SU898960A3 - Method of combusting solid carbon-containing fuel in fluidized bed - Google Patents

Method of combusting solid carbon-containing fuel in fluidized bed Download PDF

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Publication number
SU898960A3
SU898960A3 SU762395948A SU2395948A SU898960A3 SU 898960 A3 SU898960 A3 SU 898960A3 SU 762395948 A SU762395948 A SU 762395948A SU 2395948 A SU2395948 A SU 2395948A SU 898960 A3 SU898960 A3 SU 898960A3
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SU
USSR - Soviet Union
Prior art keywords
fluidized
combustion
inlet
fluidized bed
bed
Prior art date
Application number
SU762395948A
Other languages
Russian (ru)
Inventor
Ре Лотар
Хирш Мартин
Харальд Коллин Пер
Натанаэль Флинк Суне
Original Assignee
Металлгезельшафт Аг (Инофирма)
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Publication of SU898960A3 publication Critical patent/SU898960A3/en

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
    • B01J8/388—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
    • F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2206/00—Fluidised bed combustion
    • F23C2206/10—Circulating fluidised bed
    • F23C2206/101—Entrained or fast fluidised bed
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Carbon And Carbon Compounds (AREA)

Abstract

1510946 Fluidized-bed combustion METALLGES AG 9 July 1976 [5 Sept 1975] 28750/76 Heading F4B A process for combustion under approximately stoichiometric conditions in which carbonaceous material is fed through a lance 7 to a fluidized-bed reactor 1 which is fluidizedby gas supplied through an inlet 8 and by a secondary gas supplied through an inlet 2 or which can be supplied at a plurality of superimposed levels (2a-2d), Fig. 2 (not shown). At least the secondary gas contains oxygen for the combustion of the carbonaceous material in the fluidized bed. The volume ratio of fluidizing gas supplied at 8 to secondary gas supplied at 2 is in the range from 1 : 20 to 2 : 1 and the two gas supplies are adjusted so that suspension density of the fluidized bed above the inlet 2 level is in the range 15 to 100 Kg/M<SP>3</SP>. Solids entrained by the exhaust gas from the fluidized-bed are collected in the separator 6 and are recycled through a conduit 9 back into the reactor 1. Surplus solids produced are withdrawn through a conduit 10. Part of the heat of combustion is dissipated through cooling surfaces 3 in the space above the inlet 2 level. Other heat heat exchange surfaces may be located at positions 4 and 5 in the reactor and separator. Solids discharged from the conduit 10 may be fed to a fluidized-bed cooler 14, which is fluidized by oxygen containing gas which is then fed to the inlet 2. The cooler 14 has cooling registers 13 in which solids are cooled indirectly by gas supplied through a conduit 17 and later fed as fluidizing gas to the inlet 8. Part of this gas supply may be used for pneumatically feeding the carbonaceous material through the lance 7. The combustion process may be carried out under superatmospheric pressure.

Description

8 ти окном Во Сепаратор 7 подсоединен к котлу-утилизатору 9, а последний - к электрофильтру 10„ Сепаратор 7 и электрофильтр 10 трубопроводами 11 и 12 подсоединены к холодильнику 13 с кип щим слоем, который снабжен охлаждающимис  поверхност ми . Поверхности I подключены к трубопроводу 2, а холодильник 13 к трубопроводу 3. Способ сжигани  твердого углеродо содержащего топлива в кип щем слое осуществл етс  следующим образом. Топливо подаетс  в кип щий слой топки 1 по трубопроводу 4, а окислитель - двум  потоками по трубопроводам 2 и 3, расположенным один над другим, с отношением объемных расходов верхнего и нижнего потоков, равным 0, В зоне трубопроводов 2 и 3 образуетс  плотный кип щий слой, а над трубопроводом 3 плотност кип щего сло  поддерживаетс  равной 15-100 Топливо сгорает в кип щем слое топки 1, отдава  часть выделившегос  при сгорании тепла поверхност м нагрева 5 и 6 Продукты сгорани  совместно с твердыми частицами поступают в сепаратор 7, где происходит первичное отделение твердых частиц от газов и возврат их в слой через окно 8„ Далее продукты сгорани  поступают в котел-утилизатор 9, где они, охлажда сь, генерируют пар и затем в электрофильтр 10, где окончательно очищаютс  от пыли. По мере накоплени  твердого материала в слое часть его отводитс  по тру бопроводу 11 в холодильник 13 где материал охлаждаетс . Туда же отводи с  пыль, уловленна  в электрофильтреAn 8 window to the Separator 7 is connected to the recovery boiler 9, and the latter to the electrostatic precipitator 10 "Separator 7 and the electrostatic precipitator 10 by pipelines 11 and 12 are connected to the fluidized bed cooler 13, which is provided with cooling surfaces. The surfaces I are connected to the pipeline 2, and the cooler 13 to the pipeline 3. The method of burning solid carbon-containing fuel in a fluidized bed is as follows. The fuel is supplied to the fluidized bed of the furnace 1 through line 4, and the oxidant is supplied by two streams through pipelines 2 and 3, one above the other, with the ratio of the volume flow rates of the upper and lower flows equal to 0. In the area of pipelines 2 and 3, a dense dense boiling fuel is formed. layer, and above the pipeline 3, the fluidized bed density is maintained at 15-100. The fuel burns in the fluidized bed of the furnace 1, giving up part of the heat released during the heating of heating surfaces 5 and 6. The combustion products, together with solid particles, enter the separator 7, where fuel is produced. between primary separation of solids from the gases and return them in the window layer 8 "Next, the combustion products enter the heat recovery boiler 9, where it by cooling to, generate steam and then into the precipitator 10, where finally cleaned from dust. As the solid material accumulates in the layer, part of it is discharged through pipe 11 to cooler 13 where the material is cooled. There also take away from the dust caught in the electrostatic precipitator

10„ Дл  утилизации тепла материала, поступающего в холодильник 13, охлаждение осуществл етс  потоками окислител , поступающего в топку 1. Нижний поток окислител  перед поступлением его в трубопровод 2 проходит охИсточники информации, прин тые во внимание при экспертизе10 "To recover the heat of the material entering the cooler 13, the cooling is carried out by oxidant flows entering the furnace 1. The lower oxidizer flow before entering it into the pipeline 2 passes through the source of information taken into account during the examination

Claims (1)

К Гельперин Н.И. и др. Основы техники псевдоожижени . М-, Хими , 1967, с. k2k. 4 лаждающиес  поверхности 14 холодильника 13. Верхний поток служит псевдоожижающим агентом кип щего сло  холодильника 13. Подача потоков окислител  с соотношением объемов верхнего к нижнему равным 0, и поддержание плотности кип щего сло  в зоне топки 1, расположенной над верхним потоком окислител , равной 15-100 кг/м, обеспечивает хорошее зажигание твердого топлива в нижней части сло , высокие значени  коэффициентов теплопередачи к охлаждающим поверхност м нагрева 5 и 6 и равномерность температур в слое. Все это интенсифицирует сжигание топлива , так как устран ет козлообразование , локальное превышение температур и улучшает выжиг топлива Формула изобретени  Способ сжигани  твердого углеродосодержащего топлива в кип щем слое путем подачи в последний верхнего и нижнего потоков окислител  и двух расположенных одна над другой поперечных плоскост х и подвода твердого топлива между последними, с одновременным отводом тепла от зоны сжигани , рас положенной над верхним потоком окислител , и возвратом уноса топлива в слой, отличающийс  тем, что, с целью повышени  эффективности путем интенсификации сжигани , отношение объемных расходов верхнего и нижнего потоков окислител  составл ет соответственно 0,5-20, а плотность кип щего сло  в зоне, расположенной « верхним потоком окислител , поддерживают равной 15-100 кг/м.K Gelperin N.I. and others. Fundamentals of fluidization. M-, Himi, 1967, p. k2k 4 adjacent surfaces 14 of the refrigerator 13. The upper stream serves as a fluidizing agent of the fluidized bed of the refrigerator 13. The flow of oxidant with the ratio of the volumes of the upper to the lower is 0, and maintaining the density of the fluidized bed in the zone of the furnace 1 located above the upper oxidant stream of 15- 100 kg / m ensures good ignition of solid fuel in the lower part of the layer, high values of heat transfer coefficients to the cooling heating surfaces 5 and 6, and uniform temperature in the layer. All this intensifies the combustion of fuel, as it eliminates goat formation, local overheating and improves fuel burning. Claims The method of burning solid carbon-containing fuel in a fluidized bed by feeding the upper and lower oxidant streams and two transverse planes one above the other and supplying solid fuel between the latter, with simultaneous removal of heat from the combustion zone, located above the upper oxidant stream, and return of the entrainment of fuel to the layer, characterized by that, in order to increase efficiency by intensifying combustion, the ratio of the volumetric flow rates of the upper and lower oxidant flows is 0.5–20, respectively, and the density of the fluidized bed in the zone located by the “upper oxidant flow is maintained at 15-100 kg / m .
SU762395948A 1975-09-05 1976-09-03 Method of combusting solid carbon-containing fuel in fluidized bed SU898960A3 (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE2539546A DE2539546C3 (en) 1975-09-05 1975-09-05 Process for incinerating carbonaceous materials

Publications (1)

Publication Number Publication Date
SU898960A3 true SU898960A3 (en) 1982-01-15

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ID=5955703

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SU762395948A SU898960A3 (en) 1975-09-05 1976-09-03 Method of combusting solid carbon-containing fuel in fluidized bed

Country Status (15)

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JP (1) JPS5233132A (en)
AU (1) AU500206B2 (en)
BE (1) BE845872A (en)
CA (1) CA1057584A (en)
CS (1) CS212255B2 (en)
DD (1) DD126526A5 (en)
DE (1) DE2539546C3 (en)
ES (1) ES451239A1 (en)
FR (1) FR2323101A1 (en)
GB (1) GB1510946A (en)
IN (1) IN143376B (en)
RO (1) RO86704B (en)
SE (1) SE424225C (en)
SU (1) SU898960A3 (en)
ZA (1) ZA763293B (en)

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DE3306795C1 (en) * 1983-02-26 1983-12-15 L. & C. Steinmüller GmbH, 5270 Gummersbach Process for binding sulfur compounds, which are formed as reaction products when burning sulfur-containing fuels in a furnace by adding additives
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Also Published As

Publication number Publication date
ES451239A1 (en) 1977-09-16
DD126526A5 (en) 1977-07-20
SE424225B (en) 1982-07-05
SE7609676L (en) 1977-03-06
RO86704A (en) 1985-04-17
BE845872A (en) 1977-03-03
DE2539546A1 (en) 1977-03-17
FR2323101A1 (en) 1977-04-01
AU1572476A (en) 1978-01-12
RO86704B (en) 1985-05-01
AU500206B2 (en) 1979-05-10
CS212255B2 (en) 1982-03-26
JPS5728046B2 (en) 1982-06-14
DE2539546B2 (en) 1980-11-27
IN143376B (en) 1977-11-12
SE424225C (en) 1990-09-10
FR2323101B1 (en) 1982-10-01
DE2539546C3 (en) 1985-10-24
GB1510946A (en) 1978-05-17
CA1057584A (en) 1979-07-03
ZA763293B (en) 1977-05-25
JPS5233132A (en) 1977-03-14

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