flow gasifier device,
  • the carbon powder, pyrolysis gas and oxygen enter the high-temperature gas flow bed through the down burner for gasification reaction, and the synthesis gas descends in the high-temperature gas flow bed, passes through the rectification and shrinkage into the high-temperature heat exchanger, and is cooled downward, and then
  • the connecting passage formed by the optical tube membrane water-cooling wall on the inner wall enters the low-temperature heat exchanger and is rectified by the rectifying and shrinking, and then cooled upward.
  • the biomass three-stage entrained flow gasification technology with waste heat utilization as shown in FIG. 3, a horizontal burner is disposed at a lower portion of the high temperature air flow bed of the three-stage air flow bed gasification device.
  • the carbon powder, pyrolysis gas and oxygen enter the high-temperature gas flow bed through the horizontal burner for gasification reaction, and the synthesis gas rises in the high-temperature gas flow bed, passes through the rectification and shrinkage into the high-temperature heat exchanger, and is cooled upward, and then
  • the connecting passage formed by the optical tube membrane water wall through the inner wall enters the low temperature heat exchanger and is rectified by the rectifier After the downside cooling.
  • the biomass three-stage entrained flow gasification technology with waste heat utilization as shown in Figures 4, 5, 6, 7, 8, and 9, the inner wall cross section of the three-stage air flow bed gasification furnace device It is a kind of any combination of round, square, octagonal, round/square/octagonal. 4, 5, and 6:
  • the inner wall cross-section of the "high-temperature air-flow bed" furnace of the three-stage air-flow bed gasifier is implemented in a circular, square, and octagonal shape, respectively.
  • the cross-sections of the inner wall of the "high-temperature heat exchanger and low-temperature heat exchanger" of the three-stage air-flow gasifier are circular, square, octagonal, and round, respectively.
  • One of any combination of shape/square/octagonal shape was implemented.
  • the biomass three-stage entrained flow gasification technology with waste heat utilization as shown in Figures 1, 2, and 3, in the high temperature heat exchanger, uses water as a chilling agent.
  • the residence time of the syngas in the chill chamber is within 0.3 seconds.
  • the biomass three-stage entrained flow gasification technology with waste heat utilization as shown in Figures 10, 11, 12, 13, 14, and 15, in the high temperature heat exchanger, the chilling of the chilling chamber
  • the water spray method adopts one of atomized spray water from top to bottom, or atomized spray water from bottom to top, or horizontal annular atomized spray water.
  • the cross section of the inner wall of the high temperature heat exchanger is one of a circular, square, octagonal, circular/square/octagonal combination
  • the chilling of the chilling chamber The water spray methods were all arranged in a "horizontal annular atomizing water spray" arrangement.
  • the cross section of the inner wall of the high temperature heat exchanger is circular, square, octagonal, One type of circular/square/octagonal combination; in combination with the chilling water spray method of the chilling chamber shown in Fig. 1, the arrangement is arranged in a "top-down atomization spray” manner, which is combined with FIG.
  • the chilling water spray mode of the chilling chamber is arranged in a "bottom-up atomized water spray” manner, combined with the chilling water spray method of the chill chamber shown in Fig. 3
  • the water spray "mode arrangement was implemented.
  • the biomass three-stage flow-bed gasification technology with waste heat utilization, in the high-temperature heat exchanger, the high-temperature superheater heating surface tube bundle adopts a high-pressure steam purge method or a mechanical rapping method Perform ash removal.
  • the two methods of ash removal were implemented separately.
  • the biomass three-stage entrained flow gasification technology with waste heat utilization as shown in Figures 1, 2, and 3, wherein the three-stage flow-bed gasification furnace device adopts a rectification method at the syngas turn , to keep the airflow evenly distributed when the syngas enters the next step.
  • biomass raw materials are taken as examples of fuel charcoal paralysis.
  • the elemental analysis and characteristic data of paralyzed after drying are shown in Table 1:
  • the syngas side operating pressure of the three-stage entrained flow gasifier device is 3.6 MPa, and the pyrolysis gas at the inlet of the down burner/horizon burner is 3.69 kg/s, and the carbon powder is 1.2. Kg/s, the mixing temperature of carbon powder and pyrolysis gas is 350 ° C, the oxidant uses oxygen with a temperature of 150 ° C and a purity of 99.4%, and the amount of oxygen entering the high temperature gas flow bed is 1.46 kg / s.
  • the total amount of syngas (excluding chilled water) at the outlet of the three-stage entrained flow gasifier is 6.35 kg/s, and the ash content is 0.13 kg/s.
  • the carbon conversion rate of the high temperature entrained bed is 99.8%, and the gasification efficiency of the three-stage entrained flow gasifier unit is 80.2%; 4,
  • the temperature of the superheated steam is 5. 0 MPa, the outlet temperature is 480 ° C, the amount of superheated steam is 16. 0 T / h.
  • the implementation is performed on the basis of the implementation of the first embodiment.
  • the top of the high-temperature airflow bed of the three-stage airflow bed gasification device is arranged with a down burner, the carbon powder and pyrolysis.
  • Gas and oxygen enter the high temperature gas flow bed through the down burner for gasification reaction, and the synthesis gas descends in the high temperature gas flow bed, passes through the connecting channel formed by the inner wall of the membrane film water wall into the high temperature heat exchanger and passes through
  • the cooling channel is cooled upward, and then the connecting passage formed by the optical tube membrane water-cooling wall on the inner wall enters the low-temperature heat exchanger and is rectified by the rectifier and then cooled downward.
  • the biomass feedstock used is still paralyzed (see Table 1 in Specific Embodiment 1) as an example, and the main process operating conditions are as in the first embodiment.
  • the results obtained through implementation are:
  • the total amount of syngas (excluding chilled water) at the outlet of the three-stage air-flow gasifier is 6.3 kg/s, and the ash content is 0.13 kg/s.
  • the top of the high-temperature airflow bed of the three-stage airflow bed gasification device is arranged with a down burner, the carbon powder
  • the pyrolysis gas and the oxygen gas enter the high-temperature airflow bed through the down-burning burner for gasification reaction, and the syngas is descended in the high-temperature airflow bed, passes through the rectification and shrinkage into the high-temperature heat exchanger, descends and cools, and then passes through the inner wall by the light.
  • the connecting channel formed by the tubular membrane water wall enters the low temperature heat exchanger and is rectified by the rectifying and shrinking, and then cooled upward.
  • the biomass feedstock used is still numb (see Table 1 in Specific Embodiment 1) as an example, and the main process operating conditions are as in the first embodiment. The results obtained through implementation are:
  • the total amount of syngas (excluding chilled water) at the outlet of the three-stage entrained flow gasifier is 6.35 kg/s, and the ash content is 0.13 kg/s.
  • the lower part of the high-temperature airflow bed of the three-stage airflow bed gasification device is arranged with a horizontal burner, the carbon powder
  • the pyrolysis gas and oxygen enter the high-temperature gas flow bed through the horizontal burner for gasification reaction, and the synthesis gas rises in the high-temperature gas flow bed, passes through the rectification and shrinkage into the high-temperature heat exchanger, is cooled upward, and then passes through the inner wall by the light.
  • the connecting channel formed by the tubular membrane water wall enters the low temperature heat exchanger and is rectified by the rectifier and then cooled downward.
  • the biomass feedstock used is still paralyzed (see Table 1 in Specific Embodiment 1) as an example.
  • the main process operating conditions are as in the first embodiment.
  • the scars achieved through implementation are:
  • the total amount of syngas (excluding chilled water) at the outlet of the three-stage entrained flow gasifier is 6.3 kg/s, and the ash content is 0.13 kg/s.
  • the carbonization efficiency of the three-stage flow-bed gasification unit is 80. 2%;

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Description

带余热利用的生物质三段式气流床及其气化方法 技术领域
本发明的带余热利用的生物质三段式气流床气化技术，涉及 能源化工技术领域； 特别涉及生物质的热化学技术领域； 尤其涉 及生物质气化技术的技术领域；具体涉及带佘热利用的生物质气 流床气化技术领域。 背景技术 '
生物质中的植物是通过光合作用吸收空气中二氧化碳生成 的有机物质， 其分布广泛、 可利用量大、 并且是唯一可再生的含 有碳氢组分和热能的、 可储存的自然原料； 利用生物质进行能源 利用和化工生产， 具有 co2零排放的特征。 随着传统化石能源储 量的日益减少， 以及由于使用化石能源带来的环境污染问题， 重 视和发展可再生、环保能源已成为各国政府的共识。通过热化学、 生物化学等方法， 能够将生物质转变为清洁的气体或液体燃料， 生产令成柴油 /汽油、 化工产品以及满足电力需求等等， 具有全 面替代化石能源的潜力， 将成为世界各国优先发展的新能源。
将生物质转变为清洁气体或液体燃料的方法很多， 在这其 中， 生物质气化技术与其它技术相比能够适应所有的生物质种 类， 且具有工业化大型生产的能力。
生物质的气化过程是一种热化学过程， 是生物质原料与气化 剂（空气、 氧气、 水蒸气、二氧化碳等）在高温下发生化学反应， 将固态的生物质原料转变为由碳、 氢、 氧等元素组成的气体组分 的混合气体的过程， 该混合气体通常被称为合成气。 气化过程产 生的合成气的组成随气化时所用生物盾原料的性质、气化剂的类 别、 气化过程的条件以及气化炉的结构不同而不同。 而满足用于 生产合成柴油 /汽油、 化工产品合成气一一即精制合成气的气化 目标在于尽量减少原料和氧化剂（如氧气等）的消耗量以及合成 气中的甲烷含量， 并且没有焦油产生， 同时最大化系统的气化效 率、 碳转化率以及合成气中有效成分（0)和^12 ) 的含量。
精制合成气指的是： 采用气化装置气化而直接得到的合成气 的混合物中 CO和 H2为主要组分， 无焦油， CH4含量 <0. 5%。 精制 合成气主要用于生产合成柴油 /汽油、 烯烃、 烷烃、 石脑油、 润 滑油， 以及作为燃料电池原料等等， 适用于生产各种化工产品、 以及各种超清洁油品的新能源利用，特别在可再生的生物质能源 利用领域， 生物质的精制气化技术是生物质化工产业、生物质合 成油新能源产业、 具有工业化大型生产能力的关键气化技术。 分为三类： 固定床、 流化床和气流床气化技术。 固定床气化生产 的合成气热值较低， 且含有大量焦油； 流化床气化对原料的性质 很敏感， 运行温度较低， 出口合成气中焦油含量较高。 由于固定 床和流化床一般都采用空气作为氧化剂，以及气化压力一般为常 压，合成气中含有大量的焦油， 在后续设备中不得不安装焦油裂 解和净化装置， 使得气化工艺变得十分复杂。 总而言之， 这两种 气化方法的核心问题是由于气化平均温度较低，一般气化炉出口 温度都不能超过 1100°C， 而导致焦油产生和合成气中的甲烷含 量较高， 都不能满足生物质高效气化和生产精制合成气的要求。
气流床的气化温度较高， 炉内温度比较均匀， 焦油在气流床 中全部裂解， CH4含量较少， 同时气流床具有很好的放大特性， 特别适用于大型工业化的应用，是生物质生产精制合成气的最佳 方式。但是，生物质气流床气化也有以下四大核心问题需要解决： 第一， 气流床气化对原料的粒径有着严格的限制， 进入气流 床的原料需要磨成超细的颗粒， 然而按照现有的破碎或制粉技 术，无法将含纤维较多的生物质原料磨制成满足气流床运行所需 的粒径， 这就导致了无法将生物质原料直接用于气流床气化。
第二，气流床合成气出口温度都很高，一般都在 1300 °C以上， 而合成气的应用还需净化或变换， 这需要将合成气的温度降到 250 左右， 这段合成气的余热如果不能充分利用， 将导致整个 气化系统的效率低下。
第三， 由于生物质原料的碱金属 U、 Na )含量较高， 它们 在高温时以气态的形式存在， 在合成气的降温过程中， 在 800 X： ~ 600 C区间会凝结为固态而附着于换热器管子壁面， 引起受 热面管子的碱金属腐蚀和结渣并堵塞合成气通道。
第四， 由于生物质气化得到的合成气在降温过程中有析 应发生，在某一温度区间还将发生剧烈的析碳反应，合成气中的 CO反应生成 C02和碳黑，从而引起碳转化效率降低和气化效率降 低， 同时由于碳黑沉积于换热器管子金属表面， 引起金属灰化导 致金属腐蚀的发生。
目前基本上所有的生物质气流床气化技术， 针对问题一， 一 般都是先将生物质进行热解得到热解气和固态炭，然后将热解气 和固态炭粉送入气流床中气化。生物质的气流床技术有如同煤粉 气化的液态排渣方法，其合成气出口温度一般都控制在 13001C ~ 1500 之间， 如申请号为 2006101245707、 2006101245711的中 国专利， 以及德国科林公司的 Carbon - V气化技术， 还有本公司 开发的中国专利申请号为 200910210433. 9的生物质固态排渣高 温气流床气化技术。 但针对问题二、 三、 四， 目前世界上所有针 对生物质气流床气化的技术， 或没有很好地利用合成气余热、或 没有解决析碳反应的金属灰化问题、或没有较好的方法控制碱金 属腐蚀及结渣的发生。
为此， 本发明根据生物质原料特点， 以及需要解决的上述四 大问题， 在认真而充分的调查、 了解、 分析、 总结上述已有公知 技术和现状基础上，针对生物质气流床精制气化要求、余热利用 要求、控制合成气析碳反应并防止金属灰化腐蚀、控制生物质碱 金属腐蚀并防止碱金属结渣及落渣堵塞合成气通道等问题，开发 了 "带余热利用的生物质三段式气流床气化技术"， 特别适用于 生物质的精制气化及生物质合成气余热利用，不仅综合解决了上 述四大问题， 并可以安全、 高效、 稳定、 低投资地满足生物质的 精制气化合成气要求， 具有非常重要的意义。 发明内容
本发明根据生物质原料特点，针对生物盾气流床气化以及合 成气在不同温度区间的主要化学反应特点， 提供一种 "带余热利 用的生物质三段式气流床气化技术"。 以生物质为原料， 原料经 热解获得固态炭和热解气， 将固态炭研磨后获得炭粉， 炭粉由热 解气 /氮气 /二氧化碳气体输送， 同时采用氧气为氧化剂， 炭粉、 热解气和氧气通过燃烧器进入气流床中进行气化反应，得到高温 合成气，高温合成气的物理热通过气化炉内的换热器将热量传递 给水产生过热蒸汽 ,· 高温合成气冷却后流出气化炉。
本发明创造点在于： ①、将所述的带余热利用的气流床气化 炉装置分成三段，分别为高温气流床、高温换热器、低温换热器； ②、 在所述高温气流床中， 采用固态排渣的气流床气化技术， 所 述高温气流床的炉内壁采用敷有耐火材料的膜式水冷壁构成，所 述高温气流床的合成气出口温度在 1280°C ~ 1320°C之间； ③、 在所述高温换热器中， 合成气的入口温度在 1280°C ~ 1320°C之 间， 出口温度在 580°C ~ 600°C之间； 所述高温换热器的炉内壁 采用光管膜式水冷壁构成，所述高温换热器中布置有激冷室和高 温过热器， 进入所述激冷室的合成气温度在 1000°C ~ 1100°C之 间， 离开所述激冷室激冷后的合成气温度在 700°C - 800°C之间； ④、 在所述低温换热器中， 合成气的入口温度在 580°C ~ 600°C 之间， 出口温度在 220°C〜230°C之间； 所述低温换热器的炉内壁 采用光管膜式水冷壁构成，所述低温换热器中布置有低温过热器 和省煤器。
本发明的带余热利用的三段式气流床气化技术所采用的气 流床气化炉装置可以采用以下三种形式中的任意一种：
(1)、装置形式一： 所述带余热利用的三段式气流床气化炉装 置的所述高温气流床的顶部布置有下行式燃烧器， 所述炭粉、 热 解气和氧气通过所述下行式燃烧器进入高温气流床中进行气化 反应， 合成气在高温气流床中下行、 经过内壁由光管膜式水冷壁 构成的连接通道进入高温换热器中并经过整流缩口整流后上行 冷却、再经过内壁由光管膜式水冷壁构成的连接通道进入低温换 热器中并经整流器整流后下行冷却。
(2)、装置形式二： 所述带余热利用的三段式气流床气化炉装 置的所述高温气流床的顶部布置有下行式燃烧器， 所述炭粉、 热 解气和氧气通过所述下行式燃烧器进入高温气流床中进行气化 反应， 合成气在高温气流床中下行、 经过整流缩口进入高温换热 器中下行冷却、再经过内壁由光管膜式水冷壁构成的连接通道进 入^ ί氐温换热器中并经过整流缩口整流后上行冷却。
(3)、装置形式三： 所述带余热利用的三段式气流床气化炉装 置的所述高温气流床的下部布置有水平式燃烧器， 所述炭粉、 热 解气和氧气通过所述水平式燃烧器进入高温气流床中进行气化 反应， 合成气在高温气流床中上行、 经过整流缩口进入高温换热 器中上行冷却、再经过内壁由光管膜式水冷壁构成的连接通道¾ 入低温换热器并经整流器整流后下行冷却。 本发明的三段式气流床气化炉装置的炉内壁横截面为圆形、 方形、 八角形、 圓形 /方形 /八角形任意组合的一种。
本发明的所述高温换热器中， 激冷室以水作为激冷剂， 合成 气在激冷室的停留时间在 0.3秒以内， 激冷室的激冷喷水方式采 用自上向下雾化喷水、或自下向上雾化喷水、或水平环形雾化喷 水中的一种，同时对高温过热器受热面管束采用高压蒸汽吹扫方 式或采用机械振打方式进行除灰。
本发明的三段式气流床气化炉装置中在合成气转向处均采 用了整流方法， 使合成气进入下一个环节时保持气流均匀分布。
通过本发明达到的目的是：
①、为摆脱传统化石能源储量日益减少及其带来环境污染的 窘迫境地， 提供新能源利用的技术储备及技术实施；
②、 充分利用由自然生成、 数量大、 分布广、 可再生的 "生 物质" 新原料， 变废为宝并有效地保护环境；
③、 将整个气化装置分成 "高温气流床、 高温换热器、 低温 换热器" 的三段有机连接， 解决生物质气化和余热利用过程中的 各种技术问题， 构成了 "带余热利用的气流床气化炉装置"新设 备， 提供了生物质高效气化和合成气余热利用的实施载体；
④、 以高温气流床合成气出口温度控制在 "1280°C ~ 1320 之间； 高温换热器的合成气出口温度控制在 580°C ~ 600°C之间， 其中合成气激冷温度范围从 1000°C ~ 1100°C激冷至 700°C ~ 800 °C ; 低温换热器的合成气出口温度控制在 220°C〜230°C之间， 构成了可以分别解决在生物质高温气流床气化、余热利用的各阶 段温度区间的技术难题的实施条件，提供了实施高温气流床气化 以及控制析碳反应、 金属灰化腐蚀、 碱金属腐蚀的技术条件；
⑤、 以合成气温度在 580°C ~ 600°C为界， 将高温换热器和 低温换热器分开在不同的合成气通道中，为解决碱金属结渣落渣 堵塞合成气通道的技术问题提供了实施条件；
⑥、 以 "生物质固态排渣气流床技术，， 与 "合成气分温度区 间余热利用技术"科学有机结合，构成本发明突出的发明创造点；
⑦、通过本发明的实验性实施， 不仅获得了生物质气流床气 化得到 CO和 H2为主要组分、无焦油、（¾含量 <0.5%的精制合成 及供热，极大地提高了整个气化系统效率达到 94%以上，作为生 物质化工产业、 生物质合成油新能源产业的技术依托， 使其在生 产合成柴油 /汽油、 烯烃、 烷烃、 石脑油、 润滑油、 燃料电池原 料等等， 以及各种化工产品， 各种超清洁油品的经济领域发挥应 有的作用；
⑧、 合理利用能源、 有效保护环境、 提高综合经济效益。 为实现上述目的， 本发明提供的技术方案为：
一种带余热利用的生物质三段式气流床气化技术，以生物质 为原料， 原料经热解获得固态炭和热解气， 将固态炭研磨后获得 炭粉， 炭粉由热解气 /氮气 /二氧化碳气体输送， 同时采用氧气为 氧化剂， 炭粉、 热解气和氧气通过燃烧器进入气流床中进行气化 反应， 得到高温合成气， 高温合成气的物理热通过气化炉内的换 热器将热量传递给水产生过热蒸汽，高温合成气冷却后流出气化 炉； 其发明创造点与实施要点主要体现在：
①、将所述的带余热利用的气流床气化炉装置分成三段， 分 别为高温气流床、 高温换热器、 低温换热器；
②、在所述高温气流床中，采用固态排渣的气流床气化技术， 所述高温气流床的炉内壁采用敷有耐火材料的膜式水冷壁构成， 所述高温气流床的合成气出口温度在 1280°C ~ 1320°C之间；
③、 在所述高温换热器中， 合成气的入口温度在 1280°C ~ 1320°C之间， 出口温度在 580°C ~ 600°C之间； 所述高温换热器 的炉内壁采用光管膜式水冷壁构成，所述高温换热器中布置有激 冷室和高温过热器， 进入所述激冷室的合成气温度在 1000°C ~ 1100°C之间， 离开所述激冷室激冷后的合成气温度在 700°C ~ 800°C之间；
④、 在所述低温换热器中， 合成气的入口温度在 580°C ~ 600°C之间， 出口温度在 220°C〜230°C之间； 所述低温换热器的 炉内壁采用光管膜式水冷壁构成，所述低温换热器中布置有低温 过热器和省煤器。
本发明的带余热利用的三段式气流床气化炉装置可以采用 以下三种形式中的任意一种：
装置形式一：所述的带余热利用的生物质三段式气流床气化 技术，所述三段式气流床气化炉装置的所述高温气流床的顶部布 置有下行式燃烧器， 所述炭粉、 热解气和氧气通过所述下行式燃 烧器进入高温气流床中进行气化反应，合成气在高温气流床中下 行、经过内壁由光管膜式水冷壁构成的连接通道进入高温换热器 中并经过整流缩口整流后上行冷却、再经过内壁由光管膜式水冷 壁构成的连接通道进入低温换热器中并经整流器整流后下行冷 却。
装置形式二：所述的带余热利用的生物质三段式气流床气化 技术，所述三段式气流床气化炉装置的所述高温气流床的顶部布 置有下行式燃烧器， 所述炭粉、 热解气和氧气通过所述下行式燃 烧器进入高温气流床中进行气化反应，合成气在高温气流床中下 行、 经过整流缩口进入高温换热器中下行冷却、再经过内壁由光 管膜式水冷壁构成的连接通道进入低温换热器中并经过整流缩 口整流后上行冷却。
装置形式三：所述的带余热利用的生物质三段式气流床气化 技术，所述三段式气流床气化炉装置的所述高温气流床的下部布 置有水平式燃烧器， 所述炭粉、 热解气和氧气通过所述水平式燃 烧器进入高温气流床中进行气化反应，合成气在高温气流床中上 行、 经过整流缩口进入高温换热器中上行冷却、再经过内壁由光 管膜式水冷壁构成的连接通道进入低温换热器并经整流器整流 后下行冷却。
所述的带余热利用的生物质三段式气流床气化技术，所述三 段式气流床气化炉装置的炉内壁横截面为圓形、 方形、 八角形、 圆形 /方形 /八角形任意组合的一种。
所述的带余热利用的生物质三段式气流床气化技术，在所述 的高温换热器中， 所述激冷室以水作为激冷剂， 所述合成气在激 冷室的停留时间在 0.3秒以内。
所述的带余热利用的生物质三段式气流床气化技术，在所述 的高温换热器中， 激冷室的激冷喷水方式采用自上向下雾化喷 水、 或自下向上雾化喷水、 或水平环形雾化喷水中的一种， 同时 对所述的高温过热器受热面管束采用高压蒸汽吹扫方式或采用 机械振打方式进行除灰。
所述的带余热利用的生物质三段式气流床气化技术，所述三 段式气流床气化炉装置中在合成气转向处均采用了整流方法，使 合成气进入下一个环节时保持气流均匀分布。 由于采用了本发明所提供的技术方案。 由于本发明采用了 "固态排渣的气流床气化技术" 以及 "合成气分温度区间余热利 用技术"构成了 "带余热利用的生物质三段式气流床气化技术"。 由于本发明以生物质为原料， 原料经热解获得固态炭和热解气， 将固态炭研磨后获得炭粉， 炭粉由热解气 /氮气 /二氧化碳气体输 送， 同时采用氧气为氧化剂， 炭粉、 热解气和氧气通过燃烧器进 入气流床中进行气化反应， 得到高温合成气， 高温合成气的物理 热通过气化炉内的换热器将热量传递给水产生过热蒸汽，高温合 成气冷却后流出气化炉； 由于本发明采用将带余热利用的气流床 气化炉装置分成三段， 分别为高温气流床、 高温换热器、 低温换 热器； 在高温气流床中， 采用固态排渣的气流床气化技术， 高温 气流床的炉内壁采用敷有耐火材料的膜式水冷壁构成，高温气流 床的合成气出口温度在 1280 °C ~ 1320 °C之间； 在高温换热器中， 合成气的入口温度在 1280°C ~ 1320 °C之间， 出口温度在 580°C ~ 600°C之间； 高温换热器的炉内壁采用光管膜式水冷壁构成， 高 温换热器中布置有激冷室和高温过热器，进入所述激冷室的合成 气温度在 1000 °C ~ 1100°C之间， 离开所述激冷室激冷后的合成 气温度在 700°C ~ 800°C之间； 在低温换热器中， 合成气的入口 温度在 580°C ~ 600°C之间， 出口温度在 220°C〜230°C之间； 低温 换热器的炉内壁采用光管膜式水冷壁构成，低温换热器中布置有 低温过热器和省煤器。使得本发明与已有公知技术相比， 获得了 如下有益效果：
1、 由于本发明将整个气流床气化炉装置分成 "高温气流床、 高温换热器、 低温换热器" 的三段有机连接， 为生物质气化和余 热利用过程中的各种技术问题的解决提供了基础和方向，构成的
"带余热利用的气流床气化炉装置"新设备，提供了生物质高效 气化和合成气余热利用的实施载体的有益效果。
2、 由于本发明以高温气流床合成气出口温度控制在 1280°C ~ 1320°C之间 ,并采用了固态排渣的生物质气流床气化技 术， 高温气流床炉内壁采用敷有耐火材料的膜式水冷壁构成， 获 得了气流床冷气化效率可达 80%以上、 气流床的碳转化率达 99. 8%以上、气化产物为无焦油、（¾含量小于 0. 4%、合成气中 CO 和 ¾的干基组分达到 87%以上的精制合成气的有益效果。 '
3、 由于本发明的高温气流床出口合成气进入高温换热器， 高温换热器的合成气出口温度控制在 580°C ~ 600°C之间， 随后 进入低温换热器， 合成气在 220°C〜230°C之间才流出气流床气化 炉装置， 高温气流床、 高温换热器和低温换热器都布置有工质
(水、 汽）受热面， 合成气的物理热传递给水变成过热蒸汽， 过 热蒸汽可用于发电及供热，这将占到整个气化系统能量 14%的合 成气余热充分利用，实现了整个气化系统的能量利用率达到 94% 以上的有益效果。
4、 由于本发明在高温换热器中布置有激冷室， 将合成气从 从 1000°C ~ 1100°C激冷至 700°C ~ 800 °C , 并且合成气在激冷室 中的停留时间在 0.3秒以内， 该温度区间为合成气析碳反应最剧 烈区间，合成气通过快速激冷而迈过该温度区间， 这将极大地减 少了合成气的析碳反应， 控制了碳黑析出， 提高了气流床气化炉 装置的碳转化效率，控制了由于碳黑析出而与受热面管材反应导 致金属灰化腐蚀的发生。
5、 由于本发明在高温换热器中， 合成气被激冷后进入高温 过热器， 合成气的温度处于 800°C〜600°C之间， 合成气中的气态 碱金属凝结为固态， 并容易附着于受热面管子并结渣， 为了避免 碱金属腐蚀的发生和管子结渣，在高温过热器中采用高压蒸汽吹 扫或机械振打对受热面管束进行除灰，同时由于本发明采用了三 段式气流床气化炉装置，高温换热器与低温换热器在两个不同的 通道中， 高温换热器中吹灰产生的落渣直接从排淦口排出， 不会 掉入低温换热器的受热面管子中而堵塞合成气通道。
6、 由于本发明所述三段式气流床气化炉装置可以采用三种 不同的装置形式， 分别是： ①三段式气流床气化炉装置的高温气 流床的顶部布置有下行式燃烧器， 炭粉、 热解气和氧气通过下行 式燃烧器进入高温气流床中进行气化反应，合成气在高温气流床 中下行、经过内壁由光管膜式水冷壁构成的连接通道进入高温换 热器中并经过整流缩口整流后上行冷却、再经过内壁由光管膜式 水冷壁构成的连接通道进入低温换热器中并经整流器整流后下 行冷却。②三段式气流床气化炉装置的高温气流床的顶部布置有 下行式燃烧器， 炭粉、 热解气和氧气通过所述下行式燃烧器进入 高温气流床中进行气化反应，合成气在高温气流床中下行、 经过 整流缩口进入高温换热器中下行冷却、再经过内壁由光管膜式水 冷壁构成的连接通道进入低温换热器中并经过整流缩口整流后 上行冷却。③三段式气流床气化炉装置的高温气流床的下部布置 有水平式燃烧器， 炭粉、 热解气和氧气通过所述水平式燃烧器进 入高温气流床中进行气化反应， 合成气在高温气流床中上行、 经 过整流缩口进入高温换热器中上行冷却、再经过内壁由光管膜式 水冷壁构成的连接通道进入低温换热器并经整流器整流后下行 冷却。 从而获得了针对各种具体的工程设计要求和设备布置要 求， 实现了带余热利用的生物质三段式气流床气化技术的各种不 同实施方案的有益效果。 7、 由于本发明所述三段式气流床气化炉装置的炉内壁横截 面为圆形、 方形、 八角形、 圆形 /方形 /八角形任意组合的一种， 从而获得了可根据高温气流床、 高温换热器、低温换热器三段的 不同的布置要求， 以及高温气流床内的气化燃烧要求、 高温 /和 低温换热器受热面管束的布置形式要求， 选用圆形截面、 方形截 面、 八角形截面、 以及在各段之间采用圆形、 八角形与方形截面 的组合， 实现了气化炉装置受热面管束结构简单， 布置方便， 占 有空间紧凑、 材料选用方便、 安装简单、 最大限度地节省材料等 益效果。
8、 由于本发明在所述三段式气流床气化炉装置形式一 /二中 的高温气流床的顶部布置有下行式燃烧器，在所述三段式气流床 气化炉装置形式三中的高温气流床的下部布置有水平式燃烧器， 炭粉、 热解气和氧气通过燃烧器进入高温气流床中进行气化反 应，可以分别提供了生物质固态排渣气流床要求的气化燃烧方式 的实施条件， 实现了生物质的高效气流床气化反应效率。
9、 由于本发明所述激冷室的激冷喷水方式采用自上向下雾 化喷水、 或自下向上雾化喷水、 或水平环形雾化喷水中的一种， 从而获得了可根据合成气的具体的流动方向（上行或下行）以及 气流床气化炉装置的具体结构布置要求，选择上述三种喷水雾化 激冷方式中的一种， 都可实现在激冷室中 0.3秒内可将合成气从 1000°C ~ 1100°C之间激冷至 700 °C ~ 800 °C之间， 极大地降低了 合成气的析碳反应，起到了控制金属灰化腐蚀以及提高碳转化效 率的有益效果。
10、由于本发明所述三段式气流床气化炉装置中在合成气转 向处均采用了整流方法，从而获得了使合成气进入下一个环节时 保持气流均匀分布， 提高了换热器受热面的利用率， 避免了受热 面温度偏差而造成的材质寿命降低和换热效率降低等有益效果。
11、 由于本发明以 "生物质固态排渣气流床技术" 与 "合成 气分温度区间余热利用技术"的科学有机结合， 构成了可以分别 解决在生物质气流床气化、余热利用的各阶段温度区间的技术难 题的实施条件， 提供了实施生物质高效气流床气化、控制析碳反 应以防止金属灰化腐蚀，和防止碱金属腐蚀的袜术条件的有益效 果， 从而获得了完备的技术方案、 与已有公知技术相比发生了实 质性的技术飞跃与进步、 可操作性强的有益效果。
12、 由于本发明以上的各条所述， 从而获得了将生物质变廈 为宝、 开拓生物质化工产业、 开发并合理利用新能源、 为新能源 利用提供技术实施及技术储备、摆脱对传统化石能源的依赖、有 效地保护环境等有益效果。
13、由于本发明的以上各条所述及本发明设定的装置与技术 的有机融合科学合理、 效果稳定可靠， 经具体实施， 从而获得了 生物质冷气化效率可达 80%以上、 气化系统能量利用率达到 94% 以上、气流床气化炉装置中的高温气流床碳转化率达 99. 8 %以上、 整个装置中的碳转化率达到 97%以上、 气化产物为无焦油、 CH4 含量小于 0. 4%、合成气中 CO和 H2的干基组分达到 87%以上的精 制合成气，同时本发明的三段式气流床气化炉装置极大地降低了 析碳反应的发生、有效地防止了金属灰化腐蚀和碱金属腐蚀的发 生， 避免了防止碱金属结渣和落渣堵塞合成气通道， 保障了整个 气化装置的安全、 稳定和高效运行， 便于工程实施应用、 设备投 资成本低、利于广泛推广应用、以及综合经济效益佳等有益效果。 附图说明
图 1为本发明具体实施方式之一的示意图。即三段式气流床 气化炉装置的高温气流床的顶部布置有下行式燃烧器， 炭粉、 热 解气和氧气通过下行式燃烧器进入高温气流床中进行气化反应， 合成气在高温气流床中下行、经过内壁由光管膜式水冷壁构成的 连接通道进入高温换热器中并经过整流缩口整流后上行冷却、再 经过内壁由光管膜式水冷壁构成的连接通道进入低温换热器中 并经整流器整流后下行冷却的示意图。 图中： 高温气流床、 高温 换热器、低温换热器相互分立布置； 高温气流床的局部放大表示 该高温气流床的炉内壁采用敷有耐火材料的膜式水冷壁构成； 高 温换热器设置有整流缩口、 以便对合成气整流而使其均匀分布， 高温换热器的局部放大表示该高温换热器的炉内壁采用光管膜 式水冷壁构成； 高温气流床及高温换热器下端均设置有排渣口； 低温换热器设置有整流器、 以便对合成气整流而使其均匀分布， 低温换热器的局部放大表示该低温换热器的炉内壁采用光管膜 式水冷壁构成， 低温换热器设置有合成气出口。
图 2为本发明具体实施方式之二的示意图。即三段式气流床 气化炉装置的高温气流床的顶部布置有下行式燃烧器， 炭粉、 热 解气和氧气通过下行式燃烧器进入高温气流床中进行气化反应， 合成气在高温气流床中下行、经过整流缩口进入高温换热器中下 行冷却、再经过内壁由光管膜式水冷壁构成的连接通道进入低温 换热器中并经过整流缩口整流后上行冷却的示意图。 图中： 高温 气流床与高温换热器上下相联布置而与低温换热器分立布置； 高 温气流床的局部放大表示该高温气流床的炉内壁采用敷有耐火 材料的膜式水冷壁构成；高温气流床与高温换热器之间设置有整 流缩口、 以便对合成气整流而使其均匀分布； 高温换热器的局部 放大表示该高温换热器的炉内壁采用光管膜式水冷壁构成，高温 换热器下端设置有排渣口； 低温换热器设置有整流缩口、 以便对 合成气整流而使其均勾分布，低温换热器的局部放大表示该低温 换热器的炉内壁采用光管膜式水冷壁构成，低温换热器下端设置 有排渣口而上端设置有合成气出口。
图 3为本发明具体实施方式之三的示意图。即三段式气流床 气化炉装置的高温气流床的下部布置有水平式燃烧器， 炭粉、 热 解气和氧气通过水平式燃烧器进入高温气流床中进行气化反应， 合成气在高温气流床中上行、经过整流缩口进入高温换热器中上 行冷却、再经过内壁由光管膜式水冷壁构成的连接通道进入低温 换热器并经整流器整流后下行冷却的示意图。 图中： 高温气流床 与高温换热器下上相联布置而与低温换热器分立布置； 高温气流 床的局部放大表示该高温气流床的炉内壁采用敷有耐火材料的 膜式水冷壁构成， 高温气流床下端设置有排渣口； 高温气流床与 高温换热器之间设置有整流缩口、以便对合成气整流而使其均匀 分布； 高温换热器的局部放大表示该高温换热器的炉内壁采用光 管膜式水冷壁构成； 低温换热器中设置有整流器、 以便对合成气 整流而使其均匀分布，低温换热器的局部放大表示该低温换热器 的炉内壁采用光管膜式水冷壁构成，低温换热器下端设置有合成 气出口。
图 4为本发明具体实施方式中 "高温气流床" 炉内壁横截面 为圆形的示意图。图中的局部放大表示该高温气流床的炉内壁采 用敷有耐火材料的膜式水冷壁构成。
图 5为本发明具体实施方式中 "高温气流床"炉内壁横截面 为方形的示意图。图中的局部放大表示该高温气流床的炉内壁采 用敷有耐火材料的膜式水冷壁构成。
图 6为本发明具体实施方式中 "高温气流床" 炉内壁横截面 为八角形的示意图。图中的局部放大表示该高温气流床的炉内壁 采用敷有耐火材料的膜式水冷壁构成。
通过图 4、 5、 6的示意， 可根据需要而将 "高温气流床" 的 炉内壁横截面以圆形 /或方形 /或八角形的任意方式进行实施。
图 7为本发明具体实施方式中 "高温换热器及低温换热器" 炉内壁横截面为圆形的示意图。图中的局部放大表示高温换热器 及低温换热器 "炉内壁，， 均采用光管膜式水冷壁构成。
图 8为本发明具体实施方式中 "高温换热器及低温换热器" 炉内壁横截面为方形的示意图。图中的局部放大表示高温换热器 及低温换热器 "炉内壁" 均采用光管膜式水冷壁构成。
图 9为本发明具体实施方式中 "高温换热器及低温换热器" 炉内壁横截面为八角形的示意图。图中的局部放大表示高温换热 器及低温换热器 "炉内壁" 均采用光管膜式水冷壁构成。
通过图 7、 8、 9的示意， 可根据需要而将 "高温换热器及低 温换热器" 的炉内壁横截面以圆形 /或方形 /或八角形的任意组合 方式进行实施。
图 10为本发明具体实施方式中高温换热器的炉内壁采用光 管膜式水冷壁构成、横截面为圆形时、高温换热器中激冷室的 "激 冷水雾化喷嘴" 以 "水平环形雾化喷水" 方式布置的示意图。
图 11为本发明具体实施方式中高温换热器的炉内壁采用光 管膜式水冷壁构成、横截面为方形时、高温换热器中激冷室的 "激 冷水雾化喷嘴" 以 "水平环形雾化喷水" 方式布置的示意图。
图 12为本发明具体实施方式中高温换热器的炉内壁采用光 管膜式水冷壁构成、横截面为八角形时、 高温换热器中激冷室的 "激冷水雾化喷嘴"以 "水平环形雾化喷水"方式布置的示意图。
图 13为本发明具体实施方式中高温换热器的炉内壁采用光 管膜式水冷壁构成、横截面为圆形时、高温换热器中激冷室的 "激 冷水雾化喷嘴" 以 "自上向下雾化喷水 /或自下向上雾化喷水" 方式布置的示意图。即： 当合成气上行时以 "自上向下雾化喷水" 方式布置； 当合成气下行时以 "自下向上雾化喷水" 方式布置。 图 14为本发明具体实施方式中高温换热器的炉内壁采用光 管膜式水冷壁构成、横截面为方形时、高温换热器中激冷室的 "激 冷水雾化喷嘴" 以 "自上向下雾化喷水 /或自下向上雾化喷水" 方式布置的示意图。即： 当合成气上行时以 "自上向下雾化喷水" 方式布置； 当合成气下行时以 "自下向上雾化喷水" 方式布置。
图 15为本发明具体实施方式中高温换热器的炉内壁采用光 管膜式水冷壁构成、横截面为八角形时、 高温换热器中激冷室的 "激冷水雾化喷嘴" 以 "自上向下雾化喷水 /或自下向上雾化喷 水，， 方式布置的示意图。 即： 当合成气上行时以 "自上向下雾化 喷水" 方式布置； 当合成气下行时以 "自下向上雾化喷水" 方 式布置。
图中的标号： 1、 高温气流床， 101、 敷有耐火材料的膜式水 冷壁， 201、 下行式燃烧器， 202、 水平式燃烧器， 301、 连接通 道， 302、 连接通道， 303、 连接通道， 304、 连接通道， 4、 高温 换热器， 401、 光管膜式水冷壁， 5、 激冷室， 6、 高温过热器， 701、 整流缩口， 702、 整流缩口， 703、 整流缩口， 704、 整流缩 口， 8、 低温换热器， 801、 光管膜式水冷壁， 9、 整流器， 10、 低温过热器， 11、 省煤器， 12、 激冷水雾化喷嘴， 131、 落渣口， 132、 落渣口， 133、 落渣口， 134、 落渣口， 135、 落渣口， 141、 合成气出口， 142、 合成气出口， 143、 合成气出口。 具体实施方式一
下面结合说明书附图， 对本发明作详细描述。 正如说明书附 图所示：
一种带余热利用的生物质三段式气流床气化技术，以生物质 为原料， 原料经热解获得固态炭和热解气， 将固态炭研磨后获得 炭粉， 炭粉由热解气 /氮气 /二氧化碳气体输送， 同时采用氧气为 氧化剂， 炭粉、 热解气和氧气通过燃烧器进入气流床中进行气化 反应， 得到高温合成气， 高温合成气的物理热通过气化炉内的换 热器将热量传递给水产生过热蒸汽，高温合成气冷却后流出气化 炉；
①、将所述的带余热利用的气流床气化炉装置分成三段， 分 别为高温气流床、 高温换热器、 低温换热器；
②、在所述高温气流床中，采用固态排渣的气流床气化技术， 所述高温气流床的炉内壁采用敷有耐火材料的膜式水冷壁构成， 所述高温气流床的合成气出口温度在 1280°C ~ 1320°C之间；
③、 在所述高温换热器中， 合成气的入口温度在 1280°C ~ 1320 C之间， 出口温度在 580°C ~ 600°C之间； 所述高温换热器 的炉内壁采用光管膜式水冷壁构成，所述高温换热器中布置有激 冷室和高温过热器， 进入所述激冷室的合成气温度在 1000°C ~ 1100°C之间， 离开所述激冷室激冷后的合成气温度在 700°C ~ 800°C之间；
④、 在所述低温换热器中， 合成气的入口温度在 580°C ~ 600°C之间， 出口温度在 220°C~230°C之间； 所述低温换热器的 炉内壁采用光管膜式水冷壁构成，所述低温换热器中布置有低温 过热器和省煤器。
所述的带余热利用的生物质三段式气流床气化技术， 如图 1 所示，所述三段式气流床气化炉装置的所述高温气流床的顶部布 置有下行式燃烧器， 所述炭粉、热解气和氧气通过所述下行式燃 烧器进入高温气流床中进行气化反应，合成气在高温气流床中下 行、经过内壁由光管膜式水冷壁构成的连接通道进入高温换热器 中并经过整流缩口整流后上行冷却、再经过内壁由光管膜式水冷 壁构成的连接通道进入低温换热器中并经整流器整流后下行冷 却。
所述的带余热利用的生物质三段式气流床气化技术， 如图 2 所示，所述三段式气流床气化炉装置的所述高温气流床的顶部布 置有下行式燃烧器， 所述炭粉、 热解气和氧气通过所述下行式燃 烧器进入高温气流床中进行气化反应，合成气在高温气流床中下 行、 经过整流缩口进入高温换热器中下行冷却、再经过内壁由光 管膜式水冷壁构成的连接通道进入低温换热器中并经过整流缩 口整流后上行冷却。
所述的带余热利用的生物质三段式气流床气化技术， 如图 3 所示，所述三段式气流床气化炉装置的所述高温气流床的下部布 置有水平式燃烧器， 所述炭粉、 热解气和氧气通过所述水平式燃 烧器进入高温气流床中进行气化反应，合成气在高温气流床中上 行、 经过整流缩口进入高温换热器中上行冷却、再经过内壁由光 管膜式水冷壁构成的连接通道进入低温换热器并经整流器整流 后下行冷却。
在实施过程中： 按图 1、 图 2、 图 3所示， 分别进行了实施， 并分别进行了实验性考核。
所述的带余热利用的生物质三段式气流床气化技术，如图 4、 5、 6、 7、 8、 9所示， 所述三段式气流床气化炉装置的炉内壁横 截面为圓形、 方形、 八角形、 圆形 /方形 /八角形任意组合的一种。 在图 4、 5、 6的示意下： 对所述三段式气流床气化炉装置的 "高 温气流床"炉内壁横截面分别以圆形、方形、八角形进行了实施。 在图 7、 8、 9的示意下： 对所述三段式气流床气化炉装置的 "高 温换热器及低温换热器" 炉内壁横截面分别以圆形、 方形、 八角 形、 圆形 /方形 /八角形任意组合的一种进行了实施。
所述的带余热利用的生物质三段式气流床气化技术，如图 1、 2、 3 所示， 在所述的高温换热器中， 所述激冷室以水作为激冷 剂， 所述合成气在激冷室的停留时间在 0.3秒以内。
所述的带余热利用的生物质三段式气流床气化技术， 如图 10、 11、 12、 13、 14、 15 所示， 在所述的高温换热器中， 激冷 室的激冷喷水方式采用自上向下雾化喷水、 或自下向上雾化喷 水、 或水平环形雾化喷水中的一种。 在图 10、 11、 12的示意下： 对高温换热器炉内壁横截面分别为圆形、 方形、 八角形、 圆形 / 方形 /八角形任意组合的一种时，激冷室的激冷喷水方式均以 "水 平环形雾化喷水" 方式布置进行了实施。 在图 13、 14、 15的示 意下： 对高温换热器炉内壁横截面分别为圆形、 方形、 八角形、 圓形 /方形 /八角形任意组合的一种时； 结合图 1所示、 激冷室的 激冷喷水方式以 "自上向下雾化喷水"方式布置进行了实施， 结 合图 2所示、 激冷室的激冷喷水方式以 "自下向上雾化喷水" 方 式布置进行了实施，结合图 3所示、激冷室的激冷喷水方式以 "自 上向下雾化喷水" 方式布置进行了实施。 所述的带余热利用的生物质三段式气流床气化技术，在所述 的高温换热器中，对所述的高温过热器受热面管束采用高压蒸汽 吹扫方式或采用机械振打方式进行除灰。对两种除灰方式分别进 行了实施。
所述的带余热利用的生物质三段式气流床气化技术，如图 1、 2、 3 所示， 所述三段式气流床气化炉装置中在合成气转向处均 采用了整流方法， 使合成气进入下一个环节时保持气流均匀分 布。 具体的说就是图 1、 2、 3中所示的整流缩口及图 1、 3中所 示的整流器。
在上述的具体实施过程中， 生物质原料以薪炭材麻栎为例， 干燥后麻栎的元素分析和特性数据如表 1所示：
干燥后麻栎的元素分析和特性数据表
成分 单位 数值 碳 r % (kg/kg) 40. 41 氢 % (kg/kg) 5. 43 氧 0M % (kg/kg) 39. 46 氮 % (kg/kg) 0. 17 石巟 % (kg/kg) 0.13 氯 % (kg/kg) 0.00 灰分 % (kg/kg) 3.60 水分 ΜΆτ % (kg/kg) 10.8 灰熔点 FT V 1478 低位发热量 LHV MJ/kg 17.87 主要工艺操作条件如下:
( 1 )、所述三段式气流床气化炉装置的合成气侧运行压力为 3.6MPa, 下行式燃烧器 /或水平式燃烧器入口的热解气均为 3.69kg/s, 炭粉 1.2kg/s, 炭粉和热解气的混合温度为 350°C, 氧化剂采用温度为 150°C、 纯度为 99.4%的氧气， 进入高温气流 床的氧气量 1.46kg/s。
( 2 )、 所述三段式气流床气化炉装置的余热利用给水温度 152°C, 给水压力 6. OMPa, 给水量 16.3 T/h。
通过上述的具体实施得到的结果是：
①、 所述三段式气流床气化炉装置的出口合成气总量（不含 激冷水） 为 6.35kg/s， 其中含灰量 0.13kg/s。
②、 合成气出口的合成气中各组分的摩尔体积含量（N2忽略 不计， 不含激冷水）： CO: 38.5%, H2: 29.8%, C02: 9.4%, H20: 21.97%,CH4: 0.328%;其中合成气干基中 CO和 H2的含量占 87.53%;
③、 高温气流床的碳转化率为 99.8%, 三段式气流床气化炉 装置的气化效率 80.2%; ④、 合成气余热利用产生的过热蒸汽压力 5. 29MPa，出口温 度 480°C， 过热蒸汽量 16. 0 T/h。
⑤、 三段式气流床气化炉装置的能量利用效率 94. 30%。
⑥、 经过实验性运行检验， 高温 /低温换热器内的受热面管 束无结渣及腐蚀发生、高压蒸汽吹灰效果良好，合成气通道清洁； 均收到了预期的良好效果。 具体实施方式二
在具体实施方式一实施基础上进行实施， 如图 1所示， 所述 三段式气流床气化炉装置的所述高温气流床的顶部布置有下行 式燃烧器， 所述炭粉、 热解气和氧气通过所述下行式燃烧器进入 高温气流床中进行气化反应，合成气在高温气流床中下行、 经过 内壁由光管膜式水冷壁构成的连接通道进入高温换热器中并经 过整流缩口整流后上行冷却、再经过内壁由光管膜式水冷壁构成 的连接通道进入低温换热器中并经整流器整流后下行冷却。所使 用的生物质原料仍以麻栎（仍见具体实施方式一中的表 1 )为例， 主要工艺操作条件如具体实施方式一。 通过实施得到的结果是：
①、 所述三段式气流床气化炉装置的出口合成气总量（不含 激冷水）为 6. 35kg/s , 其中含灰量 0. 13kg/s。
②、 合成气出口合成气中的各组分的摩尔体积含量（N2忽略 不计， 不含激冷水）： CO: 38. 6%, H2: 29. 7%, C02: 9. 5%, H20: 21. 96%, CH,: 0. 328%;其中合成气干基中 CO和 H2的含量占 87. 53%;
③、 高温气流床的碳转化率为 99. 8%， 三段式气流床气化炉 装置的气化效率 80. 2%;
④、 合成气余热利用产生的过热蒸汽压力 5. 29MPa，出口温 度 480°C， 过热蒸汽量 16. 0 T/h。
⑤、 三段式气流床气化炉装置的能量利用效率 94. 31%。
⑥、 经过实验性运行检验， 高温 /低温换热器内的受热面管 束无结渣及腐蚀发生、高压蒸汽吹灰效果良好，合成气通道清洁； 同样获得了预期良好效果。 具体实施方式三
仍在具体实施方式一实施基础上进行实施， 如图 2所示， 只 是：所述三段式气流床气化炉装置的所述高温气流床的顶部布置 有下行式燃烧器， 所述炭粉、 热解气和氧气通过所述下行式燃烧 器进入高温气流床中进行气化反应， 合成气在高温气流床中下 行、 经过整流缩口进入高温换热器中下行冷却、再经过内壁由光 管膜式水冷壁构成的连接通道进入低温换热器中并经过整流缩 口整流后上行冷却。 所使用的生物质原料仍以麻栎（仍见具体实 施方式一中的表 1 )为例，主要工艺操作条件如具体实施方式一。 通过实施得到的结果是：
①、 所述三段式气流床气化炉装置的出口合成气总量（不含 激冷水） 为 6. 35kg/s , 其中含灰量 0. 13kg/s。
② 合成气出口合成气中的各组分的摩尔体积含量（N2忽略 不计， 不含激冷水）： CO: 38. 4%, H2: 29. 9%， C02: 9. 5%， H20: 21. 96%, CH4: 0. 328%;其中合成气干基中 CO和 H2的含量占 87. 53%; ③、 高温气流床的碳转化率为 99. 75% , 三段式气流床气化 炉装置的气化效率 80. 15%;
④、 合成气余热利用产生的过热蒸汽压力 5. 29MPa,出口温 度 480 °C， 过热蒸汽量 16. 0 T/h。
⑤、 三段式气流床气化炉装置的能量利用效率 94. 23%。
⑥、 经过实验性运行检验， 高温 /低温换热器内的受热面管 束无结渣及腐蚀发生、高压蒸汽吹灰效果良好，合成气通道清洁； 同样获得了预期良好效果。 具体实施方式四
仍在具体实施方式一实施基础上进行实施， 如图 3所示， 只 是：所述三段式气流床气化炉装置的所述高温气流床的下部布置 有水平式燃烧器， 所述炭粉、 热解气和氧气通过所述水平式燃烧 器进入高温气流床中进行气化反应， 合成气在高温气流床中上 行、 经过整流缩口进入高温换热器中上行冷却、再经过内壁由光 管膜式水冷壁构成的连接通道进入低温换热器并经整流器整流 后下行冷却。 所使用的生物质原料仍以麻栎（仍见具体实施方式 一中的表 1 )为例， 主要工艺操作条件如具体实施方式一。 通过 实施得到的结杲是：
①、 所述三段式气流床气化炉装置的出口合成气总量（不含 激冷水）为 6. 35kg/ s , 其中含灰量 0. 13kg/ s。
②、 合成气出口合成气中的各组分的摩尔体积含量（N2忽略 不计， 不含激冷水）： CO: 38. 6%, H2: 29. 7%, C02: 9. 5%, H20: 21. 87 , CH4: 0. 329%;其中合成气干基中 CO和 H2的含量占 87. 53%;
③、 高温气流床的碳转化率为 99. 8%， 三段式气流床气化炉 装置的气化效率 80. 2%;
④、 合成气余热利用产生的过热蒸汽压力 5. 29MPa，出口温 度 480°C， 过热蒸汽量 16. 0 T/h。
⑤、 三段式气流床气化炉装置的能量利用效率 94. 30%。
⑥、 经过实验性运行检验， 高温 /低温换热器内的受热面管 束无结渣及腐蚀发生， 高温换热器内采用高压蒸汽吹灰效果良 好，低温换热器内采用机械振打除灰同样良好，合成气通道清洁； 同样获得了预期良好效果。 以上所述仅为本发明的较佳实施例，并非对本发明作任何形 式上的限制； 凡本行业的普通技术人员， 均可按以上所述和说明 书附图所示而顺畅地实施本发明；但凡在不脱离本发明技术方案 而作出的更动、 爹饰与演变的等同变化， 均为本发明的等效实施 例， 均仍属于本发明技术方案的保护范围。

Claims

权 利 要 求 书
1、 一种带余热利用的生物质三段式气流床气化技术， 以生 物质为原料， 原料经热解获得固态炭和热解气， 将固态炭研磨后 获得炭粉， 炭粉由热解气 /氮气 /二氧化碳气体输送， 同时采用氧 气为氧化剂， 炭粉、 热解气和氧气通过燃烧器进入气流床中进行 气化反应， 得到高温合成气， 高温合成气的物理热通过气化炉内 的换热器将热量传递给水产生过热蒸汽，高温合成气冷却后流出 气化炉， 其特征在于：
①、将所述的带余热利用的气流床气化炉装置分成三段， 分 别为高温气流床、 高温换热器、 低温换热器；
②、在所述高温气流床中，采用固态排渣的气流床气化技术， 所述高温气流床的炉内壁采用敷有耐火材料的膜式水冷壁构成， 所述高温气流床的合成气出口温度在 1280 °C ~ 1320 °C之间；
③、 在所述高温换热器中， 合成气的入口温度在 1280°C ~ 1320°C之间， 出口温度在 580°C ~ 600°C之间； 所述高温换热器 的炉内壁采用光管膜式水冷壁构成，所述高温换热器中布置有激 冷室和高温过热器， 进入所述激冷室的合成气温度在 1000°C ~ 1100°C之间， 离开所述激冷室激冷后的合成气温度在 700°C ~ 800°C之间；
④、 在所述低温换热器中， 合成气的入口温度在 580°C ~ 600°C之间， 出口温度在 220°C〜230°C之间； 所述低温换热器的 炉内壁采用光管膜式水冷壁构成，所述低温换热器中布置有低温 过热器和省煤器。
2、 根据权利要求 1所述的带余热利用的生物质三段式气流 床气化技术， 其特征在于： 所述三段式气流床气化炉装置的所述 高温气流床的顶部布置有下行式燃烧器， 所述炭粉、 热解气和氧 气通过所述下行式燃烧器进入高温气流床中进行气化反应，合成 气在高温气流床中下行、经过内壁由光管膜式水冷壁构成的连接 通道进入高温换热器中并经过整流缩口整流后上行冷却、再经过 内壁由光管膜式水冷壁构成的连接通道进入低温换热器中并经 整流器整流后下行冷却。
3、 根据权利要求 1所述的带余热利用的生物质三段式气流 床气化技术， 其特征在于： 所述三段式气流床气化炉装置的所述 高温气流床的顶部布置有下行式燃烧器， 所述炭粉、 热解气和氧 气通过所述下行式燃烧器进入高温气流床中进行气化反应，合成 气在高温气流床中下行、经过整流缩口进入高温换热器中下行冷 却、再经过内壁由光管膜式水冷壁构成的连接通道进入低温换热 器中并经过整流缩口整流后上行冷却。
4、 根据权利要求 1所述的带余热利用的生物质三段式气流 床气化技术， 其特征在于： 所述三段式气流床气化炉装置的所述 高温气流床的下部布置有水平式燃烧器， 所述炭 4分、 热解气和氧 气通过所述水平式燃烧器进入高温气流床中进行气化反应，合成 气在高温气流床中上行、经过整流缩口进入高温换热器中上行冷 却、再经过内壁由光管膜式水冷壁构成的连接通道进入低温换热 器并经整流器整流后下行冷却。
5、 根据权利要求 1或 2或 3或 4所述的带余热利用的生物 质三段式气流床气化技术， 其特征在于： 所述三段式气流床气化 炉装置的炉内壁横截面为圆形、 方形、 八角形、 圆形 /方形 /八角 形任意组合的一种。
6、 根据权利要求 1或 2或 3或 4所述的带余热利用的生物 质三段式气流床气化技术，其特征在于：在所述的高温换热器中， 所述激冷室以水作为激冷剂，所述合成气在激冷室的停留时间在 0.3秒以内。
7、 才艮据权利要求 1或 2或 3或 4所述的带余热利用的生物 质三段式气流床气化技术，其特征在于：在所述的高温换热器中， 激冷室的激冷喷水方式采用自上向下雾化喷水、或自下向上雾化 喷水、 或水平环形雾化喷水中的一种。
8、 根据权利要求 1或 2或 3或 4所述的带余热利用的生物 质三段式气流床气化技术，其特征在于：在所述的高温换热器中， 对所述的高温过热器受热面管束采用高压蒸汽吹扫方式或采用 机械振打方式进行除灰。
9、 根据权利要求 1或 2或 3或 4所述的带余热利用的生物 质三段式气流床气化技术， 其特征在于： 所述三段式气流床气化 炉装置中在合成气转向处均采用了整流方法，使合成气进入下一 个环节时保持气流均匀分布。
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