• 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:
    A two-step method and apparatus, according to the fluidized bed principle, for the production of coke, rich gas and pyrolysis tar, with the object of executing the method in a compact apparatus arrangement, with high energy efficiency and high throughput capacity. This is accomplished by a sequence in which the fine grains removed from the drying vapor mixture are removed from the actual pyrolysis process, and a hot gas, alien to the carbonization, is used as fluidization medium in the pyrolysis reactor, and with a hot gas-high performance separator being used for the dust separation from the pyrolysis gas, with the combustion exhaust gas produced in the combustion chamber being used for the indirect heating of the fluidization medium, for the pre-heating of the gas, which is alien to the carbonization, and for the direct heating in the dryer. The dryer has a double casing in the area of the fluidized bed, and a mixing chamber is arranged directly underneath its initial flow bottom, while the pyrolysis reactor is directly connected to the combustion chamber and the pre-heater.
    公开号:SU1731787A1
    申请号:SU847773298
    申请日:1984-02-07
    公开日:1992-05-07
    发明作者:Вольфганг Михель；Хайнц Пауль；Андреас Руммель；Геро Зеер；Манфред Оссовски；Ирмтруд Хеберлайн；Дитер Кестлер；Франк Вильгельм
    申请人:Феб Швермашиненбау "Карл Либкнехт", Магдебург (Инопредприятие)；
    IPC主号:
    专利说明:

    The invention relates to a two-step process of accelerated pyrolysis of brown coal of natural moisture, multi-ash and salt-containing, mostly soft brown coal, on the principle of a fluidized bed and installation for carrying out this process while producing high-quality coke, rich gas and pyrolysis resin with low dust content.
    A known method of processing brown multi-ash and salt-containing coals and a plant for its implementation (German patent No. 2553760, cl. С 10 В 49/10, 1978). In the known method, a three-step process is carried out aimed at
    simultaneous production of three main products - coke, gas and tar. In this case, the coal is dried in a pre-drier up to the smallest moisture residues and then separated in cyclones according to grain size, then fed further to the preheater at 300 ° C. The flue gas serves to heat up as a carrier gas. In subsequent cyclones, the coal, after preheating, is again separated from the carrier gas in a fluidized bed reactor. The treatment takes place at about 600 ° C, with the heat required for the process being supplied indirectly through a heat exchanger. As a heat carrier for indirect heating boiling
    h with
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    00 VI
    The layer serves as circulating carbon dioxide. Carbon dioxide is heated in the preheater to approximately 900 ° C and transfers its heat through a heat exchanger connected directly to the reactor to a fluidized bed and returns to a preheater at a temperature of approximately 650 ° C. In this process, an additional fluidized bed is supplied by supplying air to the combustion. The gas produced in the process, heated to 600 ° C, is used as a fluidizing gas.
    The disadvantages of the known method and installation are that they have high material and production costs, insufficiently high efficiency, as well as low gas productivity.
    The aim of the invention is to increase the efficiency of gas production, reduce the cost of the process, as well as simplify installation and reduce capital costs.
    The drawing shows an installation diagram for implementing the method.
    The installation includes a dryer 1, a fluidized bed reactor 2 equipped with a heat exchanger 3, a combustion chamber 4, a hydrocarbon-containing gas heater 5.
    The dryer 1 is equipped with a heat exchange jacket 6 located in the zone of the fluidized bed. The combustion chamber 4 and the heater 5 are connected to a heat exchanger 3 located in the reactor 2.
    The installation works as follows.
    The process is subdivided into two stages: drying soft brown coal with natural moisture (raw brown coal) and its pyrolysis with simultaneous production of coke, gas, and tar with a slight dust content. For this, soft brown coal is supplied from coal 7 to the upper part of dryer 1, coal being fed through any feed system. Dryer 1 consists of a gas distribution grid 8 on which a fluidized bed is formed. Mixed gas is used as fluidizing gas, to which gases from the dryer are added. The mixed gas is formed in the mixing chamber 9, located under the grill 8, as a result of burning the city gas with air and enters with a temperature of 350 ° C through the grill 8. The temperature produced in the fluidized bed is at most 200 ° C. In the dust separator 10, the dried brown coal dust is separated from the gases. Suitable fans keep the reaction conditions stable, especially the oxygen content and the overpressure. A high rate of heating, combined with the temperature and rate of flow of the boiling medium, is realized with the aid of a fluidized bed and provides the desired high consumption of coal and maintains the onset of oxidation of the coal load within the limits necessary to obtain high-quality final products: gas, coke and tar. At the same time, on the side of the edge of the fluidized bed, the heat resistance of the jacket 6 indirectly affects the heat resistance. This prevents carbon from sticking
    5 walls of the dryer or sintering of coal along the edges of the fluidized bed.
    Dried coal is discharged above grate 8 through an external dam and, using any feed system, is fed into
    0 an intermediate bunker 11. The remote dam serves simultaneously to adjust the height of the fluidized bed and, thus, to determine the duration of the coal in the fluidized bed. From the intermediate bunker 11, dried coal goes directly into the fluidized bed of the pyrolysis reactor 2, equipped with a gas distribution grid 12. Heat is supplied, first, indirectly, through
    0 heat exchanger 3, located in the fluidized bed, and, secondly, through a heated gas, for example, natural gas. It is heated in the preheater 5, located directly at the pyrolysis reactor 2, passes through
    5, the heat exchanger 3 and thus is thermally reduced, so that in the fluidized bed of the pyrolysis reactor 2 the reaction temperature is 550-600 ° C. Similar to the heater 5 to the pyrolysis reactor 2
    0 directly connected combustion chamber 4. Here city gas is combusted, turning into smoke with a temperature of 1300 ° C. From the combustion chamber 4, the hot flue gas passes through the pipe channels of the heat exchangers 3 and indirectly releases the heat to the fluidized bed. In the heater 5, the flue gas flows with a temperature of 900-950 ° C and serves here for indirect heating of the gas. In addition, flue gas is used as a component of the mixture for direct heating in dryer 1. The coke produced in the pyrolysis reactor 2 is removed in the same way as in dryer 1, through the outboard dam to the hopper 13, so that
    B and here the residence time of the coal in the fluidized bed depends on the removal of coke.
    The dust-containing vapor-gas mixture leaving the pyrolysis reactor 2 with a temperature of 4 ° C enters the dust separator 14 for a high-performance hot gas. The fine grain is separated and fed to the collection. The seaming resin is condensed in a special pre-and secondary refrigerators, taken in a special resin collection where it is stored.
    Compared with the known, the proposed method has the following advantages.
    All three products (gas, coke and tar) are produced simultaneously, of high quality, and in large quantities. At the same time, soft brown coals with natural moisture, multi-ash and salt-containing coals are subjected first to drying and then to accelerated pyrolysis according to the principle of a fluidized bed. The installation is compact, the devices are connected directly to each other in order to avoid the loss of heat and energy. During the drying process, the problem of sintering coal on the dryer wall in the fluidized bed zone was solved with the help of a heated double casing that maintains thermal stability in these marginal zones. Only fluid that is thermally recovered and leading to an increased gas yield is used as a boiling medium. Separating fine grains from a mixture of gases and vapors from a dryer leads to a decrease in the dust content of the gas and, after separating the smallest particles of dust, to a pyrolysis resin suitable for the preparation of coke for the production of graphite electrodes. The high energy efficiency of the process is achieved in particular by the fact that the flue gas obtained in the combustion chamber serves to indirectly heat the fluidized bed of the pyrolysis reactor, to preheat the gas and as a component of the mixture for direct heating in the dryer. The vapors arising in the dryer in the first stage of the process circulate, the sensible heat of coke in connection with its reactivity is used through the connection with the immediately following process, for example gasification, burning or coking.
    Charcoal loading of more than 2 t / m h is achieved with low technical installation costs and low investment costs. The amount of produced gas increases by 95% due to the removal of small particles from the process, after drying the dust content in the resulting gases and non-condensable resins is below 100 mg / nm, which leads to a decrease in the cost of cleaning the resin and gas and, consequently, the process becomes cheaper.
    Repeated use of flue gases provides an increase in efficiency compared with the prototype by 10%.
    权利要求:
    Claims (3)
    [1]
    1. A method of processing brown multi-ash and salt containing coals, including drying the coal in a fluidized bed with combustion products and circulating gas, separating small particles of coal from the exhaust grooves, heat treating the dried coal in a fluidized bed reactor heated by indirect heat exchange with gaseous coolant and fluidizing a heated hydrocarbon gas, the evolution of gases, tar and coke, burning
    gases in the combustion chamber and the heating of the hydrocarbon holding gas, characterized in that, in order to increase efficiency, gas productivity and reduce the cost of the process, after separation, small particles of coal
    the flue gases produced in the combustion chamber are fed successively as an intermediate coolant at the stage of coal heat treatment, heating of the hydrocarbon-containing gas and
    stage of drying.
    [2]
    2. A method according to claim 1, characterized in that methane-containing or natural gas is used as the hydrocarbon-containing gas.
    [3]
    3. An installation for processing brown multi-ash and salt-containing coal, including a dryer, a fluidized bed reactor equipped with a heat exchanger, a combustion chamber, a hydrocarbon-containing gas preheater, characterized in that, in order to simplify the installation of reducing capital costs, the fluidized bed zone, the combustion chamber and the heater are connected to the heat exchanger in the reactor.
    类似技术:
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    US2560767A|1951-07-17|Distillation of carbonaceous solids
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    同族专利:
    公开号 | 公开日
    AU559402B2|1987-03-12|
    AT384030B|1987-09-25|
    DE3344847C2|1986-10-30|
    DE3344847A1|1984-09-27|
    IN161909B|1988-02-20|
    DD227594A3|1985-09-18|
    US4533438A|1985-08-06|
    ATA78484A|1987-02-15|
    AU2552784A|1984-09-27|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DD48389A|
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    US3130133A|1959-05-04|1964-04-21|Harvey Aluminum Inc|Process for desulfurizing petroleum coke|
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    US3597327A|1969-04-02|1971-08-03|Arthur M Squires|Process for pyrolyzing a solid or liquid hydrocarbonaceous fuel in a fluidized bed|
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    DE2553760C3|1975-11-29|1978-11-09|Didier Engineering Gmbh, 4300 Essen|Process for carbonization of granular coal and system for carrying out this process|
    US4069024A|1977-05-09|1978-01-17|Combustion Engineering, Inc.|Two-stage gasification system|
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    US4421603A|1982-02-26|1983-12-20|Tosco Corporation|Process for recovering carbonaceous liquids from solid carbonaceous particles|DD237762A3|1984-01-30|1986-07-30|Schwermasch Liebknecht Veb K|METHOD AND APPARATUS FOR MULTI-STAGE TREATMENT OF ORGANIC SHOOTERS|
    AT389886B|1987-12-24|1990-02-12|Waagner Biro Ag|Process and apparatus for charring biomasses in two fluidization stages|
    DE4105127A1|1991-02-15|1992-08-20|Ver Energiewerke Ag|METHOD FOR TREATING BROWN COAL FOR GAS-STEAM COMBINATION PROCESSES|
    US5707592A|1991-07-18|1998-01-13|Someus; Edward|Method and apparatus for treatment of waste materials including nuclear contaminated materials|
    US5322530A|1992-10-20|1994-06-21|Western Research Institute|Process for clean-burning fuel from low-rank coal|
    JP3153091B2|1994-03-10|2001-04-03|株式会社荏原製作所|Waste treatment method and gasification and melting and combustion equipment|
    US7987613B2|2004-10-12|2011-08-02|Great River Energy|Control system for particulate material drying apparatus and process|
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    US8062410B2|2004-10-12|2011-11-22|Great River Energy|Apparatus and method of enhancing the quality of high-moisture materials and separating and concentrating organic and/or non-organic material contained therein|
    CN101921627B|2010-07-30|2013-03-13|陕西华祥能源科技集团有限公司|Air-oil co-production device forcoupling fluidized bed pulverized coal gasification and solid heat carrier pyrolysis and method therefor|
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    CN103666506A|2013-12-13|2014-03-26|北京蓝天利源科技有限公司|Feed coal pre-pyrolysis device for large-sized pulverized coal furnace|
    CN105258491B|2015-10-28|2017-07-04|北京国电龙源环保工程有限公司|For the weary Steam Dust and the process of water reclamation system of brown coal drying|
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    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DD83249079A|DD227594A3|1983-03-23|1983-03-23|FAST PYROLYSIS OF BROWN COALS AND ARRANGEMENT FOR IMPLEMENTING THE PROCESS|
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