• 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:
    The invention relates to the production of cement and can be used in the heat treatment of the cement-raw mix by the dry method. The aim of the invention is to intensify the process. In the inventive method, a part of the exhaust gas flow from the furnace furnace is sent to the calciner, and another part is mixed with a part of the exhaust gas flow from the calciner before the heat exchanger stage located directly in front of the calciner, and the mixed stream is fed to one branch of heat exchangers, and the other part of the gas exhaust from the calciner is directed to another branch. 1 nl 8 IQ O) with two co 4; o ate cm
    公开号:SU1299495A3
    申请号:SU823505249
    申请日:1982-10-26
    公开日:1987-03-23
    发明作者:Файге Фритц；Креннбауэр Франц
    申请人:Фоест-Альпине (Фирма)；Феб Швермашиненбау-Комбинат,"Эрнст Тельманн",Магдебург (Инопредприятие)；
    IPC主号:
    专利说明:

    1129
    The invention relates to the building materials industry, primarily to methods for producing cement clinker.
    The aim of the invention is to intensify the process.
    The drawing shows a device for implementing the proposed method.
    The device contains a loading pipe 1, a tubular rotary kiln 2, a calciner 3, the first parallel branch of the heat exchanger 4, consisting of blocks 5-8 of the heat exchanger, made in the quality of cyclones, the second parallel branch of the heat exchanger 9, consisting of blocks 10-12 heat

    gas pipes, piping 13 and 14 for exhaust gas, exhaust piping 15 and 16, inlet piping 17, separator 18, cooler 19, piping 20 located between the furnace flue gas pipe and calciner 20, spool 21, fan 22. "
    The method is carried out as follows.
    The raw material 1), the flow pattern of which is indicated by dash-dotted lines, is led through feed pipe 1 to a multi-stage heat exchanger, which is heated with exhaust gas from a rotary tube furnace 2 for firing pre-heated and calcined raw powder and with exhaust gas from a calciner 3 located in front of the rotary tube furnace 2. This heat exchanger has two parallel branches 4 and 9 for the exhaust gas,. which are formed on the one hand from heat exchanger blocks 5-8, made as cyclones, and on the other hand from heat exchanger blocks 10-12.
    As can be seen from the flow pattern for the exhaust gas flows (shown by solid lines), the branches 4 and 9 for the exhaust gas are connected to the pipelines 13 and 14 for the exhaust gas rotating, it is the tubular furnace 2 and the calciner 3. The raw powder is gradually heated by the exhaust gases from the rotating the tubular furnace 2 to the calciner 3, and the exhaust gas is alternately directed here and there between: waiting for the heat exchanger blocks of both branches 4 and 9 of the spent
    O
    five
    O
    five
    0
    gas, since the exhaust pipes 15 of the heat exchanger blocks of each of the branches are connected to the inlet pipes 17 of another branch up to the heat exchanger block 5, the exhaust pipe 16 of which flows into the calcinator 3. The raw powder, neutralized in the calcinator 3, together with the exhaust gas is discharged from the calciner 3 and supplied to a separator 18 in which the raw powder is separated from the exhaust gas and immediately thereafter is supplied to the rotary tube furnace 2. Additional heat, necessary to remove the acid is obtained by burning fuel in a calciner, and the quality of the combustion air is a portion of the heated cooling air from the cooler 19 located after the rotating tube furnace 2, in which the raw powder is burned, calcined in the furnace 2 and turned into cement clinker . Another portion of the cooling air from the cooler 19 is supplied as combustion air to the rotary kiln 2.
    0
    Thus, by adding a portion of the waste stream to the exhaust gas calciner, to the stream of exhaust gases coming from the furnace
     For both branches of the exhaust gas, equal amounts of exhaust gas are provided, which allows the same heat exchanger blocks to be used for both branches of the exhaust gas and, therefore, ensures matching (identical) conditions in these branches of the exhaust gas. As a result, not only equipment costs are reduced, but the thermal coefficient of efficiency is also improved, since even under the same conditions, the temperature at the exit of exhaust gases depends on the ratio of the masses between the raw powder
    P and exhaust gas, and the entire stream of green powder indigid (whole) can be fed to one heat exchanger block of the heat exchanger. Due to the largely coinciding conditions for both branches of the exhaust gas, a common fan (compressor, blower) can be used. In addition, by adding a portion of the waste stream from the cal
    The exhaust gas scavenger to the exhaust gas flow from the kiln is diluted with respect to the concentration of ballast materials in the exhaust gas from the kiln, which greatly reduces the risk of overburning.
    Matching conditions in both branches of the exhaust gas can also be provided provided that part of the hot stream of exhaust gas from the furnace is before the part of the stream of exhaust gas from the calciner is supplied to the calciner. At the same time in the branch of the calciner there is a mixed stream of exhaust gas, which further reduces the concentration of ballast substances. In addition, by regulating a portion of the waste gas exhaust stream from the furnace, the exhaust gas supplied to the calciner, stable conditions can be provided for preheating and neutralizing the raw powder, when, due to fluctuations in furnace operation, the amount and temperature of the exhaust gases are used. waste from the furnace. Since the calciner under
    only a part of the waste stream is spent - 3b and with the fact that, for the purpose of intensification: 1x from the exhaust gas furnace, and the prevailing share of the gas flow supplied to the calciner consists of heated air, the exhaust gases from the furnace are the calcination process has virtually no adverse effect.
    In order to be able to use the higher temperature of the exhaust gases from the kiln, for high

    Heating the raw powder, it may be in front of the heat exchanger stage, located directly in front of the calciner, brought to the hot exhaust gas flow from the furnace, before the exhaust gas flow from the kiln is mixed with a portion of the exhaust gas flow from the calcinator. Then, together with the mixed stream, which, with respect to the exhaust gas leaving the furnace, has an insignificant temperature, the raw powder is sent to the last heat exchanger stage in the direction of the scientific research institute for moving the unbaked powder before it enters the calciner.
    权利要求:
    Claims (1)
    [1]
    Invention Formula
    The cement clinker production method by preheating the raw mix with waste gases in two parallel branches of cyclone heat exchangers, with the raw mix flow alternately directed from one branch to another, decarbonating in a calciner and roasting in a rotary kiln, distinguishing process sification, one part the waste gas stream from the furnace is sent to the calciner, and the other is mixed with a part of the gas stream outgoing from the calciner in front of the heat exchanger stage, located directly in front of a calciner, with the mixed stream being fed to one branch of the heat exchangers, and the second part of the stream from the calciner gases to the other branch.
    类似技术:
    公开号 | 公开日 | 专利标题
    CA1036814A|1978-08-22|Apparatus for calcining cement
    KR930005296B1|1993-06-17|Process for the heat treatment of fine-grained material
    US4514170A|1985-04-30|Apparatus for the heat treatment of fine-grained material
    US4298393A|1981-11-03|Method and system for burning fine-grained material, particularly for the manufacture of cement clinkers
    US4381916A|1983-05-03|Method and apparatus for roasting fine grained ores
    US4022568A|1977-05-10|Method and apparatus for heat treating pulverous raw materials
    GEP20032952B|2002-12-10|Method and Apparatus for Producing Cement Clinker
    US4211573A|1980-07-08|Method and apparatus for the production of cement clinker low in alkali from alkali-containing raw material
    SU1299495A3|1987-03-23|Method for producing cement clinker
    CA2403564A1|2001-10-04|Method and apparatus for manufacturing cement clinker from particulate cement raw material
    US4392822A|1983-07-12|System for burning fine-grained material, particularly for the manufacture of cement clinkers
    GB1506863A|1978-04-12|Installations for the manufacture of cement by the dry process
    KR860001645B1|1986-10-15|Process and apparatus for producing cement
    US4191586A|1980-03-04|Method and apparatus for reducing the calorific consumption of a cement producing plant
    SU1426450A3|1988-09-23|Method of producing cement clinker
    DK151873B|1988-01-11|PLANT FOR HEAT TREATMENT OF CEMENTRAMEL
    SU737381A1|1980-05-30|Method and device for cement clinker annealing
    SU359490A1|BAKED THERMAL EXCHANGE DEVICE
    SU665824A3|1979-05-30|Apparatus for heat treatment of loose material
    SU976265A1|1982-11-23|Installation for heat treatment of fine material
    SU1694508A1|1991-11-30|Method of heat treatment of powdered material
    SU552489A1|1977-03-30|Device for heat treatment of bulk material
    EP0030409A1|1981-06-17|Method of and plant for manufacturing pulverous or granular material, for example cement
    SU1735688A1|1992-05-23|Cement clinker calcination plant
    RU2076291C1|1997-03-27|Device for thermal treatment of powder-like material
    同族专利:
    公开号 | 公开日
    UA5762A1|1994-12-29|
    DK472982A|1983-04-28|
    CS247069B2|1986-11-13|
    EP0078250B1|1984-07-11|
    DK156509C|1990-01-29|
    DK156509B|1989-09-04|
    YU239982A|1985-04-30|
    US4431453A|1984-02-14|
    ES8401000A1|1983-12-01|
    EP0078250A1|1983-05-04|
    MD53C2|1995-03-31|
    SI8212399A8|1996-06-30|
    RO88458A|1986-01-30|
    ES516569A0|1983-12-01|
    IN157895B|1986-07-19|
    HRP940744B1|1996-12-31|
    DE3260374D1|1984-08-16|
    MD53B1|1994-08-31|
    YU42810B|1988-12-31|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2466950C2|2006-11-13|2012-11-20|Лафарж Са|Method for production of cement|GB960863A|1960-09-13|1964-06-17|Dessau Zementanlagenbau Veb|Process for the calcination of raw silicate material|
    JPS4942716A|1972-08-31|1974-04-22|
    CH601128A5|1973-11-08|1978-06-30|Ishikawajima Harima Heavy Ind|Cement powder preheating|
    FR2281333B1|1974-08-05|1979-03-09|Fives Cail Babcock|
    CS179624B1|1975-04-30|1977-11-30|Jiri Filous|Method of firing a cement clinker and arrangement for utilization of this method|
    SE7604394L|1976-04-14|1977-10-15|Cementa Ab|WAY TO CALCINATE FRAMEWORK FOR CEMENT MANUFACTURE AND PRECALCINATOR FOR EXERCISE OF THE SET|
    DE2712239C2|1977-03-21|1984-05-10|Klöckner-Humboldt-Deutz AG, 5000 Köln|Method and device for the production of low-alkali cement clinker from alkali-containing raw material|
    JPS5748254B2|1978-08-04|1982-10-15|
    AT365772B|1979-10-19|1982-02-10|Voest Alpine Ag|METHOD FOR PRODUCING CEMENT AND SYSTEM FOR CARRYING OUT THE METHOD|
    AT365160B|1979-11-21|1981-12-28|Voest Alpine Ag|METHOD AND DEVICE FOR CALCINATING CEMENT FLOUR|DE3319083A1|1983-05-26|1984-11-29|Klöckner-Humboldt-Deutz AG, 5000 Köln|METHOD AND DEVICE FOR PRODUCING LIME-BASED BINDERS, IN PARTICULAR CEMENTS|
    DE3333718A1|1983-09-17|1985-04-04|Klöckner-Humboldt-Deutz AG, 5000 Köln|PLANT FOR BURNING FINE-GRAINED GOODS, PARTICULARLY TO CEMENT CLINKER|
    AT381694B|1985-01-11|1986-11-10|Voest Alpine Ag|METHOD AND DEVICE FOR THERMALLY TREATING FINE-GRAINED GOODS, IN PARTICULAR FOR BURNING CEMENT FLOUR|
    DE102005052753A1|2005-11-04|2007-05-10|Polysius Ag|Plant and process for the production of cement clinker|
    MD354Z|2010-11-09|2012-06-30|Андрей СМОЛЕНСКИЙ|Coupler of the single-bottom plow with a motor hoe|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DD81234385A|DD203528B1|1981-10-27|1981-10-27|DEVICE FOR CALCINATING CEMENT GROOVE|
    AT0488281A|AT376649B|1981-11-13|1981-11-13|METHOD FOR PRODUCING CEMENT AND DEVICE FOR CARRYING OUT THE METHOD|MD94-0072A| MD53C2|1981-10-27|1994-04-05|Process for cement clinker production|
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