CN110760342B - Boiler starting method of circulating fluidized bed boiler - Google Patents

Boiler starting method of circulating fluidized bed boiler Download PDF

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CN110760342B
CN110760342B CN201810826363.9A CN201810826363A CN110760342B CN 110760342 B CN110760342 B CN 110760342B CN 201810826363 A CN201810826363 A CN 201810826363A CN 110760342 B CN110760342 B CN 110760342B
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gas
pressure
furnace
gasification
valve
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CN110760342A (en
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张刚
刘海建
霍学斌
吴松怡
隋盈鑫
李军明
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Xinneng Energy Co Ltd
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Xinneng Energy Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/726—Start-up
    • 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
    • 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
    • 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
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • 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
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • 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
    • 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

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Industrial Gases (AREA)

Abstract

The invention discloses a method for starting a circulating fluidized bed gasification furnace, which comprises a furnace baking temperature rise and pressure rise stage, a bed building preparation stage, a bed building stage and a synthetic gas treatment stage. The method has the advantages that when the method is used for starting the gasifier, the temperature and pressure raising processes of the gasifier are carried out simultaneously, so that the problem that the temperature and pressure raising processes can not be carried out simultaneously in the traditional gasifier starting method is solved; the mixed gas without heating treatment is used as the pulverized coal conveying gas and the fluidizing agent, so that the pulverized coal in the gasification furnace can maintain a better fluidizing state, the occurrence of slag bonding accidents of the gasification furnace is avoided, the temperature and pressure rise process is shortened, the start time is short, the unqualified synthetic gas amount is low, the resource waste is reduced, and the environmental protection load of enterprises is lightened; the temperature rise process mainly depends on the oven gas, the oven gas has high thermal efficiency, the ignition coal powder consumption is reduced, and the production cost of enterprises is reduced.

Description

Boiler starting method of circulating fluidized bed boiler
The technical field is as follows:
the invention relates to the field of coal chemical industry, in particular to a method for starting a circulating fluidized bed gasification furnace.
Background art:
at present, three fluidized bed gasification processes, namely coal pressurized catalytic gasification, ash agglomeration and U-gas, are adopted, a traditional three-stage furnace starting mode of furnace heating, material feeding and bed building and system pressure boosting is adopted, and the heating and pressure boosting processes are carried out strictly according to requirements. The traditional furnace starting mode has the following problems: 1. and (3) oven drying: in the traditional method, flue gas generated after combustion of liquefied petroleum gas or natural gas is used as a heat source for baking the furnace, the temperature of the furnace is increased to 850 ℃ from room temperature for about 24 hours, and the time consumption in the temperature increasing process is long; 2. feeding and bed building processes: after the temperature of the furnace rises to 580 ℃, introducing a gasifying agent into the furnace and adding coal powder, wherein the coal powder directly reduces the temperature of the furnace after being added into the furnace due to low temperature of the coal powder, so that the coal gasification reaction cannot be normally carried out; therefore, part of the pulverized coal input at this stage is combusted to increase the furnace temperature, and the other part of the pulverized coal participates in the gasification reaction, but because the furnace temperature and the furnace pressure can not meet the gasification reaction requirement, the pulverized coal is not completely gasified and can only be discharged out of the furnace along with the synthesis gas, the synthesis gas has low quality and high oxygen content, cannot enter the subsequent working section and is sent to a torch for treatment, so the pulverized coal is easy to explode, and can only be discharged into the atmosphere, thereby the resources are seriously wasted, and the environment is polluted; 3. and (3) boosting: before the boosting process starts, equipment and pipelines need to be heated and tightened to ensure the air tightness of the equipment and the pipelines, then the pressure is gradually increased from the normal pressure to a preset pressure value according to the actual condition, and as the fluidized state of furnace burden in a furnace is violently changed at the boosting key point (generally 1.0MPa, 2.0MPa and 3.0MPa), once the conditions of unstable flow pattern or local overtemperature and the like are generated, the slag bonding accident of the gasification furnace can be caused; therefore, when the pressure rises from one pressure key point to another pressure key point, the pressure rising rate is required to be gradually reduced, and the time duration of maintaining after reaching the higher pressure key point is also required to be continuously increased so as to ensure that the temperature and the pressure of the bed in the fluidized bed gasification furnace are in a controllable range and have a better fluidization state; therefore, the boosting process lasts a long time, typically several days. The problems are more obvious along with the increase of the volume of the circulating fluidized bed gasification furnace, and comprehensively, the problems of long operation period, serious resource waste, complicated flow, high difficulty and serious environmental pollution exist in the starting process of the traditional circulating flow bed gasification furnace.
The invention content is as follows:
the invention aims to provide a furnace starting method of a circulating fluidized bed gasification furnace, which has the advantages of short operation period, resource waste reduction, operation difficulty reduction and environmental pollution relief.
The purpose of the invention is implemented by the following technical scheme: a method for starting a circulating fluidized bed gasifier comprises the steps of firstly, introducing preheating oven gas into a gasifier system to carry out temperature rise and pressure rise operation on the gasifier system, enabling the preheating oven gas to pass through the gasifier system to obtain circulating gas, mixing and recycling part of the circulating gas with the preheating oven gas through a compressor in the temperature rise and pressure rise operation process, controlling the temperature rise and pressure rise rate of the gasifier until the furnace top temperature T of the gasifier is reached4Is lifted to T4650 ℃ at 450-3Lifting to P of 2.0MPa or less3Less than 3.5 MPa; and then, stopping mixing part of the circulating gas with the preheating furnace drying gas, starting to convey pulverized coal into the gasification furnace, taking the circulating gas as the conveying gas of the pulverized coal, starting to convey a gasifying agent into the gasification furnace when the thickness of the bed layer in the gasification furnace is 2m, and treating the synthetic gas generated by the gasification furnace.
Further, the method specifically comprises the following steps:
a furnace baking temperature rise and pressure rise stage: conveying the oven gas to a preheater through an oven gas pipeline, and heating to 100 ℃ to obtain preheated oven gas; opening a distribution plate valve and a central pipe valve, conveying the preheated oven gas into a distribution plate gasification agent pipeline and a central pipe gasification agent pipeline respectively, and increasing the internal temperature of the gasification furnace and the cyclone separator through the preheated oven gas; the preheating oven gas after heat exchange with the gasification furnace and the cyclone separator is subjected to dust removal by a dust remover and heat recovery by a waste heat boiler to obtain circulating gas; starting a circulating gas valve, conveying the circulating gas to the oven gas pipeline through a compressor to be mixed with the oven gas, wherein the mixing volume ratio of the circulating gas to the oven gas is 1-2: 10, obtaining mixed gas; the mixed gas is conveyed into the preheater and heated to 100 ℃ to obtain preheated mixed gas, and the preheated mixed gas enters the gasification furnace and the cyclone separator through the distribution plate gasification agent pipeline and the central pipe gasification agent pipeline respectively to raise the internal temperature of the gasification furnace and the cyclone separator; repeating the operation, gradually increasing the temperature of the preheated mixed gas by controlling the heat medium inlet amount of the preheater and the delivery amount of the mixed gas, and controlling the temperature rise rate in the gasification furnace to be 25 ℃/h and the pressure rise rate to be 0.2 MPa/h; until the furnace top temperature T of the gasification furnace4Is lifted to T4650 ℃ at 450-3Lifting to P of 2.0MPa or less3If the pressure is less than 3.5MPa, the temperature and pressure raising stage of the oven is finished;
bed building preparation stage: after the temperature and pressure raising stage of the drying oven is completed, closing a circulating gas valve, continuously conveying the preheated drying oven gas into the gasification oven through the distribution plate gasification agent pipeline, and continuously conveying the circulating gas into the gasification oven through the central pipe gasification agent pipeline; charging the interior of a coal lock, when the internal pressure of the coal lock is at least 200KPa higher than the internal pressure of the gas chamber of the gasification furnace, opening a coal outlet valve, a coal inlet valve and a pulverized coal conveying gas valve, taking the circulating gas as pulverized coal conveying gas, adjusting the opening of the pulverized coal conveying gas valve, keeping the internal pressure of a pulverized coal pipeline 10-50KPa higher than the internal pressure of the gas chamber of the gasification furnace, and completing the bed building preparation stage;
a bed building stage: after the bed building preparation stage is completed, when the furnace top temperature T is reached4Is lifted to T4600 ℃, said furnace top pressure P3Lifting to P less than or equal to 3.0MPa3When the pressure is less than 3.5MPa, conveying pulverized coal into the gasification furnace through a coal bunker and the coal lock, and when the thickness of the bed layer in the gasification furnace is 2m, conveying gasification agent into the gasification furnace through the distribution plate gasification agent pipeline and the central pipe gasification agent pipeline, and controlling the temperature rise rate of the gasification furnace to be 30-60 ℃/h and the pressure rise rate to be 0.2-0.3 MPa/h; in this process, the recycle gas acts as a fluidizing agent and stabilizes the furnace top temperature T4Maintaining the fluidization state of the coal dust in the gasification furnace by using the preheating oven gas as a fluidizing agent at 600 ℃; when the thickness of the bed layer in the gasification furnace is continuously increased, closing the distribution plate valve and the central pipe valve, and stopping conveying the preheating oven gas and the circulating gas;
and (3) a synthesis gas treatment stage: in the bed building stage, after the circulating gas valve is closed, in order to maintain the furnace top pressure P3The synthesis gas produced by the gasification furnace needs to be treated; when the synthetic gas line pressure P5When the pressure is higher than 8.0MPa, opening an emptying valve to empty the synthesis gas; when the oxygen content of the synthesis gas is more than 0.1 percent, the pressure P of the synthesis gas pipeline5When the process design pressure is less than the process design pressure, closing the emptying valve, opening a flare valve, and sending the synthesis gas to a flare treatment system through a flare pipeline;when the oxygen content of the synthesis gas is less than or equal to 0.1 percent and the pressure P of the synthesis gas pipeline5And when the process design pressure is not less than the process design pressure, closing the torch valve and opening the crude gas valve, and conveying the synthesis gas to a methanol synthesis working section through a qualified gas pipeline.
Further, the oven gas is any one or combination of nitrogen or carbon dioxide, and when the oven gas comprises the nitrogen and the carbon dioxide, the nitrogen and the carbon dioxide can be mixed according to any proportion.
The invention has the advantages that: 1. the heating and boosting processes of the gasification furnace are carried out simultaneously, so that the problems that the heating and boosting can not be carried out simultaneously, the furnace starting time is long, the ignition coal is wasted much, the environmental pollution is serious and the heat efficiency is low in the traditional gasification furnace starting method are solved; in the invention, the furnace top temperature T of the gasification furnace is firstly measured4Raising the temperature to over 450 ℃ and the furnace top pressure P3Increasing the pressure to 2.0MPa or less P3Less than 3.5MPa, and preparation is made for adding the coal powder; then the furnace top temperature T is measured4Rise to T4600 ℃ and furnace top pressure P3Increasing the pressure to be less than or equal to 3.0MPa and less than or equal to P3If the pressure is less than 3.5MPa, adding pulverized coal to build a bed layer; in the process, the temperature and pressure rise are fast, the reason is that the high-temperature and high-pressure condition is firstly formed in the gasifier, then the coal powder is conveyed, under the high-temperature and high-pressure condition, the gas-phase density in the unit volume in the gasifier is increased, the contact probability of the gasifying agent and the coal powder is increased, further the gasification reaction of the coal powder is accelerated, the coal powder is enabled to react rapidly to release a large amount of heat, the temperature rise and pressure rise process is accelerated, and the temperature rise, the pressure rise and the feeding can be carried out simultaneously; 2. The heating process mainly depends on the oven gas, the oven gas is heated by the preheater and then enters the gasification furnace and the cyclone separator for heat exchange, and the oven gas after heat exchange is treated by the flue gas purification system and then is recycled by the flue gas circulation system, so that the heat efficiency of the oven gas is improved, the ignition coal powder consumption is reduced, the resources are saved, and the production cost of enterprises is reduced; 3. the temperature and pressure rising process is shortened, the unqualified synthesis gas amount generated in the temperature and pressure rising process is reduced, the resource waste is reduced, only part of unqualified synthesis gas with high oxygen content is discharged, and the rest unqualified synthesis gas with low oxygen content can be sent to a torch for treatment, so that the environmental protection load of enterprises is reduced; 4. so as not to be heatedThe mixed gas is used as the coal powder conveying gas and the fluidizing agent, so that the coal powder in the gasification furnace can maintain a better fluidized state, the occurrence of slag bonding accidents of the gasification furnace is avoided, and the pressure boosting process is shortened.
Description of the drawings:
in order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic view of example 1.
1 part of gasification furnace, 1 part of furnace top temperature sensor, 1 part of furnace bottom temperature sensor, 1 part of gas chamber, 1 part of furnace body pressure sensor, 1 part of gas chamber pressure sensor, 1 part of furnace top pressure sensor, 1 part of distribution plate gasification agent pipeline, 1 part of central pipe gasification agent pipeline, 1 part of distribution plate gasification agent pressure sensor, 1 part of central pipe gasification agent pressure sensor, 1 part of coal inlet system, 2 part of coal bunker, 2 part of coal lock, 2 part of coal powder pipeline, 2 part of coal outlet valve, 2 part of coal inlet valve, 2 part of coal drying gas system, 3 part of furnace drying gas pipeline, 3 part of preheater, 3 part of heat medium pipeline, 3 part of furnace drying gas valve, 3-5 parts of oven gas pressure sensor, 3-6 parts of inlet gas temperature sensor, 3-7 parts of heat medium valve, 3-8 parts of distribution plate valve, 3-9 parts of central pipe valve, 4 parts of flue gas purification system, 4-1 parts of cyclone separator, 4-2 parts of dust remover, 4-3 parts of waste heat boiler, 4-4 parts of flue gas pressure sensor, 4-5 parts of synthesis gas temperature sensor, 4-6 parts of return material pipeline, 4-7 parts of return material pressure sensor, 4-8 parts of return material temperature sensor, 4-9 parts of synthesis gas pipeline, 4-10 parts of qualified gas pipeline, 4-11 parts of torch pipeline, 4-12 parts of vent pipeline, 4-13 parts of synthesis gas pressure sensor, 4-14 parts of crude gas valve, 4-15 parts of torch valve, 4-16 parts of vent valve, 5 parts of flue gas circulation system and 5-1 parts of compressor, 5-2 parts of circulating gas pipeline, 5-3 parts of circulating gas valve, 5-4 parts of coal powder conveying gas valve and 5-5 parts of circulating gasification valve.
The specific implementation mode is as follows:
example 1:
as shown in fig. 1, the start-up system of the circulating fluidized bed gasification furnace comprises a gasification furnace 1, a coal feeding system 2, a furnace baking gas system 3, a flue gas purification system 4 and a flue gas circulation system 5,
the upper part, the middle part and the lower part of the furnace body of the gasification furnace 1 are respectively provided with a furnace top temperature sensor 1-1, a furnace temperature sensor 1-2 and a furnace bottom temperature sensor 1-3, the gas chamber 1-4 of the gasification furnace 1 and the furnace body above the gas chamber are respectively provided with a furnace body pressure sensor 1-5 and a gas chamber pressure sensor 1-6, and the top of the furnace body of the gasification furnace 1 is provided with a furnace top pressure sensor 1-7; the gasification furnace 1 comprises distribution plate gasification agent pipelines 1-8 and central pipe gasification agent pipelines 1-9, wherein distribution plate gasification agent pressure sensors 1-10 are arranged on the distribution plate gasification agent pipelines 1-8, and central pipe gasification agent pressure sensors 1-11 are arranged on the central pipe gasification agent pipelines 1-9.
The coal feeding system 2 comprises a coal bunker 2-1, a coal lock 2-2 and a coal powder pipeline 2-3, an outlet of the coal bunker 2-1 is connected with an inlet of the coal lock 2-2 through a lower coal valve 2-4, an outlet of the coal lock 2-2 is connected with the coal powder pipeline 2-3, a coal outlet valve 2-5 and a coal feeding valve 2-6 are sequentially arranged on the coal powder pipeline 2-3, and the coal lock 2-2 of the coal feeding system 2 is connected with a coal powder inlet of the gasification furnace 1 through the coal powder pipeline 2-3.
The oven gas system 3 comprises an oven gas pipeline 3-1, a preheater 3-2 and a heat medium pipeline 3-3, an oven gas valve 3-4 is arranged at the gas inlet end of the oven gas pipeline 3-1, the outlet of the oven gas pipeline 3-1 is connected with the gas inlet of the preheater 3-2, an oven gas pressure sensor 3-5 is arranged at the outlet of the preheater 3-2, the heat medium inlet of the preheater 3-2 is connected with the outlet of the heat medium pipeline 3-3, an inlet gas temperature sensor 3-6 is sequentially arranged on the heat medium pipeline 3-3, 3-7 of a heat medium valve, 3-2 of an outlet of a preheater of the oven gas system 3 is connected with 1-8 of a distribution plate gasifying agent pipeline through a distribution plate valve 3-8, and 3-2 of the outlet of the preheater is also connected with 1-9 of a central tube gasifying agent pipeline through a central tube valve 3-9.
The flue gas purification system 4 comprises a cyclone separator 4-1, a dust remover 4-2 and a waste heat boiler 4-3, wherein a flue gas pressure sensor 4-4 is arranged at an outlet of the cyclone separator 4-1, an outlet of the cyclone separator 4-1 is connected with an inlet of the dust remover 4-2, an outlet of the dust remover 4-2 is connected with an inlet of the waste heat boiler 4-3, a synthetic gas temperature sensor 4-5 is arranged at an outlet of the waste heat boiler 4-3, and the cyclone separator 4-1 of the flue gas purification system 4 is communicated with a flue gas outlet of the gasification furnace 1; the material returning port of the cyclone separator 4-1 is connected with the material returning port of the gasification furnace 1 through a material returning pipeline 4-6, and a material returning pressure sensor 4-7 and a material returning temperature sensor 4-8 are sequentially arranged on the material returning pipeline 4-6.
The outlet of the waste heat boiler 4-3 is also connected with the inlet of a synthetic gas pipeline 4-9, the outlet of the synthetic gas pipeline 4-9 is respectively connected with a qualified gas pipeline 4-10, a torch pipeline 4-11 and an emptying pipeline 4-12, a synthetic gas pressure sensor 4-13 is arranged on the synthetic gas pipeline 4-9, a crude gas valve 4-14 is arranged on the qualified gas pipeline 4-10, a torch valve 4-15 is arranged on the torch pipeline 4-11, and an emptying valve 4-16 is arranged on the emptying pipeline 4-12.
An outlet of a waste heat boiler 4-3 of the flue gas purification system 4 is connected with an inlet of a compressor 5-1 of a flue gas circulating system 5, the flue gas circulating system 5 comprises the compressor 5-1 and a circulating gas pipeline 5-2, and an outlet of the compressor 5-1 is connected with an inlet of the circulating gas pipeline 5-2; an outlet of a circulating gas pipeline 5-2 of the flue gas circulating system 5 is respectively connected with a furnace gas pipeline 3-1, a coal powder pipeline 2-3 and a distributing plate gasifying agent pipeline 1-8, a circulating gas valve 5-3 is arranged on a pipeline between the outlet of the circulating gas pipeline 5-2 and the furnace gas pipeline 3-1, a coal powder gas delivery and supply valve 5-4 is arranged on a pipeline between the outlet of the circulating gas pipeline 5-2 and the coal powder pipeline 2-3, and a circulating gasifying valve 5-5 is arranged on a pipeline between the outlet of the circulating gas pipeline 5-2 and the distributing plate gasifying agent pipeline 1-8.
Example 2:
the method for starting the circulating fluidized bed gasification furnace in the embodiment 1 specifically comprises the following steps:
a furnace baking temperature rise and pressure rise stage: the oven gas is nitrogen; conveying the oven gas into a preheater 3-2 through an oven gas pipeline 3-1, and heating to 100 ℃ to obtain preheated oven gas; opening a distribution plate valve 3-8 and a central pipe valve 3-9, conveying preheated oven gas into a distribution plate gasifying agent pipeline 1-8 and a central pipe gasifying agent pipeline 1-9 respectively, and increasing the internal temperature of the gasification furnace 1 and the cyclone separator 4-1 through the preheated oven gas; the preheated oven gas after heat exchange with the gasification furnace 1 and the cyclone separator 4-1 is subjected to dust removal by a dust remover 4-2 and heat recovery by a waste heat boiler 4-3 in sequence to obtain circulating gas; opening circulating air valve 5-3 to circulateThe gas is conveyed to a baking furnace gas pipeline 3-1 through a compressor 5-1 to be mixed with the baking furnace gas, and the mixing volume ratio of the circulating gas to the baking furnace gas is 1: 10, obtaining mixed gas; the mixed gas is conveyed into a preheater 3-2 and heated to 100 ℃ to obtain preheated mixed gas, the preheated mixed gas is respectively conveyed into a distribution plate gasifying agent pipeline 1-8 and a central pipe gasifying agent pipeline 1-9, and the internal temperatures of the gasification furnace 1 and the cyclone separator 4-1 are improved through the preheated mixed gas; repeating the operation, and controlling the temperature rise rate of the interior of the gasification furnace 1 to be 25 ℃/h and the pressure rise rate to be 0.2MPa/h by controlling the heat medium inlet amount of the preheater 3-2 and the delivery amount of the mixed gas; until the furnace top temperature T of the gasification furnace 14Is lifted to T4450 ℃ and the furnace top pressure P3Is lifted to P32.0MPa, finishing the stage of heating and boosting the furnace;
bed building preparation stage: after the temperature and pressure raising stage of the oven is completed, closing the circulating gas valve 5-3, continuously conveying preheated oven gas into the gasification furnace 1 through the distribution plate gasification agent pipeline 1-8, and continuously conveying circulating gas into the gasification furnace 1 through the central pipe gasification agent pipeline 1-9; when the internal pressure of the coal lock 2-2 is 200KPa higher than the internal pressure of the air chamber 1-4 of the gasification furnace 1, opening the coal outlet valve 2-5, the coal inlet valve 2-6 and the coal powder delivery valve 5-4, taking the circulating gas as the coal powder delivery gas, adjusting the opening of the coal powder delivery valve 5-4, keeping the internal pressure of the coal powder pipeline 2-3 higher than the internal pressure of the air chamber 1-4 of the gasification furnace 1 by 10KPa, and completing the bed building preparation stage;
a bed building stage: after the bed building preparation stage is finished, when the temperature T of the furnace top is reached4Is lifted to T4600 ℃, furnace top pressure P3Is lifted to P3When the pressure is 3.0MPa, delivering pulverized coal into the gasification furnace 1 through the coal bunker 2-1 and the coal lock 2-2, and delivering a gasification agent into the gasification furnace 1 through the distribution plate gasification agent pipelines 1-8 and the central pipe gasification agent pipelines 1-9 when the thickness of the bed layer in the gasification furnace 1 is 2m, wherein the temperature rise rate of the gasification furnace 1 is controlled to be 30 ℃/h, and the pressure rise rate is controlled to be 0.2 MPa/h; in this process, the circulating gas acts as a fluidizing agent and stabilizes the furnace top temperature T4The preheated furnace gas is used as a fluidizing agent to maintain the fluidization state of the coal powder in the gasification furnace 1 at 600 ℃; to the bed in the gasifier 1When the thickness is continuously increased, closing the distribution plate valve 3-8 and the central pipe valve 3-9, and stopping conveying the preheating oven gas and the circulating gas;
and (3) a synthesis gas treatment stage: in the bed building stage, after the circulating gas valve 5-3 is closed, the pressure P of the furnace top is maintained3The synthesis gas produced by the gasification furnace 1 needs to be treated; when the pressure P of the synthesis gas line is 4-95When the pressure is higher than 8.0MPa, opening an emptying valve 4-16 to perform emptying treatment on the synthesis gas; when the oxygen content of the synthesis gas is more than 0.1 percent and the pressure P of the synthesis gas pipeline is 4-95When the pressure is less than 8.0MPa, closing the emptying valve 4-16, opening the flare valve 4-15, and sending the synthetic gas to a flare treatment system through a flare pipeline 4-11; when the oxygen content of the synthesis gas is less than or equal to 0.1 percent and the pressure P of the synthesis gas line is 4-95And when the pressure is more than or equal to 2.5MPa, closing the torch valve 4-15, opening the crude gas valve 4-14, and conveying the synthesis gas to the methanol synthesis section through the qualified gas pipeline 4-10.
Example 3:
the method for starting the circulating fluidized bed gasification furnace in the embodiment 1 specifically comprises the following steps:
a furnace baking temperature rise and pressure rise stage: the oven gas is carbon dioxide; conveying the oven gas into a preheater 3-2 through an oven gas pipeline 3-1, and heating to 100 ℃ to obtain preheated oven gas; opening a distribution plate valve 3-8 and a central pipe valve 3-9, conveying preheated oven gas into a distribution plate gasifying agent pipeline 1-8 and a central pipe gasifying agent pipeline 1-9 respectively, and increasing the internal temperature of the gasification furnace 1 and the cyclone separator 4-1 through the preheated oven gas; the preheated oven gas after heat exchange with the gasification furnace 1 and the cyclone separator 4-1 is subjected to dust removal by a dust remover 4-2 and heat recovery by a waste heat boiler 4-3 in sequence to obtain circulating gas; opening a circulating air valve 5-3, conveying circulating air to a drying furnace air pipeline 3-1 through a compressor 5-1 to be mixed with the drying furnace air, wherein the mixing volume ratio of the circulating air to the drying furnace air is 1.5: 10, obtaining mixed gas; the mixed gas is conveyed into a preheater 3-2 and heated to 100 ℃ to obtain preheated mixed gas, the preheated mixed gas is respectively conveyed into a distribution plate gasifying agent pipeline 1-8 and a central pipe gasifying agent pipeline 1-9, and the internal temperatures of the gasification furnace 1 and the cyclone separator 4-1 are improved through the preheated mixed gas; repeating the above operation by controllingControlling the heat medium inlet amount and the mixed gas conveying amount of the heat exchanger 3-2, and controlling the temperature rise rate of the inside of the gasification furnace 1 to be 25 ℃/h and the pressure rise rate to be 0.2 MPa/h; until the furnace top temperature T of the gasification furnace 14Is lifted to T4500 ℃ and the top pressure P3Is lifted to P3Finishing the furnace heating and boosting stage under the pressure of 3.0 MPa;
bed building preparation stage: after the temperature and pressure raising stage of the oven is completed, closing the circulating gas valve 5-3, continuously conveying preheated oven gas into the gasification furnace 1 through the distribution plate gasification agent pipeline 1-8, and continuously conveying circulating gas into the gasification furnace 1 through the central pipe gasification agent pipeline 1-9; when the internal pressure of the coal lock 2-2 is increased by 500KPa until the internal pressure of the coal lock 2-2 is higher than the internal pressure of the air chamber 1-4 of the gasification furnace 1, opening a coal outlet valve 2-5, a coal inlet valve 2-6 and a coal powder conveying gas valve 5-4, taking circulating gas as coal powder conveying gas, adjusting the opening degree of the coal powder conveying gas valve 5-4, keeping the internal pressure of the coal powder pipeline 2-3 higher than the internal pressure of the air chamber 1-4 of the gasification furnace 1 by 30KPa, and completing a bed building preparation stage;
a bed building stage: after the bed building preparation stage is finished, when the temperature T of the furnace top is reached4Is lifted to T4600 ℃, furnace top pressure P3Is lifted to P3When the pressure is 3.2MPa, delivering pulverized coal into the gasification furnace 1 through the coal bunker 2-1 and the coal lock 2-2, and delivering a gasification agent into the gasification furnace 1 through the distribution plate gasification agent pipelines 1-8 and the central pipe gasification agent pipelines 1-9 when the thickness of the bed layer in the gasification furnace 1 is 2m, wherein the temperature rise rate of the gasification furnace 1 is controlled to be 40 ℃/h, and the pressure rise rate is controlled to be 0.25 MPa/h; in this process, the circulating gas acts as a fluidizing agent and stabilizes the furnace top temperature T4The preheated furnace gas is used as a fluidizing agent to maintain the fluidization state of the coal powder in the gasification furnace 1 at 600 ℃; when the thickness of the bed layer in the gasification furnace 1 is continuously increased, closing the distribution plate valve 3-8 and the central pipe valve 3-9, and stopping the conveying of the preheating oven gas and the circulating gas;
and (3) a synthesis gas treatment stage: in the bed building stage, after the circulating gas valve 5-3 is closed, the pressure P of the furnace top is maintained3The synthesis gas produced by the gasification furnace 1 needs to be treated; when the pressure P of the synthesis gas line is 4-95When the pressure is higher than 8.0MPa, opening an emptying valve 4-16 to perform emptying treatment on the synthesis gas;when the oxygen content of the synthesis gas is more than 0.1 percent and the pressure P of the synthesis gas pipeline is 4-95When the pressure is less than 8.0MPa, closing the emptying valve 4-16, opening the flare valve 4-15, and sending the synthetic gas to a flare treatment system through a flare pipeline 4-11; when the oxygen content of the synthesis gas is less than or equal to 0.1 percent and the pressure P of the synthesis gas line is 4-95And when the pressure is more than or equal to 2.5MPa, closing the torch valve 4-15, opening the crude gas valve 4-14, and conveying the synthesis gas to the methanol synthesis section through the qualified gas pipeline 4-10.
Example 4:
the method for starting the circulating fluidized bed gasification furnace in the embodiment 1 specifically comprises the following steps:
a furnace baking temperature rise and pressure rise stage: the oven gas is nitrogen and carbon dioxide mixed according to any proportion; conveying the oven gas into a preheater 3-2 through an oven gas pipeline 3-1, and heating to 100 ℃ to obtain preheated oven gas; opening a distribution plate valve 3-8 and a central pipe valve 3-9, conveying preheated oven gas into a distribution plate gasifying agent pipeline 1-8 and a central pipe gasifying agent pipeline 1-9 respectively, and increasing the internal temperature of the gasification furnace 1 and the cyclone separator 4-1 through the preheated oven gas; the preheated oven gas after heat exchange with the gasification furnace 1 and the cyclone separator 4-1 is subjected to dust removal by a dust remover 4-2 and heat recovery by a waste heat boiler 4-3 in sequence to obtain circulating gas; opening a circulating air valve 5-3, conveying circulating air to a drying furnace air pipeline 3-1 through a compressor 5-1 to be mixed with the drying furnace air, wherein the mixing volume ratio of the circulating air to the drying furnace air is 2: 10, obtaining mixed gas; the mixed gas is conveyed into a preheater 3-2 and heated to 100 ℃ to obtain preheated mixed gas, the preheated mixed gas is respectively conveyed into a distribution plate gasifying agent pipeline 1-8 and a central pipe gasifying agent pipeline 1-9, and the internal temperatures of the gasification furnace 1 and the cyclone separator 4-1 are improved through the preheated mixed gas; repeating the operation, and controlling the temperature rise rate of the interior of the gasification furnace 1 to be 25 ℃/h and the pressure rise rate to be 0.2MPa/h by controlling the heat medium inlet amount of the preheater 3-2 and the delivery amount of the mixed gas; until the furnace top temperature T of the gasification furnace 14Is lifted to T4650 ℃ and the furnace top pressure P3Is lifted to P3Finishing the furnace heating and boosting stage under the pressure of 3.4 MPa;
bed building preparation stage: after the temperature and pressure raising stage of the oven is completed, closing the circulating gas valve 5-3, continuously conveying preheated oven gas into the gasification furnace 1 through the distribution plate gasification agent pipeline 1-8, and continuously conveying circulating gas into the gasification furnace 1 through the central pipe gasification agent pipeline 1-9; when the internal pressure of the coal lock 2-2 is 700KPa higher than the internal pressure of the air chamber 1-4 of the gasification furnace 1, opening the coal outlet valve 2-5, the coal inlet valve 2-6 and the coal powder delivery valve 5-4, taking the circulating gas as the coal powder delivery gas, adjusting the opening of the coal powder delivery valve 5-4, keeping the internal pressure of the coal powder pipeline 2-3 50KPa higher than the internal pressure of the air chamber 1-4 of the gasification furnace 1, and completing the bed building preparation stage;
a bed building stage: after the bed building preparation stage is finished, when the temperature T of the furnace top is reached4Is lifted to T4600 ℃, furnace top pressure P3Is lifted to P3When the pressure is 3.4MPa, delivering pulverized coal into the gasification furnace 1 through the coal bunker 2-1 and the coal lock 2-2, and delivering a gasification agent into the gasification furnace 1 through the distribution plate gasification agent pipelines 1-8 and the central pipe gasification agent pipelines 1-9 when the thickness of the bed layer in the gasification furnace 1 is 2m, wherein the temperature rise rate of the gasification furnace 1 is controlled to be 60 ℃/h, and the pressure rise rate is controlled to be 0.3 MPa/h; in this process, the circulating gas acts as a fluidizing agent and stabilizes the furnace top temperature T4The preheated furnace gas is used as a fluidizing agent to maintain the fluidization state of the coal powder in the gasification furnace 1 at 600 ℃; when the thickness of the bed layer in the gasification furnace 1 is continuously increased, closing the distribution plate valve 3-8 and the central pipe valve 3-9, and stopping the conveying of the preheating oven gas and the circulating gas;
and (3) a synthesis gas treatment stage: in the bed building stage, after the circulating gas valve 5-3 is closed, the pressure P of the furnace top is maintained3The synthesis gas produced by the gasification furnace 1 needs to be treated; when the pressure P of the synthesis gas line is 4-95When the pressure is higher than 8.0MPa, opening an emptying valve 4-16 to perform emptying treatment on the synthesis gas; when the oxygen content of the synthesis gas is more than 0.1 percent and the pressure P of the synthesis gas pipeline is 4-95When the pressure is less than 8.0MPa, closing the emptying valve 4-16, opening the flare valve 4-15, and sending the synthetic gas to a flare treatment system through a flare pipeline 4-11; when the oxygen content of the synthesis gas is less than or equal to 0.1 percent and the pressure P of the synthesis gas line is 4-95And when the pressure is more than or equal to 2.5MPa, closing the torch valve 4-15, opening the crude gas valve 4-14, and conveying the synthesis gas to the methanol synthesis section through the qualified gas pipeline 4-10.
Example 5:
the conventional three-stage type furnace starting mode described in the background art is taken as a comparison group, the furnace starting method disclosed by the invention is taken as a test group, the furnace starting time, the ignition coal quantity, the unqualified synthesis gas quantity and the like are compared, and the comparison result is shown in table 1.
TABLE 1 two sets of comparison results
Group of Duration of furnace start Ignition coal quantity Cost of ignition coal Unqualified synthesis gas volume
Control group 101 hours 500 ton of 25 ten thousand yuan 350 ten thousand NM3
Test group 40 hours 150 ton of 7.5 ten thousand yuan 40 ten thousand NM3
As can be seen from Table 1, when the method of the present invention is used for starting the furnace, the gas is introducedThe temperature and pressure raising processes of the gasifier are carried out simultaneously, so that the problem that the temperature and pressure raising cannot be carried out simultaneously in the traditional gasifier starting method is solved; the mixed gas without heating treatment is used as the pulverized coal conveying gas and the fluidizing agent, so that the pulverized coal in the gasification furnace can maintain a better fluidizing state, the occurrence of slag-bonding accidents of the gasification furnace is avoided, the temperature and pressure rising process is shortened, the furnace starting time can be shortened to 40 hours, and the unqualified synthetic gas amount generated in the temperature and pressure rising process is reduced to 40 ten thousand NM3The resource waste is reduced, and the environmental protection load of enterprises is lightened; the heating process mainly depends on the oven gas, the oven gas is heated by the preheater and then enters the gasification furnace and the cyclone separator for heat exchange, and the oven gas after heat exchange is treated by the flue gas purification system and then is recycled by the flue gas circulation system, so that the heat efficiency of the oven gas is improved, the ignition coal powder consumption is reduced, the ignition coal waste can be reduced to 150 tons, the resources are saved, and the production cost of enterprises is reduced.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.

Claims (3)

1. The method for starting the circulating fluidized bed gasifier is characterized by comprising the steps of firstly introducing preheating oven gas into a gasifier system to carry out temperature rise and pressure rise operation on the gasifier system, obtaining circulating gas after the preheating oven gas passes through the gasifier system, mixing and recycling part of the circulating gas with the preheating oven gas through a compressor in the temperature rise and pressure rise operation process, controlling the temperature rise and pressure rise rate of the gasifier until the furnace top temperature T of the gasifier is reached4Is lifted to T4650 ℃ at 450-3Lifting to P of 2.0MPa or less3Less than 3.5 MPa; and then, stopping mixing part of the circulating gas with the preheating furnace drying gas, starting to convey pulverized coal into the gasification furnace, taking the circulating gas as the conveying gas of the pulverized coal, starting to convey a gasifying agent into the gasification furnace when the thickness of the bed layer in the gasification furnace is 2m, and treating the synthetic gas generated by the gasification furnace.
2. The furnace starting method of the circulating fluidized bed gasification furnace according to claim 1, which comprises the following steps:
a furnace baking temperature rise and pressure rise stage: conveying the oven gas to a preheater through an oven gas pipeline, and heating to 100 ℃ to obtain preheated oven gas; opening a distribution plate valve and a central pipe valve, respectively conveying the preheated oven gas into a distribution plate gasification agent pipeline and a central pipe gasification agent pipeline, and further lifting the internal temperature of the gasification furnace and the cyclone separator through the preheated oven gas; the preheating oven gas after heat exchange with the gasification furnace and the cyclone separator is subjected to dust removal by a dust remover and heat recovery by a waste heat boiler in sequence to obtain the circulating gas; starting a circulating gas valve, conveying the circulating gas to the oven gas pipeline through the compressor to be mixed with the oven gas, wherein the mixing volume ratio of the circulating gas to the oven gas is 1-2: 10, obtaining mixed gas; the mixed gas is conveyed into the preheater and heated to 100 ℃ to obtain preheated mixed gas, and the preheated mixed gas enters the gasification furnace and the cyclone separator through the distribution plate gasification agent pipeline and the central pipe gasification agent pipeline respectively to raise the internal temperature of the gasification furnace and the cyclone separator; repeating the operation, gradually increasing the temperature of the preheated mixed gas by controlling the heat medium inlet amount of the preheater and the delivery amount of the mixed gas, and controlling the temperature rise rate in the gasification furnace to be 25 ℃/h and the pressure rise rate to be 0.2 MPa/h; up to T4＝450-650℃、2.0MPa≤P3If the pressure is less than 3.5MPa, the temperature and pressure raising stage of the oven is finished;
bed building preparation stage: after the temperature and pressure raising stage of the drying oven is completed, closing a circulating gas valve, continuously conveying the preheated drying oven gas into the gasification oven through the distribution plate gasification agent pipeline, and continuously conveying the circulating gas into the gasification oven through the central pipe gasification agent pipeline; charging the interior of a coal lock, when the internal pressure of the coal lock is at least 200KPa higher than the internal pressure of the gas chamber of the gasification furnace, opening a coal outlet valve, a coal inlet valve and a pulverized coal conveying gas valve, taking the circulating gas as pulverized coal conveying gas, adjusting the opening of the pulverized coal conveying gas valve, keeping the internal pressure of a pulverized coal pipeline 10-50KPa higher than the internal pressure of the gas chamber of the gasification furnace, and completing the bed building preparation stage;
a bed building stage: after the bed building preparation stage is completed, when the furnace top temperature T is reached4Is lifted to T4600 ℃, said furnace top pressure P3Lifting to P less than or equal to 3.0MPa3When the pressure is less than 3.5MPa, conveying pulverized coal into the gasification furnace through a coal bunker and the coal lock, and when the thickness of the bed layer in the gasification furnace is 2m, conveying the gasification agent into the gasification furnace through the distribution plate gasification agent pipeline and the central pipe gasification agent pipeline, and controlling the temperature rise rate of the gasification furnace to be 30-60 ℃/h and the pressure rise rate to be 0.2-0.3 MPa/h; in this process, the recycle gas acts as a fluidizing agent and stabilizes the furnace top temperature T4Maintaining the fluidization state of the coal dust in the gasification furnace by using the preheating oven gas as a fluidizing agent at 600 ℃; when the thickness of the bed layer in the gasification furnace is continuously increased, closing the distribution plate valve and the central pipe valve, and stopping conveying the preheating oven gas and the circulating gas;
and (3) a synthesis gas treatment stage: in the bed building stage, after the circulating gas valve is closed, in order to maintain the furnace top pressure P3The synthesis gas produced by the gasification furnace needs to be treated; when the synthetic gas line pressure P5When the pressure is higher than 8.0MPa, opening an emptying valve to empty the synthesis gas; when the oxygen content of the synthesis gas is more than 0.1 percent, the pressure P of the synthesis gas pipeline5When the process design pressure is less than the process design pressure, closing the emptying valve, opening a flare valve, and sending the synthesis gas to a flare treatment system through a flare pipeline; when the oxygen content of the synthesis gas is less than or equal to 0.1 percent and the pressure P of the synthesis gas pipeline5And when the process design pressure is not less than the process design pressure, closing the torch valve and opening the crude gas valve, and conveying the synthesis gas to a methanol synthesis working section through a qualified gas pipeline.
3. The method for starting up the circulating fluidized bed gasification furnace according to claim 2, wherein the oven gas is any one or a combination of nitrogen and carbon dioxide, and when the oven gas comprises the nitrogen and the carbon dioxide, the nitrogen and the carbon dioxide can be mixed in any proportion.
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Publication number Priority date Publication date Assignee Title
CN1966624A (en) * 2005-11-17 2007-05-23 财团法人工业技术研究院 Gasification stove start-up device
CN102994162A (en) * 2012-12-10 2013-03-27 中国五环工程有限公司 Circulating fluidized bed gasifier system and starting method thereof
JP2014224206A (en) * 2013-05-17 2014-12-04 株式会社Ihi Method for operating gas production system using circulating fluidized bed gasification furnace
CN104974798A (en) * 2015-07-07 2015-10-14 航天长征化学工程股份有限公司 Control method for operation of pulverized coal burner of pulverized coal pressure gasification reaction device

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1966624A (en) * 2005-11-17 2007-05-23 财团法人工业技术研究院 Gasification stove start-up device
CN102994162A (en) * 2012-12-10 2013-03-27 中国五环工程有限公司 Circulating fluidized bed gasifier system and starting method thereof
JP2014224206A (en) * 2013-05-17 2014-12-04 株式会社Ihi Method for operating gas production system using circulating fluidized bed gasification furnace
CN104974798A (en) * 2015-07-07 2015-10-14 航天长征化学工程股份有限公司 Control method for operation of pulverized coal burner of pulverized coal pressure gasification reaction device

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