• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Invention m. used to produce high steam parameters in fluidized bed steam generators. The purpose of the invention is to demonstrate the efficiency of combustion. The fuel and primary air are supplied to form the primary combustion zone, the fuel is partially oxidized and the oxidation products are cleaned on the solid particles of an alkaline sorbent to produce a reducing gas and sulfur-containing particles. Then, the gas and secondary air are supplied to form the secondary combustion zone, the gaseous components are separated from the solid ii. Separate solid particles and combustion products with a low sulfur content downstream of the secondary zone are removed. The alkaline sorbent is introduced into the primary combustion zone, at the exit of the cut, particles containing alkaline sulfate, alkaline oxide and alkaline sulfide are obtained, to-rye then fed to the secondary combustion zone. After separation and removal of the combustion products, additional air is supplied to the stream of solid particles with the formation of an oxidation zone of the particles, where the alkaline sulphide contained in them is converted into alkaline sulphate, after which part of the particles are returned to the primary combustion zone. 10 hp f-ly, 1 ill. g with 4 00 00 el ka a
    公开号:SU1438626A3
    申请号:SU864027058
    申请日:1986-02-28
    公开日:1988-11-15
    发明作者:Д.Фрейли Лоуэлл；Хсяо Ке-Хсиен；Лин Юнг-Йи；Садхукхан Пасупати
    申请人:Дзе М.В.Келлог Компани (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to the energy sector and can be used to obtain high parameters steam in fluidized bed steam generators.
    The aim of the invention is to increase the combustion efficiency.
    The drawing shows a system in which the described method can be implemented.
    The system comprises a vertical one to one, a crossover 2 and a short circulation pipe 3 for the flow of solid particles. Vertical one hundred to one has an outlet 4, a solid particle, 5 air spraying for fluidization of a dense bed 1, an evaporative coil 7, an inlet 8 for intake of primary air and an inlet 9 for secondary air. The inlet 8 goes into the gas and solid particles mixing section 10 formed by restrictive orifices 11 made of refractory insulation. The restrictive orifices 111 divide the vertical one hundred to one into a dense fluidized bed 6, section 10 and section 12 of the flow with a structured core. The system additionally contains a primary separator 13 i cyclones 14. Cyclones 14 are designed to remove the hot gas heated through the annular pipe 15 for heat exchange and gas cleaning. The primary separator -13 and cyclones 14 are connected to the vertical pipe 16, in which the continuation is tight — I o layer 6 to the restrictor neck 17; the air inlet 18 in the lower part of the vertical fflbi 16 serves to output the oxidative io gas to the area of oxidation and solid btx. particles.
    I Example. The system operates in the Pittsburgh bituminous stone, coal number 8, containing 4.3 wt.% 4era | 8.5 wt.% Ash; 3.3% by weight of water and milled into particles with an average size of 50 μm, and Greer limestone and the quality of fresh alkaline sorbent for sulfur capture, containing 90% by weight of cadmium carbonate, ground to particles with an average size of 30 μm .
    I 2.1 kg / .c of coal and 0.47 kg of festoon are mixed with 16.3 kg / s of air and injected into the mixing section 10 through the inlet

    8. Approximately 97% by weight of coal is burned in a mixing section 10 under partial oxidation conditions at 900 ° C and a pressure of 1.15 kg / cm to obtain a flow of reducing gas passing through the upper neck 11 and having the following composition, mol% :
    Oxygen
    Nitrogen. 68.9
    Dioxide
    carbon13,7
    Carbon monoxide.
    S
    five
    0 | Q
    0
    five
    45
    50
    55
    Hydrogen sulfide, part per thousand N0, part
    6.3
    2.8
    1510 74
    on thu
    Dioxide
    sulfur, part
    .a thousand chuo
    The turbulence conditions in section 10 provide about 978 kg / s of oxidized solid particles from the dense layer 6. The solid particles are 52 wt.% CaSO, 14 wt.% CaO and contain traces of CaCO and 32 wt.% ash and inert substances. A mixture of gas and solid particles passes upward through the vertical one hundred to 1 in the form of a stream with a structural core with a gas velocity of 13.7 m / s, with a density of solid particles of about 16 kg / m and a flow rate of 979 kg / s, measured in the vertical stand 1 at a point below the inlet 9. At this point, the partial oxidation of the coal is almost complete, almost all the sulfur components in the coal are isolated as hydrogen sulfide and reacted with a small amount of calcium oxide in the trapped solids to form calcium sulfide. Due to the fact that the feed rate of the fresh material is low compared to the circulation rate of solid particles in the system, the calcium sulfide content in the captured solid particles is a weight percentage. The gas is little different in composition from the gas in the code from section 10, only the hydrogen sulfide content is reduced to 65 hours per thousand.
    Through the inlet 9 into the vertical one hundred to one 7.6 kgUs are introduced.
    secondary air, which is sufficient to oxidize the rest of the coal and the components of the reducing gas, however, due to insufficient residence time in the crossover 2 and the circulation pipe 3, the calcium sulfide component in the trapped particles is not sufficiently oxidized. Under these conditions, the combustion gas stream entering the primary separator 13 from the secondary combustion zone has the following composition, mol%:
    Oxygen Nitrogen
    Carbon dioxide Carbon monoxide Hydrogen sulfide NOj ,, part
    1.9
    74.1
    14.7
    Traces 0.0 0.0
    43
    99
    per thousand chu Sulfur dioxide, part per thousand chu
    Combustion gas is separated from trapped solids in primary separator 13 and cyclones 14. Primary separator 13 removes about half of the solid particles. The combustion gas has a temperature of about 900 ° C and flows through the nozzle 15 at a speed of 25.7 m / s.
    Separated solid particles containing calcium sulfide descend from the separator 13 and cyclones 14 to the upper part of the vertical pipe 16, forming a dense fluidized bed. Through the inlet 18, 0.8 kg / s of air is introduced to oxidize almost all the calcium sulphide to calcium sulphate in the oxidation zone in the vertical pipe 16. A dense fluidized bed with a capacity of 641 kg / m is used, the gas velocity is 0.6 m / s, which provides a residence time of solid particles in the oxidation zone of 32 s. When the temperature of the vertex pipe 16 is equal, sulfur dioxide forms little or not formed at all. The oxidized solids pass through the bottom of layer 6, close the circulation loop, and 0.66 kg / s of oxidized solids are blown out of the outlet 4 to remove ash and calcium sulphate from the system. The remaining part of the oxidized solid particles passes
    0
    0
    It is fed to the evaporation coil 7 and around it and is recycled to the mixing section 10.
    权利要求:
    Claims (11)
    [1]
    1. The method of burning sulfur-containing fuel in a fluidized bed system by supplying fuel
    and primary air to form a primary combustion zone, partial oxidation of fuel and purification of oxidation products on solid particles of an alkaline sorbent to produce a reducing gas and sulfur-containing particles, supply of gas and secondary air to form a secondary combustion zone, separated by gaseous co-axes g: r.-l 1 of those who suffer from solids and the removal of individual solid particles and combustion products with a low sulfur content after the secondary zone, that is, so that, in order to 5 and 3)}), p (Christmas tree sorbent is introducedthe primary combustion zone, at the exit of which there are obtained particles containing alkaline sulfate oxide n sulfide, which are then in the secondary combustion zone, and after separating and discharging the combustion products, additional air is fed into the stream of solid particles, forming an oxidation zone of particles, where the contained they contain alkaline sulphide to alkaline sulphate, after which part of the particles are returned to the primary combustion zone.
    [2]
    2. A method according to claim 1, wherein the sulfur containing fuel and alkaline sorbent are introduced into the lower part of the primary combustion zone.
    five
    0
    [3]
    3. The method according to p. 2,
    about tl and h and 45
    50
    55
    This is because the primary air is supplied in the amount of 40-95% of stoichiometric to the lower part of the primary combustion zone.
    [4]
    4. The method according to claim 1, about tl and h and y and with the fact that in the primary combustion zone maintain a temperature of 650- and a pressure of 1-2 kg / cm.
    [5]
    5. A method according to claim 2, characterized in that all the oxygen of the primary air is oxidized in the primary combustion zone, and the amount of molecular oxygen in the gaseous medium in the secondary combustion zone is 1-8 mol%.
    five
    [6]
    6. The method according to nij. 1 and 3, characterized in that the total amount of air supplied to the primary and secondary combustion zones is maintained at 100-130% of stoichiometric.
    [7]
    7. The method according to claim 1, about 10 and with the fact that
    tons of l and h - the zone of oxidation of solid particles support the regime of fluidization at 590–985 ° C and the residence time of solid particles in it 1–30 s.
    [8]
    8. A method according to claim 2, characterized in that the density of the fluidized bed in the lower part of the primary combustion zone is maintained at 320-960 kg / m.
    that
    layer density at the top
    and zoE.
    4386266
    [9]
    9. The method according to claim 1, characterized by the fact that the fluidized bed
     parts of the primary combustion zone
    non-secondary combustion is maintained at 8-320 kg / m.
    [10]
    10. The method according to claim. 9, about t l and h
    This is due to the fact that the gaseous components pass through the primary combustion zone for 1-3 seconds.
    [11]
    11. A method according to claim 9, characterized in that the mass ratio of the solid particles returned to the primary combustion zone and the alkaline sorbent is maintained at 200 to 10,000, and the particles and sulfur-containing fuel are 100 to 3300.
    15
     Sosch-go
    W
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    EG17736A|1991-06-30|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    US06/707,252|US4579070A|1985-03-01|1985-03-01|Reducing mode circulating fluid bed combustion|
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