WO2011029285A1 - Gazeifieur a lit fluidise multicouche - Google Patents

Gazeifieur a lit fluidise multicouche Download PDF

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Publication number
WO2011029285A1
WO2011029285A1 PCT/CN2010/001410 CN2010001410W WO2011029285A1 WO 2011029285 A1 WO2011029285 A1 WO 2011029285A1 CN 2010001410 W CN2010001410 W CN 2010001410W WO 2011029285 A1 WO2011029285 A1 WO 2011029285A1
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WO
WIPO (PCT)
Prior art keywords
overflow device
longitudinal axis
fluidized bed
space
overflow
Prior art date
Application number
PCT/CN2010/001410
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English (en)
Chinese (zh)
Inventor
毕继诚
李克忠
程相龙
曲旋
张�荣
孙东凯
李金来
甘中学
Original Assignee
新奥科技发展有限公司
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Publication date
Priority claimed from CN 200910170387 external-priority patent/CN102021038B/zh
Priority claimed from CN201010279560.7A external-priority patent/CN102399595B/zh
Application filed by 新奥科技发展有限公司 filed Critical 新奥科技发展有限公司
Publication of WO2011029285A1 publication Critical patent/WO2011029285A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
    • 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
    • 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

Definitions

  • the present invention relates to a gasifier, and more particularly to a multi-layer fluidized bed gasifier for gasification of coal to produce a methane-rich gas.
  • the invention relates to a multi-layer fluidized bed gasification furnace device for preparing a methane-rich gas by gasification of a pulverized coal multi-layer fluidized bed.
  • China is a country rich in coal and oil-poor. With the rapid development of society and economy, China's natural gas demand has risen sharply, and the proportion in the energy structure has increased rapidly. While domestic natural gas is still in the early stage of exploration and development, imports are also in their infancy, and supply capacity is seriously lagging behind, resulting in an increasingly prominent contradiction between natural gas supply and demand.
  • Using coal with relatively large resource advantages in China it can be gasified to produce gas, which not only promotes the efficient and clean utilization of coal, but also utilizes existing natural gas pipelines to effectively alleviate the supply and demand of natural gas at a lower economic cost. Contradictions, this is a powerful measure for the comprehensive utilization of coal resources.
  • the usual coal gasification and methane production process that is, the gasification agent composed of oxygen (or air) and/or water vapor (H 2 0) at a high temperature is gasified in a single-layer gasification furnace to form a gasification reaction.
  • a small amount of decane (CH 4 ) synthesis gas (mainly hydrogen, carbon monoxide and carbon dioxide), followed by a water gas shift and a decaneization process, and a two-step process for the preparation of decane.
  • the disadvantages of this type of coal gasification process are: The gasification reaction has high energy consumption, high requirements on equipment, and requires three reaction devices, complicated processes, and the like.
  • the catalytic gasification of coal to produce methane is an important way to clean and use coal.
  • the catalytic gasification technology of coal is used.
  • the coal is mainly composed of water vapor (H 2 0 ) and hydrogen (H 2 at relatively low temperature). ), a gas mixture of carbon monoxide (CO) is subjected to a gasification reaction under the catalytic action of a catalyst to form a high concentration of methane (CH 4 ).
  • the coal-catalyzed gasification process for preparing methane technology mentioned in the related patent uses cryogenic separation to separate methane from gas production with carbon monoxide and hydrogen, and recycles hydrogen and carbon monoxide in the reaction gas to the gasifier.
  • the methanation reaction is converted to methane in a gasifier to increase the production of system methane.
  • This coal catalytic gasification process can be carried out in a single-layer gasifier, but has the disadvantages of low gasification reaction rate, long reaction time, low carbon conversion rate, high investment in gas separation system, and the like; In order to meet the heat balance of the reactor, the coal catalytic gasification process needs to heat the superheated steam into the higher temperature, and the steam superheating system and the heat exchange system have higher load and poor economy.
  • U.S. Patent 4,077,778 teaches the use of a multi-stage fluidized bed to effect catalytic gasification of coal to increase carbon conversion.
  • the mainstream bed operation has a higher gas velocity, and some carbon particles are entrained to the secondary fluidized bed, and the gasification reaction is carried out at a lower gas velocity, the solid phase residence time is increased, and the carbon conversion rate is maximized.
  • multi-stage gasification can increase carbon utilization from 70-85% to over 95%.
  • the multi-stage fluidized bed coal catalytic gasification process adopts multi-stage fluidized bed, which has high equipment investment and complicated operation.
  • U.S. Patent No. 4,094,650 teaches the use of an alkali metal catalyzed gasification of a carbonaceous solid to produce methane which is recovered for reuse.
  • the water-soluble catalyst is recovered by multistage washing, and the insoluble catalyst is recovered by lime digestion.
  • U.S. Patent No. 0,277,437 based on U.S. Patent No. 4,094,650, which utilizes a primary treatment to separate the alkali metal material from the reactor solid residue, simplifies the alkali metal catalyst recovery process, and improves the economics and overall efficiency of the catalytic gasification process, but The recycling system is still complicated and the recycling method is expensive.
  • U.S. Patent No. 4,318,712 discloses a whole process for direct decaneization of coal.
  • the coal is pre-mixed with the catalyst before entering the coal gasification reactor, and the superheated steam is used not only as a gasifying agent but also as a heat source.
  • the reaction temperature in the furnace was maintained, and the temperature in the furnace was controlled at 700. C or so, superheated steam temperature 850. C, gasifier reaction pressure
  • the force is 3.5 MPa, and the coal reacts with the superheated steam under the action of the catalyst to directly obtain the product rich decane gas.
  • GPE of the United States has conducted further research on the basis of EXXON process technology.
  • U.S. Patent No. 20070000177A1 also discloses a process for direct methanation of coal.
  • the catalyst is an alkali metal carbonate or an alkali metal hydroxide, and the gasifying agent is water vapor.
  • the main technical features in addition to the addition of a highly efficient decane catalyst, calcium oxide is added to the reacted pulverized coal to absorb the carbon dioxide produced during the reaction, thereby further increasing the decane content.
  • the reaction temperature is generally controlled at 700. Around C, the reaction rate is slow, the conversion rate of carbon is low, the heat of the external heating system is difficult to maintain, and the operation of the catalyst recovery unit is increased, and the catalyst recovery effect directly affects the production cost.
  • U.S. Patent No. 5,064,444 proposes to divide a fluidized bed gasifier into a pyrolysis section, a gasification section, and a cooling section in the case of pressurized steam vaporization. Separate with a partition. A serpentine coil (snake heat exchanger) is placed in the pyrolysis section and the gasification section of the gasification furnace, and 900 is introduced therein. C ⁇ 950. The high temperature gas of C (such as the gas after the combustion of the fuel) heats the coal powder to provide the heat required for gasification and pyrolysis to obtain the gas.
  • the fluidized bed gasifier can be either vertical or horizontal, with a capacity of 700.
  • the superheated steam of C ⁇ 800'C is a gasifying agent, and the cooling section is supplied with saturated steam and pneumatically fed.
  • the device prolongs the residence time of the pulverized coal, is favorable for solid phase processing, and has high utilization rate of heat energy, but the utilization rate of the reaction volume in the gasification furnace is low, which affects solid phase processing; the residual carbon content in the vertical furnace operation is high, It is difficult to use effectively; compared with gas-solid contact heat transfer, the heat transfer rate is slow, and the solid phase in the bed is unevenly heated; at the same time, the equipment is complicated, especially the horizontal furnace.
  • the present invention has been made in an effort to provide a gasification apparatus rich in methane gas by using a low-investment, process-pulverized coal gasification process.
  • the present invention provides a multi-layer fluidized bed gasification furnace for gasification of coal to produce a gas rich in decane gas, the fluidized bed gasification furnace comprising:
  • a gasifier housing having a vertical longitudinal axis defining an interior space therein;
  • At least two layers of gas distributors in the interior space of the housing that are perpendicular to the longitudinal axis and are arranged at different heights along the longitudinal axis, in the form of orifices, the at least two layers of gas distribution
  • the first gas distributor and the second gas distributor located below the first distributor, the first gas distributor and the second distributor separating the internal space of the casing into an upper layer Space, intermediate space and lower space;
  • a raw material inlet disposed at an upper portion of a side of the casing, the raw material inlet leading to the upper space for inputting raw materials into the upper space, the overall flow direction of the raw material is from top to bottom along the longitudinal axis ;
  • a ash outlet located at the bottom of the housing
  • a gasification agent inlet for vaporizer entry near a side of the ash outlet at the bottom of the housing, the overall flow direction of the gasifying agent being bottom-up along the longitudinal axis;
  • the first gas distributor is provided with a first overflow device in a tubular form open at both ends
  • the second gas distributor is provided with a second overflow device in a tubular form with both ends open.
  • the first overflow device and the second overflow device are configured to move the raw material from top to bottom along a tortuous line, and flow from the upper space to the intermediate layer space through the first overflow device, and then The intermediate layer space flows into the lower space through the second overflow device
  • the lower end of the first overflow device and the upper end of the second overflow device are spaced apart from each other in a horizontal direction perpendicular to the longitudinal axis to prevent the material from passing straight down.
  • the shortest distance between the upper end of the first overflow device and the inner wall of the gasifier housing is within the inner diameter of the gasifier housing.
  • the shortest distance between the upper end of the second overflow device and the inner wall of the gasifier housing is between 1/5 and 1/2 times the inner diameter of the gasifier housing, and preferably
  • the shortest distance between the lower end outlet and the inner wall of the gasifier housing is between 1/10 and 1/6 times the inner diameter of the gasifier housing .
  • the projections of the upper and lower outlets of the first overflow means are spaced apart from each other on a horizontal plane perpendicular to the longitudinal axis.
  • the first overflow means forms an angle with the longitudinal axis that is greater than or equal to the angle of repose of the coal feedstock.
  • the angle of repose of coal raw materials varies according to environmental factors such as coal particle size, temperature, humidity and pressure. In actual production, the angle of repose of coal under real gasification conditions is determined by various factors of real coal gasification. The range of the angle is selected based on the principle that the angle of the angle is greater than or equal to the angle of repose of the coal under real gasification conditions.
  • the first overflow means forms an angle of less than or equal to 60 with the longitudinal axis.
  • the first overflow device includes an upper section and a lower section, and an upper section of the first overflow device is parallel to the longitudinal axis, and a lower section of the first overflow device
  • the longitudinal axis forms an angle greater than or equal to the angle of repose of the coal material, and the arc between the upper and lower sections of the first overflow device Connected.
  • the first overflow device includes an upper section and a lower section, and an upper section of the first overflow device is parallel to the longitudinal axis, and a lower section of the first overflow device
  • the longitudinal axis forms less than or equal to 60.
  • the angle between the lower section of the first overflow means and the longitudinal axis preferably forms an angle of between 30 and 50, most preferably 45.
  • Angle of inclusion (the angle of repose of coal raw materials varies according to environmental factors such as coal particle size, temperature, humidity and pressure. In actual production, the parameters of various factors in real coal gasification are used to determine coal under real gasification conditions. The angle of repose, and the range of the angle is greater than or equal to the angle of repose of the coal under real gasification conditions, to select the range of the angle), between the upper and lower sections of the first overflow device The arc transitions are connected.
  • the projections of the upper and lower outlets of the second overflow means are spaced apart from each other on a horizontal plane perpendicular to the longitudinal axis.
  • the second overflow means forms an angle with the longitudinal axis that is greater than or equal to the angle of repose of the coal feedstock.
  • the angle of repose of coal raw materials varies according to environmental factors such as coal particle size, temperature, humidity and pressure. In actual production, the angle of repose of coal under real gasification conditions is determined by various factors of real coal gasification. The range of the angle is selected based on the principle that the angle of the angle is greater than or equal to the angle of repose of the coal under real gasification conditions.
  • the second overflow means forms an angle of less than or equal to 60 with the longitudinal axis.
  • the second overflow device includes an upper section and a lower section, an upper section of the second overflow device is parallel to the longitudinal axis, and a lower section of the second overflow device is The longitudinal axis forms an angle greater than or equal to the angle of repose of the coal material, and the upper and lower sections of the second overflow device are connected by a circular arc transition.
  • the second overflow device includes an upper section and a lower section, an upper section of the second overflow device is parallel to the longitudinal axis, and a lower section of the second overflow device is The longitudinal axis forms less than or equal to 60.
  • the angle between the lower section of the second overflow device and the longitudinal axis is preferably 30.
  • Angle of inclusion the angle of repose of coal raw materials varies according to environmental factors such as coal particle size, temperature, humidity and pressure. In actual production, the parameters of various factors in real coal gasification are used to determine coal under real gasification conditions. The angle of repose, and the range of the angle is greater than or equal to the angle of repose of the coal under real gasification conditions to select the range of the angle), between the upper and lower sections of the second overflow device The arc transitions are connected.
  • At least one of the longitudinally central portion or the longitudinally lower portion of the housing is further provided with an auxiliary feed port.
  • At least one gas distributor for further separating the space is further disposed in any one of the upper space, the intermediate space, and the lower space, and the at least one An overflow device arranged by a layer gas distributor.
  • a third gas distributor is further disposed below the second gas distributor.
  • the third gas distributor has a funnel shape.
  • the portion of the overflow device above the gas distributor is an overflow weir, and the height of the weir is calculated by the solid phase processing time and the bed layer:
  • the unit is h D -- the inner diameter of the furnace body, the unit is nr
  • the distance between two adjacent gas distributors is determined by the height of the overflow device between them and the height of the bed holding capacity, which is calculated by:
  • H the distance between two adjacent gas distributors, in units of m;
  • Hl the height of the overflow device between the two gas distributors, in m
  • h l the height of the material holding amount between the two gas distributors, in units of m
  • the impregnated catalyst coal powder is added to the intermediate layer space B (catalytic gasification zone) of the three-layer fluidized bed gasifier under the action of the rotary feeder; the raw coal is added from the upper pyrolysis section of the reactor, and successively passes through multiple layers of fluidization.
  • Bed gasifier upper space A partial pyrolysis zone
  • intermediate zone space B catalytic gasification zone
  • lower zone space C residual gasification zone.
  • the high-temperature hot gas generated by the reaction heats the feed cold coal powder to cause partial pyrolysis to produce a product rich in methane-rich pyrolysis gas and tar.
  • the partially pyrolyzed coal powder enters the catalytic gasification zone, and catalytic gasification, decaneization and the like are generated under the action of the catalyst to generate effective gas components such as methane, carbon monoxide and hydrogen, and carbon dioxide, a small amount of hydrogen sulfide and ammonia. Wait.
  • the unreacted coal residue enters the residue gasification zone and is gasified to generate carbon monoxide, hydrogen, carbon dioxide and other gases under the action of oxygen and water vapor, while carbon monoxide and hydrogen enter the upper catalytic gasification zone, and decane occurs under the action of the catalyst.
  • Chemical reaction increase system decane yield, high temperature Water vapor provides some heat to the catalytic gasification zone.
  • the device integrates three reactors of coal pyrolysis, coal catalytic gasification and residue gasification to realize logistics coupling and heat coupling, and self-supply heat to reduce the energy consumption of superheated steam.
  • the problem of carbon residue in the residue is solved; the average residence time is prolonged, the gas production capacity is increased, and the carbon conversion rate is increased.
  • the gasification of the multi-layer fluidized bed gasification furnace is used to prepare a gas rich in decane gas, which has high thermal efficiency, high solid phase processing depth, high decane content in the gas product, and simple equipment. Easy to operate.
  • the uppermost layer of the multi-layer bed will inhibit the formation of tar to promote the formation of tar, reduce the amount of catalyst, and reduce the cost of the catalyst; at the same time, some industrial wastes (such as black liquor of paper mills, industrial waste alkali, etc.) can be utilized as catalyst raw materials. , increase methane content.
  • each overflow device Since the distance between the upper end of each overflow device and the inner wall of the gasifier housing is large (the shortest distance between the upper end inlet and the inner wall of the gasifier housing is in the inner diameter of the gasifier housing) 1/5 times to 1/2 times), the problem of "slow material flow, formation of retention and fluidized dead zone" can be avoided, and at the same time, since the upper and lower outlets of each overflow device are perpendicular to the gasifier
  • the projections of the horizontal plane of the longitudinal axis of the housing are spaced apart from one another (e.g., each overflow device is in the form of a partial inclined tube), such that, for example, between the lower outlet of the first overflow device and the upper inlet of the second overflow device
  • the lateral distance is maximized, so that the length of the lateral flow path of the material in each layer space is extended as much as possible, which can promote the fluidization reaction of the material to be more fully performed, thereby effectively improving the overall efficiency of the fluidized bed.
  • Figure 1 is a structural view of an embodiment of the present invention
  • Figure 5 is a schematic structural view of various variations of the overflow device of the present invention, wherein Figure 5a is a simplified illustration of the arrangement of the vertically arranged overflow devices of Figures 1-4, and Figure 5b The arrangement of the overflow device in Figure 5c is a more advantageous and preferred manner.
  • the present invention provides a multi-layer fluidized bed gasification furnace for gasification of coal to produce a gas rich in decane gas, the fluidized bed gasification furnace comprising:
  • a gasifier housing 3 having a vertical longitudinal axis defining an interior space therein;
  • At least two layers of gas distributors 2 in the form of orifice plates arranged in the interior space of the housing 3 perpendicular to the longitudinal axis and at different heights along the longitudinal axis, the at least two layers
  • the gas distributor 2 includes a first gas distributor and a second gas distributor located below the first distributor, the first gas distributor and the second distributor to the inner space of the casing Separated into upper space A, intermediate space B and lower space C;
  • a raw material inlet 4 disposed at an upper portion of the side of the casing, the raw material inlet leading to the upper space A for inputting raw materials into the upper space A, the overall flow direction of the raw material being along the longitudinal axis Top down
  • gasifying agent inlet for gasifying agent entering near a side of the ash outlet 7 at the bottom of the casing, the overall flow direction of the gasifying agent being bottom-up along the longitudinal axis;
  • the overflow device is generally indicated by the numeral 1, wherein the overflow device located above is referred to as a first overflow device, and the overflow device located below is referred to as a second overflow device.
  • a first overflow device having a tubular form open at both ends is disposed through the first gas distributor, and the second gas distributor is provided with a second overflow device having a tubular form open at both ends.
  • An overflow device and a second overflow device for flowing the raw material from top to bottom along a tortuous line, flowing from the upper space A through the first overflow device to the intermediate layer space B, and then The intermediate layer space B flows into the lower space C through the second overflow device, and the lower end of the first overflow device and the upper end of the second overflow device are perpendicular to the
  • the longitudinal axes are spaced apart from each other in the horizontal direction to prevent the material from passing straight down.
  • the shortest distance between the upper end of the first overflow device and the inner wall of the gasifier housing is in the gasifier housing.
  • the inner diameter is between 1/5 and 1/2 times
  • the shortest distance between the upper end of the second overflow device and the inner wall of the gasifier housing is 1 in the inner diameter of the gasifier housing Between /5 and 1/2 times.
  • Each of the shortest distances exemplarily shown in Figure 5b is about 1/3 times the inner diameter of the gasifier housing
  • the shortest distances exemplarily shown in Figure 5c are the inner diameter of the gasifier housing.
  • the shortest distance suitable for use in the present invention is that the ratio of the inner diameter of the gasifier housing can vary from 1/2 to 1/5 times both inclusive.
  • the spacing between each of the overflow means and the inner wall of the gasifier housing is small, such that the respective overflow means are spaced apart from each other in a horizontal direction perpendicular to the longitudinal axis. Larger distances are advantageous in terms of preventing material flow shorts and promoting sufficient reaction of the material.
  • each overflow device is adjacent to the inner wall of the gasifier housing (in other words, the distance between the upper end inlet of the overflow device and the inner wall of the housing is too close) during the fluidization process due to all areas on the gas distributor
  • the material flows toward the upper inlet of the overflow device on the gas distributor, in a partial region between the upper inlet of the overflow device and the inner wall of the gasifier housing, due to the overflow device and the gasifier shell
  • the space between the inner walls is narrow, and the resistance formed is larger than other regions, so that the gas short circuit does not flow therethrough, so that the flow of the material in the partial region tends to be slow, causing the flow to stagnant to form a fluidized dead zone.
  • the shortest distance between the upper end of each overflow device and the inner wall of the gasifier housing is 1/5 times the inner diameter of the gasifier housing ( At the critical point), the flow of the material tends to be slow and tends to form a fluidized dead zone.
  • the shortest distance is less than 1/5 times the inner diameter of the gasifier casing, the fluidized dead zone is clearly formed.
  • the spacing between the upper end of each overflow device and the inner wall of the gasifier housing is greater, rather than in the immediate vicinity of the gasifier housing as in Figure 5a.
  • the inner wall that is, the shortest distance is less than 1/5 times the inner diameter of the gasifier shell), so that the problem of "slow material flow, formation of retention and fluidized dead zone" can be avoided, thereby effectively increasing the flow.
  • the overall efficiency of the chemical bed In a preferred embodiment of the invention, the projections of the upper and lower outlets of the first overflow device on a horizontal plane perpendicular to the longitudinal axis are spaced apart from one another.
  • the first overflow device has an angle formed with the longitudinal axis that is greater than or equal to an angle of repose of the coal material.
  • the first overflow device includes an upper section and a lower section, and an upper section of the first overflow device is parallel to the longitudinal axis, and a lower section of the first overflow device Forming less than or equal to 60 with the longitudinal axis.
  • the angle between the lower portion of the first overflow device and the longitudinal axis preferably forms an angle of between 30 and 50, most preferably 45. Angle of inclusion (the angle of repose of coal raw materials varies according to environmental factors such as coal particle size, temperature, humidity and pressure.
  • the parameters of various factors in real coal gasification are used to determine coal under real gasification conditions.
  • the angle of repose, and the range of the angle is greater than or equal to the angle of repose of the coal under real gasification conditions to select the range of the angle), between the upper and lower sections of the first overflow device
  • the arc transitions are connected.
  • the projections of the upper and lower outlets of the second overflow device on a horizontal plane perpendicular to the longitudinal axis are spaced apart from one another.
  • the angle between the second overflow device and the longitudinal axis is greater than or equal to the angle of repose of the coal material.
  • the second overflow device includes an upper section and a lower section, an upper section of the second overflow device is parallel to the longitudinal axis, and a lower section of the second overflow device Forming less than or equal to 60 with the longitudinal axis.
  • the angle between the lower section of the second overflow device and the longitudinal axis is preferably 30. To 50. Angle, most preferred shape Into 45.
  • Angle of inclusion the angle of repose of coal raw materials varies according to environmental factors such as coal particle size, temperature, humidity and pressure. In actual production, the parameters of various factors in real coal gasification are used to determine coal under real gasification conditions. The angle of repose, and the range of the angle is greater than or equal to the angle of repose of the coal under real gasification conditions to select the range of the angle), between the upper and lower sections of the second overflow device The arc transitions are connected.
  • the upper sections of the first overflow means and the second overflow means are each parallel to the longitudinal axis and the lower sections form an angle of about 45 with the longitudinal axis. And both are inclined toward the left side of the figure.
  • the upper sections of the first overflow means and the second overflow means are both parallel to the longitudinal axis, and the angles formed by the lower sections and the longitudinal axis are about 45 degrees, but the lower sections are respectively oriented. Tilt left and right.
  • each overflow device can also simply take the form of an integral inclined tube, that is, the upper and lower sections are in a straight line, which is perpendicular to the longitudinal axis of the gasifier housing.
  • the first overflow means of the upper and lower sections in a straight line is in the form of an integral inclined tube which forms a clamp with the longitudinal axis of less than or equal to 60°. angle.
  • the second overflow device of the upper and lower sections in a straight line takes the form of an integral inclined tube, and the integral inclined tube forms less than the longitudinal axis.
  • the descending material has a certain velocity and does not form a material retention in the overflow device.
  • the shortest distance between the lower end outlet of each overflow device and the inner wall of the gasifier housing is between 1/10 and 1/6 times the inner diameter of the gasifier, that is, Maintaining a sufficient distance from the nearest inner wall ensures that the particles are flowing there (for example, in Figure 5b, the shortest distance between the lower end outlet of the first overflow means and the inner wall is 1/1 of the inner diameter of the gasifier) 10 times), and therefore, does not tend to form a hold.
  • the lower end outlet of each overflow device is kept at a certain distance from the upper end inlet of the next overflow device, as shown in FIG. 5b and FIG. 5c, so as to extend the lower end outlet and the second overflow of the first overflow device as much as possible.
  • the length of the lateral flow path of the material between the upper inlets of the flow device is intended to promote sufficient reaction of the material.
  • the raw coal inlet The number of inlets of the raw coal loaded with the catalyst may be different.
  • the arrangement and manner of the particular overflow arrangement in Figures 5b and 5c can be optimized in conjunction with the gasifier shown in Figures 1 through 4 and other gasifiers not shown.
  • the inlets of the raw coal inlet 4 and the raw coal loaded with catalyst shown in Fig. 1 are respectively located on both sides of the gasification furnace, but in practice, the two inlets may also be disposed on the same side of the gasification furnace and in the week.
  • the upward position is in the same position, in which case the specific arrangement of the two-layer overflow device of Figure 1 can take the specific position and form of Figure 5b.
  • This arrangement allows the arrangement of the overflow means in each layer to more conveniently balance both the prevention of "material retention - fluidized dead zone" and the extension of the length of the lateral flow path of the material.
  • the arc transition segment, the radius of curvature of the arc transition segment can be set according to specific design conditions and can be varied within a reasonable range.
  • each of the overflow devices may be generally tubular, the upper portion of the overflow device may have a circular cross section, and the lower portion of the overflow device may have an elliptical cross section.
  • the long axis of the ellipse should be consistent with the direction of extension of the lower section to maximize the flow section of the material along the extension direction, and the inner diameter of the elliptical short axis should be the same as the circular cross section of the upper section.
  • the arc transition between the upper and lower sections is a reducer joint pipe, so that the circular cross section of the upper section and the elliptical cross section of the lower section naturally transition smoothly, so that the flow resistance of the material in each section minimize.
  • the lengths of the upper and lower sections of each overflow device may be designed such that the length of the upper section is smaller than the length of the lower section, specifically, the length of the upper section may be 0.2 to 0.6 times the axial projection length of the lower section.
  • the curvature of the arc transition between the upper and lower sections of each overflow device may be determined based on the effective cross-sectional area of the overflow device and the specific length ratio between the upper and lower segments described above.
  • the longitudinal middle portion of the housing is also provided with an auxiliary central feed opening 4.
  • the longitudinal lower portion of the housing is further provided with an auxiliary lower feed opening 5 (see Fig. 2).
  • At least one layer of gas distributor for further separating the space is provided in any one of the upper space A, the intermediate space B, and the lower space C.
  • An overflow device arranged by the at least one gas distributor.
  • a third gas distributor is further disposed below the second gas distributor.
  • the third gas distributor is funnel shaped (see Figure 3).
  • the present invention provides a gasification apparatus which can be applied to a multi-layer fluidized bed coal gasification to obtain a methane-rich gas system, which is a multi-layer fluidized bed gasification furnace, comprising: an upper space A ( Partial pyrolysis zone), intermediate zone space B (catalytic gasification zone), lower zone space C (residual gasification zone).
  • the raw coal enters the upper space A through the feed port 4 of the multi-layer fluidized bed space A, that is, the partial pyrolysis zone.
  • the feed cold coal powder is heated by the high temperature hot gas generated by the lower end reaction, so that partial pyrolysis occurs.
  • Pyrolysis of raw coal produces pyrolysis gas, tar and semi-coke rich in methane.
  • the gaseous catalyst entering the upper space A (partial pyrolysis zone) changes its form due to the decrease of temperature, separates from the gas product, and remains in the furnace to continue to participate in the gasification reaction to realize the recycling of the catalyst in the furnace.
  • the mixture of coal and catalyst enters the intermediate layer space B through the feed port 4 of the intermediate layer space B, that is, the catalytic gasification zone of the gasifier, where the mixture of coal and catalyst passes from the upper space A through the overflow device 1
  • the partially pyrolyzed coal powder is mixed and gasified with a gasifying agent by a catalyst to form an effective gas component such as CH 4 , CO, H 2 , C0 2 , a small amount of H 2 S and NH 3 , and the like.
  • the main reactions are as follows:
  • the lower space C (residue gasification zone) CO and H 2 can enter the intermediate space B (catalytic gasification zone), methanation reaction occurs under the action of the catalyst, and the system is increased.
  • the methane yield in addition, the high-temperature steam generated in the lower space C (residue gasification zone) provides the heat required for partial reaction in the intermediate space B (catalytic gasification zone).
  • the coal residue which is not sufficiently reacted in the intermediate layer space B (catalytic gasification zone) enters the lower space C (residue gasification zone), and is gasified by the action of 0 2 and steam to generate gases such as CO, H 2 and C0 2 .
  • the main reactions are as follows: c + o 2 ⁇ co 2 (5)
  • CO and H 2 generated in the lower space C (residue gasification zone) of the gasifier can enter the upper intermediate space B (catalytic gasification zone), The methanation reaction occurs under the action of the catalyst, thereby increasing the system decane yield.
  • the generated high temperature gas and water vapor can provide partial heat to the intermediate layer space B (catalytic gasification zone), thereby reducing the ash.
  • the slag carbon content and improve the comprehensive utilization of feed pulverized coal.
  • the higher temperature in the lower space C causes some of the catalyst to volatilize in the gaseous form to the intermediate layer space B (catalytic gasification zone), and the recycling of the catalyst in the fluidized bed can reduce the catalyst in the initial pulverized coal.
  • the amount of addition in the catalyst reduces the burden on the catalyst recovery system, even without the need to additionally configure a catalyst recovery system.
  • the gasification agent superheated steam and a small amount of oxygen enter the residue gasification zone from the bottom of the gasifier, and burn and gasify with the residue, while providing the required heat to the intermediate space B (catalytic gasification zone).
  • a slagging device is connected below the multi-layer fluidized bed gasification furnace, and the slagging device is used to discharge the ash after gasification in the gasification zone of the residue.
  • the high-temperature furnace gas produced by the multi-layer fluidized bed gasification furnace is discharged from the top of the furnace and enters the subsequent separation and purification process.
  • the gasification furnace outlet gas (high-temperature furnace gas) passes through the isothermal dust filter unit, and the filtered dust is returned to the gasification furnace to continue the gasification reaction, and the filtered gas is sent to the gas-liquid cooling separation unit.
  • Gas-liquid separation To low temperature tar and crude gas. Thereafter, the crude gas enters the gas purifying device to remove acid gases such as carbon dioxide and hydrogen sulfide, thereby obtaining a gas rich in decane.
  • the furnace in the lower space C (residue gasification zone) of the multilayer fluidized bed can be used.
  • a feed port 5 is disposed on the side wall of the body 3, and a small amount of raw coal is supplied to the residue gasification zone through the feed port, and the combustion of the small amount of raw coal in the lower space C (residue gasification zone) can provide auxiliary energy to satisfy The temperature requirements required for catalytic gasification.
  • the distributor of the lower fluidized bed lower space C can be replaced, using a funnel-shaped distributor through the air inlets 6, 7
  • the ash discharge gas velocity and the fluidization gas velocity are separately regulated.
  • overflow devices in order to avoid the reverse flow of gas, to achieve a continuous and stable overflow between the beds, and at the same time to facilitate the control of the overflow flow of the material, other forms of overflow devices can be used, such as with mechanical transmission Plug-type overflow device for the device.
  • the position of the plug 8 is adjusted by a mechanical transmission to change the direction of the gas and the cross-section of the lower opening to achieve a smooth overflow.
  • the scale setting in the figure can be modified (that is, the modified scale setting is different from that shown in Figure 1-4.
  • a ratio such that the shortest distance between the upper end of the first overflow device and the inner wall of the gasifier housing is between 1/5 and 1/2 times the inner diameter of the gasifier housing, and the second overflow The shortest distance between the upper end of the flow device and the inner wall of the gasifier housing is between 1/5 and 1/2 times the inner diameter of the gasifier housing.
  • the arrangement of the overflow device is modified and optimized based on the previous embodiments.
  • the first overflow device located above The shortest distance between the upper end of the gasifier and the inner wall of the gasifier housing is between 1/5 and 1/2 times the inner diameter of the gasifier shell, and the upper end of the second overflow device located below is gas
  • the shortest distance between the inner walls of the furnace shell is between 1/5 and 1/2 times the inner diameter of the gasifier shell.
  • Each of the shortest distances exemplarily shown in Figure 5b is about 1/3 times the inner diameter of the gasifier housing.
  • the upper sections of the first overflow means and the second overflow means are both parallel to the longitudinal axis, and the lower sections form an angle of about 45 with the longitudinal axis and are oriented toward the left side of the figure. The direction is tilted.
  • the arrangement of the overflow device is improved and optimized based on the previous embodiments.
  • the shortest distance between the upper end of the first overflow device and the inner wall of the gasifier housing is 1/5 to 1/2 of the inner diameter of the gasifier housing.
  • the shortest distance between the upper end of the second overflow device located below and the inner wall of the gasifier housing is between 1/5 and 1/2 times the inner diameter of the gasifier housing.
  • Each of the shortest distances exemplarily shown in Figure 5c is about 1/2 times the inner diameter of the gasifier housing.
  • each overflow means and the second overflow means are each parallel to the longitudinal axis, and the lower sections form an angle of about 45 with the longitudinal axis. However, each lower section is inclined toward the left and right sides of the figure.
  • a plug-type overflow device with a mechanical transmission as shown in Figure 4 can be used in combination as needed.
  • the height of the weir (the portion of the overflow device above the gas distributor) is determined by the solid phase processing time and the bed holding amount, using the following formula
  • the distance between two adjacent gas distributors is determined by the height of the overflow device between them and the height of the bed holding capacity, calculated by:
  • Hl the height of the overflow device between the two gas distributors, in m
  • h l the height of the material holding amount between the two gas distributors, in units of m
  • the gasification agent is introduced from the bottom of the gasification furnace.
  • the raw coal is added from the upper pyrolysis section of the reactor and passes through the upper space A of the multi-layer fluidized bed, the intermediate layer space B, and the lower layer.
  • Space (:. In the upper space A (partial pyrolysis zone) of the multi-layer fluidized bed, the high temperature heat generated by the catalytic gasification reaction of the feed cold coal powder in the intermediate layer space B (catalytic gasification zone)
  • the gas is heated to partially pyrolyze the pulverized coal to form a pyrolysis gas rich in CH 4 and a product such as tar.
  • the partially pyrolyzed coal powder passes through the first overflow device and enters the multi-layer fluidized bed.
  • the intermediate layer space B (catalytic gasification zone) undergoes catalytic gasification, methanation and the like under the action of a catalyst to generate effective gas components such as CH 4 , CO, H 2 and C0 2 , a small amount of H 2 S and NH. 3, etc.
  • the coal residue that is not sufficiently reacted in the intermediate space B (catalytic gasification zone) enters the lower space C (residue gasification zone) of the multi-layer fluidized bed through the second overflow device, at 0 2 Gasification under the action of water vapor to generate gases such as CO, H 2 and C0 2 .
  • the lower space C (residue gasification zone) of the multi-layer fluidized bed the residue reacts with oxygen to generate a large amount of heat, and provides the required heat for the intermediate layer space B (catalytic gasification section), thereby reducing the ash carbon content, and Increasing the comprehensive utilization rate of the feed coal powder; meanwhile, in the lower space C (residue gasification zone), some of the catalyst is volatilized in a gaseous form to the intermediate layer space B (catalytic gasification zone) of the multi-layer fluidized bed, thereby The recycling of the catalyst in the fluidized bed is achieved.
  • the effect of this recycling of the catalyst in the fluidized bed is: it can reduce the amount of catalyst added in the initial pulverized coal, reduce the burden on the catalyst recovery system, and even eliminate the need to additionally arrange a catalyst recovery system; in the gasification zone of the gasifier residue (multilayer The CO and H 2 produced in the fluidized bed lower space C) can enter the multi-layer fluidized bed intermediate layer space B (catalytic gasification zone), and the decaneization reaction occurs under the action of the catalyst, thereby increasing the system decane production.
  • the generated high-temperature steam can provide partial heat to the catalytic gasification zone, thereby reducing the ash carbon content and improving the comprehensive utilization of the feed coal powder.
  • Partial pyrolysis zone, catalytic gasification zone and residue gasification zone of multi-layer fluidized bed gasifier can be divided into single layers according to the residence time and process operation conditions. Or multiple layers, each layer is separated by a gas distributor, and an overflow device is installed.
  • each overflow device may be a mechanical overflow device, such as a plug or valve at the lower end of the overflow device, or a pneumatically controlled overflow device such as a straight tube, a conical tube, or an L-shaped valve.
  • the projections of the upper and lower end outlets of each of the overflow devices are spaced apart from each other on a horizontal plane perpendicular to the longitudinal axis.
  • each of the overflow devices includes an upper section and a lower section, the upper section being parallel to the longitudinal axis, and the lower section and the longitudinal axis being shaped It is less than or equal to 60.
  • the angle between the upper section and the lower section is connected by a circular transition section.
  • the gas distributor of each of the overflow devices in the upper portion of the multi-layer fluidized bed may be a plate distributor, a tilt distributor or a funnel-shaped distributor, or a combination thereof.
  • the gas distributor 2 at the lower gas inlet of the multi-layer fluidized bed may be a flat plate distributor, a tilt distributor, a funnel-shaped distributor, or a gas distributor with a jet.
  • the multi-layer fluidized bed gasifier can be used under normal pressure and pressure.
  • the object of the present invention is to provide a multi-layer fluidized bed gasification furnace which is rich in decane gas by powder coal gasification, and the gasification furnace realizes continuous stable overflow between layers of fluidized bed through an overflow device, Pyrolysis, gasification, and combustion are coupled into a multi-layer fluidized bed to achieve fractional conversion, and energy distribution is performed centering on catalytic gasification and methane production to realize full-price development of coal resources.
  • the gasification reaction through the residue gasification zone of the lower bed space C of the multilayer bed supplies hydrogen and carbon monoxide to the catalytic gasification zone of the intermediate layer space layer B, thereby promoting the methanation reaction.
  • the decane generated in the pyrolysis section of the multi-layer bed space A directly escapes from the gasifier, thereby avoiding oxidation and increasing the methane content in the gas phase product, and at the same time, various other products such as tar formation by pyrolysis can be obtained. From a thermal point of view, make the most of it The thermal energy of the gas from the intermediate layer space B has a high thermal efficiency and also brings convenience to the subsequent processing system.
  • each overflow device since the projections of the upper end inlet and the lower end outlet of each overflow device on a horizontal plane perpendicular to the longitudinal axis are spaced apart from each other (for example, each overflow device adopts a partial inclined tube), for example, in the first overflow device.
  • the lateral distance between the lower outlet and the upper inlet of the second overflow device is maximized, so that the length of the lateral flow path of the material in each layer space is extended as much as possible, which can promote the fluidization reaction of the material to proceed more Sufficient, thereby effectively improving the overall efficiency of the fluidized bed.
  • the uppermost layer of the multi-layer bed will inhibit the formation of tar to promote the formation of tar, reduce the amount of catalyst, and reduce the cost of the catalyst; at the same time, some industrial waste can be used as a catalyst raw material to increase the methane content.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne un gazéifieur à lit fluidisé comprenant : un boîtier de gazéifieur (3); au moins deux couches de distributeurs de gaz (2) sous forme de plaques perforées, disposées perpendiculairement à l'axe longitudinal du boîtier et à différentes hauteurs le long de l'axe longitudinal, séparant ainsi l'espace intérieur en un espace supérieur (A), un espace intermédiaire (B) et un espace inférieur (C); un orifice d'entrée de matériau brut (4); un orifice de sortie de scories (7) et un orifice d'entrée d'agent gazéifiant formés sur le fond du boîtier; et un orifice de sortie de gaz de charbon formé sur le sommet du boîtier. Des premier et deuxième dispositifs de trop-plein (1) de forme tubulaire, ouverts aux deux extrémités, sont disposés respectivement à travers les premier et deuxième distributeurs de gaz. Ces dispositifs de trop-plein permettent l'écoulement du matériau brut du haut vers le bas, le long d'une ligne en zigzag. Le matériau brut s'écoule à partir de l'espace supérieur (A), à travers le premier dispositif de trop-plein, jusqu'à l'espace intermédiaire (B), puis de l'espace intermédiaire à l'espace inférieur (C) à travers le deuxième dispositif de trop-plein.
PCT/CN2010/001410 2009-09-14 2010-09-14 Gazeifieur a lit fluidise multicouche WO2011029285A1 (fr)

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CN 200910170387 CN102021038B (zh) 2009-09-14 2009-09-14 一种煤炭气化制取富甲烷气体的多层流化床气化炉
CN200910170387.4 2009-09-14
CN201010279560.7 2010-09-13
CN201010279560.7A CN102399595B (zh) 2010-09-13 2010-09-13 多层流化床气化炉

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